Vol 1 of 1 - Plant Operation Maintenance and Safety Manual

4 A b u D h a b i G a s Industries L t d .

Abu Dhabi Gas Industries Ltd. GASCO Project No. 5221 Ethane Recovery Maximization Project

DIVISION 10 PLANT OPERATION, MAINTENANCE AND SAFETY MANUAL

Volume 1 of 1

FLUOR Contract AOWT 2004

Fluor Mideast, Ltd. Contract No. AOWT

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the E R M Project - Rev. 1

GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-001

ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Operating, Maintenance and Safety Manual Addendum for the ERM Project

Approved Rev.

Date

Description

By

Chk.

Disc.

Proj.

20-Dec-04

Client Comments Incorporated

DTS

DTS

RvdV

MS

26-Sept-04

Issued for Review

DTS

DTS

RvdV

MS

GASCO


Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project - Rev. 1


Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project T A B L E OF CONTENTS

INTRODUCTION CHAPTER 1:

DESIGN BASIS

CHAPTER 2:

PROCESS DESCRIPTION

CHAPTER 3:

INITIAL START-UP

CHAPTER 4:

NORMAL START-UP

CHAPTER 5:

NORMAL OPERATION

CHAPTER 6:

NORMAL SHUTDOWN

CHAPTER 7:

EMERGENCY SHUTDOWN

CHAPTER 8:

SAFETY

CHAPTER 9:

EQUIPMENT AND DATA SHEETS

CHAPTER 10:

DRAWINGS




INTRODUCTION

CONTENTS

SECTION

PAGE

1.0

FOREWORD

2

2.0

PROJECT OVERVIEW

3

INTRODUCTION


1.0



FOREWORD This manual describes the modifications made to Unit 44 for the Ethane Recovery Maximization (ERM) Project. This manual should be read in conjunction with the existing Unit 44 Operating, Maintenance and Safety Manual and the supplement prepared for the C2 Enhancement Project (Project 1219). The information contained in this manual provides a basis for the safe start-up, normal operation, normal shutdown, and emergency shutdown for the new equipment and systems. The manual provides a description ofthe new E R M operating modes and discusses how the new systems are integrated into the existing unit. The procedures described in this manual should be considered as guidelines and may have to be adapted at site. It is the prime responsibility of the Operations personnel to interpret the instructions and where necessary adjust them to suit the conditions prevailing at any time taking into account the local conditions during the preparation and commissioning of the new E R M extension. In order to facilitate assimilation and understanding of information, the format and contents of this manual follow that of the existing Operating, Maintenance and Safety Manual.

INTRODUCTION


2.0



PROJECT OVERVIEW The objective of the E R M Project was to increase the ethane production from Unit 44 by at least 400 TPD based on the design feed rate, composition, and inlet conditions defined in the Design Basis Memorandum. C2 recovery is increased in Unit 44 by adding the following new equipment: • • • • • •

Cold Demethanizer (44-V-308) Cold Demethanizer Bottoms Pumps (44-P-302A/B) 2 Feed Chiller (44-E-318) Debutanizer Trim Condenser (44-E-406) N G L Subcooler (44-E-407) Propane Refrigeration Package (44-ME-201) nd

The new Refrigeration Package includes a two-stage Refrigeration Compressor (44-C-202) with an electric motor driver. An existing air cooler purchased for a previous project is used as the Refrigerant Condenser (44-E-203) for the new system. The package also includes two K O drums (44-V-206/207) and two subcooling exchangers (44-E-204/5).

INTRODUCTION


3.0



PURPOSE The puipose of this addendum is: •

To review and explain the modifications that have been made to the existing unit and update, as required, the process description and the start up and shutdown procedures.

•

To provide the procedure to switch from C2 Enhancement mode to E R M mode.

•

To provide the procedure to switch from E R M mode to lower ethane recovery modes.

•

Provide details for the normal operation ofthe E R M mode.

INTRODUCTION

Fluor Mideast, Ltd. ContractNo. AOWT



CHAPTER 1

DESIGN BASIS

CONTENTS

SECTION 1.0

2.0

PAGE

GENERAL

2

1.1

2

Integration of E R M Project into Existing Facilities

FEED CHARACTERISTICS

3

2.1 2.2

Feed Gas Flow and Conditions Feed Gas Composition

3 4

2.3

Flexibility and Turndown

4

3.0

PRODUCT SPECIFICATIONS

5

4.0

3.1 Lean Gas 3.2 N G L 3.3 C5+ Condensate EFFLUENTS

5 5 5 6

5.0

PRINCIPLES OF OPERATION 5.1 5.2 5.3 5.4

Feed Chilling Demethanizer / Recycle Gas Loop Debutanizer New Propane Refrigeration System

7 7 7 8

6.0

PROCESS FLOW DIAGRAMS AND MATERIAL BALANCES

7.0

UTILITY REQUIREMENTS

10

8.0

CHEMICALS AND CONSUMABLES

11

CHAPTER 1

9



1.0


GENERAL A comprehensive Design Basis Memorandum containing mutually agreed and approved compilations of basic data, design criteria, and other parameters was developed for the ERM Project. The key information is provided in this section ofthe manual. Refer to RPT-AOWT44-06-001 for additional data.

1.1

Integration of ERM Project into Existing Facilities OGD-I Train 3 was commissioned in 1996 and processes approximately 610 MMSCFD of Thammama-F gas. The train consists of condensate stabilization (Unit 24), M D E A sweetening (Unit 34), molecular sieve dehydration of gas, and deep-NGL recovery by propane chilling followed by a turboexpander-based unit (Unit 44). OGD-I Train 3 was originally designed to produce a N G L stream containing a minimum quantity of ethane (maximum 5 mol %). However, in 2001, the unit underwent some modifications to recover about 300 TPD of total C2 (known as C2 Enhancement Project) to supplement the feed to the petrochemical plant at Ruwais. The objective ofthe E R M Project was to further increase the ethane production from OGD-I Train 3 by at least 400 TPD based on the design feed rate, composition, and inlet conditions defined in the Design Basis Memorandum. Within OGD-I Train 3, the focus ofthe E R M Project was entirely on Unit 44. No modifications were made to Unit 24 and 34. The main functions of Unit 44 are: •

Chill the sweet gas from Unit 34 to condense HC liquids and water upstream of the molecular sieve dryers

•

Dehydrate the feed gas to the NGL Recovery Unit

•

Recover C2+ NGL

•

Fractionate the raw NGL into a C2-C4 product and a C5+ product

CHAPTER 1



2.0


FEED CHARACTERISTICS The feed to OGD-I Train 3 is non-associated gas from the Thammama-F reservoir. The well fluid is sent to Unit 24 where the gas is separated from the condensate, and the condensate is stabilized to the specification. The sour gas from Unit 24 is then fed to the Gas Sweetening Unit, Unit 34, for acid gas removal. The sweet gas is sent to Unit 44, the Dehydration and N G L Recovery Units. The following cases were originally considered in the design of Train 3: •

Low Condensate Case

•

Maximum Condensate Case

•

Low H2S Case

Unit 44 was originally designed for the Low Condensate Case, and checked for the other cases. For the E R M Project, the design of the new equipment was based on the Low Condensate Case. The original design feed rate was increased by 5% to reflect the results of Step 1 of the Habshan Capacity Enhancement. The new equipment is also suitable for the Max Condensate Case. As for Low Condensate Case, the original Max Condensate design feed rate was increased by 5% to reflect the results of Step 1 of the Habshan Capacity Enhancement. The rates, conditions, and compositions for the sweet gas from Unit 34 are given in the sections below. 2.1

Feed Gas Flow and Conditions Low Condensate Case

34-V-103

Source of Feed Normal Rate (dry basis), MMscfd Temperature, C 0

Max Condensate Case

616 + 5%

627 + 5% 58 max.

Pressure, barg

65.5 min

Water Content

Saturated

Data source: Low Condensate Case data are from the C2 Enhancement Material Balance, PFD 44-0020012. Max Condensate Case data are from the C2 Enhancement Material Balance, PFD 44-0020-013.

CHAPTER 1

Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44


Doc. No.: PP-AOWT-44-00-001

Addendum for the ERM Project - Rev. 1

2.2

GASCO ProjectNo.: 13522102

Feed Gas Composition Outlet of 34-V-103 (Dry Basis) Low Condensate Case

Max Condensate Case

Mole %

Mole %

N2

0.300%

0.319%

Cl

76.766%

75.463

C2

9.313%

9.733

C3

5.089%

5.637

iC4

1.569%

1.771

nC4

2.558%

2.904

iC5

0.714%

0.772

nC5

0.595%

0.640

NC6

0.444%

0.453

NBP[I]_91

0.431%

0.394

NBP[1]_138

0.065%

0.056

NBP[1L182

0.006%

0.005

H2S

20 ppmv

20 ppmv

C02

2.143%

1.850%

M-Mercaptan

11 ppmv

0 ppmv

E-Mercaptan

13 ppmv

0 ppmv

nP-Mercaptan

45 ppmv

18 ppmv

Component

Data Source: Low Condensate Case data are from the C2 Enhancement Material Balance, PFD 440020-012. Max Condensate Case data are from the C2 Enhancement Malerial Balance, PFD 44-0020013.

2.3

Flexibility and Turndown Unit 44 can be operated in either C2 recovery mode or C2 rejection mode. As the objective of the project is to recover additional C2, the design case for the E R M Project was the C2 recovery mode of operation. However, the design of the new equipment allows the unit to be switched back to C2 rejection mode of operation without demerits to existing performance. The plant is also designed with the flexibility to operate at any point between the maximum C2 recovery case and the C2 rejection case. New equipment was designed for turndown to 50% of design rates.

CHAPTER



3.0

PRODUCT SPECIFICATIONS

3.1

Lean Gas


The lean gas specifications are given below. 0

Hydrocarbon dew point

-5 C max. at 39.2 bara

Water dew point

-30 C max. at 39.2 bara

H2S Content

20 ppm vol. max

Net calorific value

900 BTU/SCF min.

o

Required conditions at the export gas grid: Temperature

62°C max.

Pressure

41.5 barg

Data Source: OGD-II "Operating, Maintenance and Safety Manual: Overall Plant Summary and Start-up Considerations", Chapter]: Overall Plant Description. Date: October 1999, Rev.:A, Page 116. 3.2

NGL The N G L product specifications are given below. C2 Recovery Mode

C2 Rejection Mode

C1/C2

4.5 wt% max.

Not Applicable

C02/C2

5.5 wt% max.

Not Applicable

C2 and lighter

Not Applicable

5 mol% max.

Water Content

5 ppm wt max.

5 ppm wt max.

4 mol% max.

4 mol% max.

C5+ Content

3.3

C5+ Condensate The C5+ condensate from the bottom ofthe Debutanizer (44-V-401) is to contain 1 mol% (max.) C4.

CHAPTER 1


4.0


EFFLUENTS The ERM Project does not impact the effluents from Unit 44.

CHAPTER 1







5.0

PRINCIPLES OF OPERATION The E R M Project impacts the following areas of Unit 44: •

Feed Chilling

•

Demethanizer / Recycle Gas Loop

•

Debutanizer

•

Propane Refrigeration System

A high-level overview of the modified operation is provided in this section. Refer to Chapter 2 for additional information.

5.1

Feed Chilling The 2nd Feed Chiller (44-E-318) is added upstream of the 1 st Stage Feed K O Drum (44-V301). Propane refrigerant from the new Refrigeration Package is fed to the shell side of the kettle-type exchanger. This new exchanger lowers the temperature profile of the majority of the downstream unit and allows more ethane to be recovered from the feed gas.

5.2

Demethanizer / Recycle Gas Loop The Demethanizer (44-V-306) in Unit 44 is fabricated out of Low Temperature Carbon Steel (LTCS). This currently limits ethane recovery as operating temperatures at the top of the tower must be maintained a safe margin from the design temperature (-45°C). In order to operate at the colder temperatures that result from the addition of the 2 Feed Chiller, a new 8-tray stainless steel Cold Demethanizer (44-V-308) is added. This column acts as an extension ofthe existing Demethanizer. The liquid from the existing Recovery Tower Bottom Flash Drum (44-V-307) and 2nd Stage Liquid from 44-E-314 are combined and fed to the top of 44-V-308. The overhead vapor from 44-V-306 is fed to the bottom of 44-V-308 and the new Cold Demethanizer Bottoms Pumps (44-P-302A/B) pump the liquid from the bottom of 44-V-308 back to the top of 44-V-306 via the existing Demethanizer Reflux Condenser (44-E-305). nd

In the recycle gas loop, new bypasses are added around 44-E-315 and 44-E-303. The total bypass of the 1st Stage Liquid/Recycle Gas Exchanger (44-E-315) helps maintain lower temperatures in 44-V-306. The Recovery Tower Reboiler (44-E-303) is not required when operating in C2 recovery mode.

5.3

Debutanizer Raw N G L from the Demethanizer is sent to the Debutanizer (44-V-401) forfractionationinto C2-C4 N G L and a C5+ product. Currently, the Debutanizer overhead vapor is fully condensed in an air-cooled condenser. The Debutanizer currently operates very close to the design pressure of the equipment. Because the pressure of the Debutanizer cannot be increased any further, the temperature required to condense the Debutanizer overhead stream

CHAPTER 1




will decrease as the ethane content of the NGL increases. For the E R M Project, a new Debutanizer Trim Condenser (44-E-406) is added downstream of the existing aircooler to completely condense the C2 rich NGL product. Propane refrigerant from the new Refrigeration Package is fed to the shell side ofthe kettle-type exchanger. New cold insulation is applied to the existing Debutanizer Overhead Accumulator (44-V-402) and to the existing line from 44-V-402 to the Debutanizer Overhead Pumps (44-P-401 A/B). A new N G L Subcooler (44-E-407), which is a kettle-type exchanger with propane refrigerant on the shell side, cools the NGL product from Unit 44 down to 20 C. Subcooling the NGL ensures that the vapor pressure of the combined NGL stream is less than the maximum operating pressure of the existing NGL Storage Spheres (45-V-501 A/B/C). o

5.4

New Propane Refrigeration System The new Refrigeration Package (44-ME-201) includes a two-suction Propane Compressor (44-C-202) with an electric motor driver, a high pressure knock-out drum (44-V-206), a low pressure knock-drum (44-V-207), and a propane receiver (44-V-205). As discussed above, the new system provides the following two levels of refrigerant to the process: 0

o

Low level at about -26 C and 1.0 barg to 44-E-318 for chilling the feed gas

»

High level at about 16 C and 6.4 barg to 44-E-406/7 for condensing and subcooling the N G L product

0

Subcooling the refrigerant is required due to the remote location ofthe new chillers. An existing air cooler (currently tagged 45-E-701) purchased for a previous project is used as the Propane Condenser for the new system (44-E-203).

CHAPTER 1


6.0



PROCESS FLOW DIAGRAMS AND MATERIAL BALANCES The E R M Process Flow Diagrams for Unit 44 are included in this section. Drawing Number

Description

44-00-20-001

Inlet Gas Dehydration

44-00-20-003

N G L Recovery Plant Sheet 1

44-00-20-004

N G L Recovery Plant Sheet 2

44-00-20-004A

NGL Recovery Plant Sheet 3

44-00-20-005

Fractionation

44-00-20-006

N G L Refrigeration Area

44-00-20-006A

E R M Refrigeration Package

The following four Material Balance cases are also provided:

CHAPTER 1

Document Number

Description

44-00-20-010

Low Condensate Case - C2 Rejection Mode

44-00-20-011

Max Condensate Case - C2 Rejection Mode

44-00-20-012

Low Condensate Case - C2 Recovery Mode

44-00-20-013

Max Condensate Case - C2 Recovery Mode

44-V-101

44-r-ios

41-F-I01 A/8

,

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I. IHC ClUlPtCNI C»P*C!T1ES U C l CUED CII IKIS P^D REFER IO THE LO* CCNDidSilE WSE. « flECOVtF.r UOOE. :.FOR V-iJEfiJu DRAWINGS: 44-00-20012 i*-00-;001D 4iHX)-2001J *»-00-!00;I

FLUOR. EJHAKE RECOVERV

WL»»K5. fl£FEP IC IHE FDllOUWC : LOK COVDEnSUE C*SE. C2 RECO'/ERI : LOW COH0ENi*TE C*S-:. C2 REJEC"!OH : M»X CON0EHS*TE C»Si. C: RECOVEST : M l CONKHSm C»SE. RZJEC'ION

MAX IMIZAT; OM

PROCESS FLOW OI^GFfiM I M E T GftS DEHYGRflTiON THAMMAMA ' F * S23!

|4,4l

1001

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F[£t) CHILLER 10.78 Gcol/Hr

FECfCLE O'S COVPRESSOR (STElU ItSSlNE DRIVER)

^-£-306 FEED CHiLLEfi B.99 Gcul/Hr

«-E-3:6 1ST S U K L fOyiC/FEtO EJC--»HG£R S . N Ocol/Hr

ISl SEISE lIOJID/HiCYCL: MS FKChlMCEFI 0.03 Gcol/Hr

^4-£-31•^

PtCTCLE IRIH COOLER WD SHOE LlOUIO/fEtD EJCHJHCEB 0.3S CMt/Mr Z-Ot Ceat/hr

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DEUElHWIIIER 2.
44-£-3C5

44-P-301A/B

OEtfir^lKlUR REFIL1 CCKDEHSES COO CiCl/Hr

CEiCrHfJIUR REBOIlEfl OR»»-CFr PLWS

NOTES: 1. tLl Ifl*EB*TyRES" PRESSURES. FLO» iUANT11IES IND CWOSIIIIWS »RE FDR PRCCESS DrslCN PURPOSES OKLY. NO CU*BJ.HI££ IS EXPRESSED OR ItfUEC-. 2. U L FLOn R*IES WO PROCESS -IWSIT IONS SHQUM »F!E 11 OPERA TINO COHDHIOHS. Wf.ESS OTWERUSE MOIED. 3. THE EOUIPVEfJT C*P»CITiES IN:lC*TEO DM '415 PFO P£/Ea 10 7H£ i o * C O N D C « * ; £ CSSI. cs R c z o n t r UOOE. (.FOR wTEfi;*L BlLiNCES. REfE" TO THE FCLLOtlli: OH**INGS: t*~2Q-!00-2 t LC* CONDENS*C»S£. Z2 SECOVEST <*~jO-200;0 : LCW COiDEtftilE CASE. C2 REJECTION *4-00-ZDD): : M»X COSDENSATE CASE. CZ BECO.'ERT * J - ? 0 - Z 0 0 n i MAI CONOEMSATE CASE- Cl REJSCTICM

FLUOR. ETHANE RECOVERY MAXi M IZAT IGN PR3JECT PROCESS FLOW DIAGRAM KGL PSCGVESY PLAMT SHT 2 THAKMAMA T ' D=flW;riG MJH9ER

JJE* LINES.

\4A}

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WPBOVEO FOR CON'SIFOiO*

ESIE33ISI3EIBI

AP=ROV£D FOR OESIGN ISSUED FJI APPFOWL ISStEO

RE •'IE v

HQTES: I. ALL lEuPERATUBES. PRESSURES. FLO* C U A N I T T V E S " i.vo

c & p o s n m w JB£

onn.

FOB PROCESS ; E S I C H FUKPOSES

na cuARAWTiE is EXPRESSED OT I W L I E D .

!. IKE EOUIPMENI CAPACITIES l ^ K S I t ; OH IHIS PFJ REFER TO THE 10* C0W)EI1S*!£ CASE. C i RECOVER" UOOE. I. FOfi MATERIAL BALANCES. REFER TO lÊ FOLLOXINC ORAMINOS: •M-03-20017 : LO* COttCENSAlE CASE. C2 RECOVERT <1-0>200IO = L0» COIIC-EHSAIE CASE- C2 FEJECTICH J < - 0 0 - 2 0 0 1 3 : VAX CONDEHSAIE CASE. CZ RECQvERi « i - 0 3 - ; 0 0 l l : VAX COWCEMSAIE CASE. C2 ÊJECrjCM NEK LINES. EOUIPMENT. ANO INS7RUIENIS

ETHANE

!i4.

FLUOR,

R E C O V E R Y MAX I M l Z A T ] Of I P R O J E C T

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44-£-406

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HQTES: 1. ALL • E I P E B A I U R E S . PRESSURES. FLO* OUA-UIIIES AHD COlPOSiriONS ARE FOR PROCESS OESIvN PURPOSES DMLY. NO CUARAMIEE IS EXPRESSED OR IMPLIED2. ALL FLO RATES WO PROCESS CONDIIIONS SHOVN m AT OPERAIINC C0N0II10I1S. O-T.ESS CTKERÎSE NOTEO. 3. TKE EOUIPMENT CAPAClliES M C I C A T E D OH IHIS PFO REFER TO IHE LC» CCKDENStlc CASE. C2 RECOVERI lOCE. 4. FOR MAT-RIAL DRAVINGS: 44-O0-2CO13 44-00-20010 44-O0-2C013 4'-O0-ZO0H

BALANCES. REFER 10 THE FOL LOW! IiG : : : :

LCW COMDENSATE LOT COWDENSAIE UAX COMOEHSAlE MAX CONDENSATE

NE* LINES. EOUIPNENT. AKD INSIRJICHIS

CASL. CASE. CASE. CASE.

C2 RECOVERV C2 PEJECIION Ct RECDvERY C2 REJECT IOM

FLUOR. THOIJE

RECOVERY MAXIMIZATION PRDCESS FLCW DIAGRAM FRACTiONAT!DN TH^^MftHfl ' F ' ORfiwiNG NUMBER

l±4j

10,0]

PPOJECT

>

44-E-306 FEED CKILLER tcol/Hr

44-V-2CJ nm siiCE sxricN osuu ID » J.T™

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2.on ID X M n

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44-E-310 HEI FEED CHlUEt 10.71 Gcol/Hr

44-E-201 BEFRtSERWI COwaENSER 21.6! Ctol/Hr

44-E-202 REFR1CEPAM I 5U3COOLifl l . l l Gcoi/Xr

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NOTES: 1. ALL TEMPERATURES. PRESSURCS. ELC" DUAiniTIES XUO COUPOSHIONS ARE FOR PROCESS DESIGN PURPOSES ONLT- NO GUARANTEE IS EXPR-ISSEO OR IfP'.IED. 2. ALL ^LOw RATES AND PROCESS CCNOITIONS SHOWi APE Af (FEB* f I WC COWfTICWS. yvLESS 0IrtER»I5E NE-TEO. J.IHE ZOUIPICNI CAPACITIES IN0ICAIE3 ON IHIS PFD REFEi TO IHE LO* CEWOENSAIE CASE• CZ RECOVERT IODE. 4. FOR IATERIAL BALANCES. REF;R 10 TrE FOLLO*iNG DRAVINGS: 4^-03-?00ir i LCV CONCENSAIE CASE. C2 firCOVES) 4^-02-20010 : LOV CDIICEHSATE CASE. Z i REJLCIION 4'-00-200l3 : MAX CDNCtNEATE CASE- CZ RECOVERi 4 ' - 0 a - 2 0 0 n : UAX CONCENSATE CASE. C2 SEJECTION

ISSLtO FCR R

FLUOR. ETHANE

R E C O V E R t MAX IMf ZA T I O N PRDCESS FLOW DIAGRAM NGL REFRIGERATION AREA THSKMAKP "F" DflAWiHC NUMEIER

PROJECT

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Sk^ j ETHAIJE

FLU0R

-

RECOVERY viftxIMIZATION P R O J E C T PROCESS FLOW DIAGRAM ERM REFRIGERATION PACKAGE THAKMPHA ' - ' DRflWItj; HUX&ER

I-4,4|

1001

| REV.


Ethane Recovery Maximization (ERM) Project Material Balance Low Condensate Case - C2 Rejection Mode Rev.2

GASCO ProjectNo.: 13522102 Doc. No.: 44-00-20010

ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Material Balance Low Condensate Case C2 Rejection Mode Revision 2

Rev.

Date

Description

By

Chk.

Disc.

>l9

Approved Proj. GASCO

GS-L-FML046

13-Feb-04

Approved for Construction

4-Sep-03

Approved for Design

OPM

DTS

ED

7-Aug-03

Issued for Approval

OPM

DTS

ED

FLUOR Conlracl AOWT Rev.2

GASCO Ethane Reoovery Maxtmization

LOW CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composilion (kgmole/h) Nilrooen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weighl Vapor Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

1

10

11

20

22

23

24

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

39.5 10013.0 1165.5 568.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

39.5 10013.0 1165.5 588.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

56.3 14281.0 1662.3 838.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5 0.0 0.2 0.2 0.3 0.0

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

96.6 24733.6 3000.5 1639.8 50S.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

96.6 24733.6 3000.5 1639.B 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

96.6 24733.6 3000.5 1639.6 505.5 8242. 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 21.9

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 0.0

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.0 0.0 0.0 0.0 0.0 87.7

0.8 439.5 172.7 212.6 110.3 216.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

32330.0 732576 5B.0 66.5 1.00 -686.7 22.66

32330.0 732576 43.9 65.8 0.98 -694.9 22.66

32330.0 732576 27.0 65.4 0.95 -705.4 22.66

30659.8 653637 27.0 65.3 1.00 -647.7 21.32

30637.9 653241 27.8 62.8 1.00 -645.5 21.32

1582.5 77359 27.0 65.3 0.00 -51.7 48.88

1582.5 77359 18.1 31.4 0.23 -51.7 48.88

87.7 1581 27.0 65.3 0.00 -6.0 18.02

1582.5 77359 51.9 30.7 0.36 -49.7 48.88

12627.7 269239 27.6 62.5 1.00 -266.1 21.32

12627.7 269239 -7.0 60.8 0.91 -274.2 21.32

18010.1 384000 27.6 62.5 1.00 •379.5 21.32

14023.5 299000 27.5 62.4 1.00 -295.5 21.32

64.4 0.62 0.014 0.034 22.66 732575 647.9

66.6 0.64 0.014 0033 22.14 703470 636.6

69.3 0.66 0.014 0.032 21.32 653737 614.4

69.2 0.66 0.014 0.032 21.32 653637 614.4

65.6 0.65 0.013 0.032 21.32 653241 614.0

69.2 0.66 0.014 0.032 21.32

32.4 0.54 0.012 0.027 22.08 8149 7.4

69.2 0.66 0.014 0.032 21.32

35.0 0.54 0.013 0.028 27.02 15318 11.4

65.3 0.65 0.013 0.032 21.32 269239 253.1

71.9 0.74 0.012 0.030 19.72 227245 230.9

65.3 0.65 0.013 0.032 21.32 384000 360.9

65.2 0.65 0.013 0.032 21.32 299000 281.0

529.8 0.60 0.129 0.073 7.99 55.33 28130 53.1

513.4 0.60 0.121 0.074 7.70 48.87 77259 150.5

513.6 0.60 0.121 0.074 7.71 48.88

513.6 0.60 0.121 0.074 7.71 48.88 77359 150.6

577.8 0.57 0.168 0.081 10.59 57.04 69207 119.8

513.6 0.60 0.121 0.074 7.71 48.88

551.9 0.60 0.137 0.073 8.59 61.09 62041 112.4

976

1580

—

Simulation Basis: Train 3 - Selecled Option + 5'X. - C3 Mode Rev. 5A

o.o

1581

Paget of 10

480.6 0.62 0.103 0.079 7.53 38.02 41994 87.4

FLUOR Contract AOWT Rev.2

GASCO Elhane Recovery Maximization


Stream Number Compoaition (kgmole/h) Nilrogen Methane Ethane Propane I-Butane n-8utane i-Pentane n-Pentane n-Hexane NBP91 NBP138 'NBP182 H2S C02

25

26

28

29

30

31

32

33

34

36

37

38

43

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9

56.3 14281.0 1662.3 83B.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7

93.9 23052.2 2308.3 869.6 169.6 216.5 27.3 18.1 3.7 1.3 0.0 0.0 0.5 596.8

54.7 13434.6 1345.2 506.8 99.0 126.2 15.9 10.5 2.2 0.7 0.0 0.0 0.3 349.0

54.7 13434.6 1345.2 506.8 99.0 126.2 15.9 10.5 2.2 0.7 0.0 0.0 0.3 349.0

14.6 3622.9 362.8 136.7 26.7 34.0 4.3 2.8 0.6 0.2 0.0 0.0 0.1 94.1

14.8 3622.9 362.8 136.7 26.7 34.0 4.3 2.8 0.6 0.2 0.0 0.0 0.1 94.1

93.9 23052.4 2308.4 869.7 169.8 216.5 27.3 18.1 3.7 1.3 0.0 0.0 0.5 598.8

92.2 22086.3 1945.6 564.8 79.9 85.5 6.2 3.5 0.3 0.1 0.0 0.0 0.4 546.0

92.2 22086.3 1945.6 564.8 79.9 85.5 6.2 3.5 0.3 0.1 0.0 0.0 0.4 546.0

CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Row (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat How (Qcal/h)

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

o.o

0.1 0.1 0.2 0.0

0.0 0.0 0.1 0.0

0.0 0.0 0.1 0.0

0.2 0.2 0.3 0.0

0.3 0.3 0.5 0.0

0.1 0.1 0.0 0.0

0.1 0.0 0.0 0.0

0.1 0.0 0.0 0.0

0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0

0.1 0.1 0.0 0.0

0.1 0.0 0.0 0.0

0.1 0.0 0.0 0.0

14023.5 299000 -6.7 61.3 0.91 • -304.5

3986.6 85000 27.5 62.4 1.00 -84.0

3986.6 85000 -21.4 60.9 0.85 -87.8

18010.1 384000 -15.2 60.8 0.88 -394.2

30637.9 653241 -11.9 60.7 0.89 -668.4

27360.2 532785 -11.9 60.7 1.00 -573.6

15945.2 310501 -11.9 60.7 1.00 -334.3

15945.2 310501 -35.9 60.2 0.91 -342.2

4300.0 83734 -11.9 60.7 1.00 -90.2

4300.0 83734 -32.4 60.2 0.93 -91.9

27360.6 532797 -32.3 60.2 0.93 -584.8

25410.9 474718 -32.2 60.2 1.00 -532.7

25410.9 474718 -50.7 39.6 0.95 -535.5

21.32

21.32

21.32

21.32

21.32

19.47

19.47

19.47

19.47

19.47

19.47

18.68

18.68

72.5 0.74 0.012 0.030 19.74 252761 256.6

65.2 0.65 0.013 0.032 21.32 85000 79.9

77.1 0.82 0.012 0.029 19.00 64216 67.7

74.6 0.78 0.012 0.029 19.31 305472 317.0

73.3 0.76 0.012 0.029 19.47 532749 548.3

73.3 0.76 0.012 0.029 19.47 532785 548.3

73.2 0.76 0.012 0.029 19.47 310458 319.5

85.9 0.98 0.012 0.029 18.53 267767 289.7

73.2 0.76 0.012 0.029 19.47 83722 86.2

83.4 0.93 0.012 0.029 18.67 74485 79.9

83.2 0.93 0.012 0.029 18.68 474504 509.1

83.4 0.93 0.012 0.029 18.68 474718 509.2

52.0 0.75 0.010 0.024 18.04 433423 481.6

466.1 0.63 0.096 0.080 7.33 34.21 20784 44.6

473.1 0.63 0.100 0.080 7.45 35.87 78528 166.0

476.6 0.62 0.101 0.079 7.50 36.78 120493 252.8

476.4 0.62 0.101 0.079 7.49 36.75 —

476.5 0.62 0.101 0.079 7.49 36.75 43 0.1

421.3 0.69 0.074 0.079 6.26 28.66 42734 101.4

476.5 0.62 0.101 0.079 7.49 36.75 12 0.0

430.5 0.68 0.07B 0.080 6.49 29.75 9249 21.5

431.1 0.68 0.079 0.080 6.50 29.80 58293 135.2

430.7 0.68 0.079 0.080 6.49 29.79 -

474.9 0.64 0.096 0.087 8.27 29.94 41296 87.0

-

-

-

—

~

Molecular W e i g h t

Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermai Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weighl Mass Flow (kg/h) Actual Volume Flow (m3/h) Waler Phase Mass Flow (kg/h)

479.5 0.62 0.103 0.079 7.49 37.98 46239 96.4

Slmulalion Basis: Train 3 • Selected Option . 514 • C3 Mono Rev. 5A

--

— — — — — -

Page 2 of 10

-


QASCO Elhane Recoveiy Maximizalion


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 N8P138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperalure C O Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weighl Vapor Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Row (m3/h) Water Phase Mass Flow (kg/h)

se

57

58

70

72

73

75

76

77

i.i

0.5 S79.6 332.2 298.4 89.3 130.3 21.1 14.5 3.4 1.2 0.0 0.0 0.1 43.2 0.0 0.1 0.1 0.0 0.0

25 913.9 87.1 24.0 3.6 4.1 0.4 0.2 0.0 0.0 0.0 0.0 0.0 24.8 0.0 0.0 0.0 0.0 0.0

95.8 24294.4 2747.4 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

95.8 24294.3 2747.3 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

95.8 24294.3 2747.3 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

95.8 24294.3 2747.3 139.6 2.6 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.6 667.7 0.0 0.0 0.0 0.0 0.0

89.7 22735.7 2671.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0

435.7 7943 -43.9 39.7 l.OO -9.1 18.23

1514.0 50136 -43.9 39.7 0.00 -43.0 33.11

1060.7 19998 -29.7 39.7 1.00 •22.2 18.85

27949.2 510831 -56.6 39.5 1.00 -588.4 18.28

27949.0 510826 -46.0 39.1 1.00 -584.1 18.28

0.0 0 22.0 38.6 1.00 0.0 18.28

27949.0 510826 -11.9 38.8 1.00 •572.9 18.28

27949.0 510826 22.0 38.6 1.00 -562.9 18.28

26156.0 478055 22.0 38.4 1.00 -526.7 18.28

83.4 0.93 0.012 0.029 18.68

49.6 0.71 O.OtO 0.024 18.23 79« 8.7

49.6 0.71 0.010 0.024 18.23

46.1 0.65 0.011 0.025 18.82 19926 21.2

57.2 0.83 0.010 0.024 18.28 510829 560.1

49.8 0.71 0.010 0.024 18.28 510826 560.1

31.4 0.57 0.012 0.030 18.28

37.9 0.59 0.011 0.027 18.28 510826 560.1

31.4 0.57 0.012 0.030 18.28 510826 560.1

31.3 0.57 0.012 0.030 18.28 478055 524.2

430.7 0.68 0.079 0.080 6.49 29.79 58079 134.9

498.8 0.62 0.112 0.088 9.04 33.11

498.8 0.62 0.112 0.088 9.04 33.11 50136 100.5

521.1 0.69 0.127 0.087 9 64 37.88 72 0.1

415.8 0.75 0.065 0.085 6.40 24.79 2 0.0

50

52

53

64

2.0 1241.9 519.6 557.5 225.4 389.2 107.6 86.6 46.0 30.6 1.5 0.0 0.1 68.9 0.0 0.2 0.2 0.5 0.0

1.4 527.3 56.5 17.6 2.9 34 0.4 0.2 0.0 0.0 0.0 00 0.0 15.2 0.0 0.0 0.0 0.0 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 86.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

1.6 966.1 362.8 304.9 90.0 131.0 21.1 14.6 3.4 1.2 0.0 0.0 0.1 52.9 0.0 0.1 0.1 0.0 0.0

3277.6 120456 -11.9 60.7 0.00 -94.7 36.75

624.9 12055 -20.5 39.7 1.00 •13.1 19.29

2652.7 108401 -20.5 39.7 0.00 -81.6 40.86

1949.8 58079 -32.2 60.2 0.00 -52.1 29.79

73.3 0.76 0.012 0.029 19.47

44.7 0.62 0.011 0.026 19.29 12055 12.5

44.7 0.62 0.011 0.026 19.29

476.4 0.62 0.101 0.079 7.49 36.75 120456 252.8

531.5 0.59 0.134 0.086 9.78 40.86

531.5 0.59 0.134 0.086 9.78 40.86 108401 204.0

Slmulalion Basis: Train 3 • Salocted Option . 5% • C3 Mode Bev. 5A

386.5 30.6 6.4 0.7 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 9.6 0.0 0.0 0.0 0.0 0.0

Page 3 o l i o

o.o o.o o.o o.o o.o o.o

0.0

0.0 0.0 0.0

FLUOR Contract AOWT Rev. 2

GASCO Ethane Recovery Maximization


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaplan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature C O Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume Row (m3*) Water Phase Masa Flow (kg/h)

78

79

80

81

89

90

91

92

93

94

95

96

103

89.7 22735.7 2571.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0 0.0 0.0 0.0 0.0

89.7 22735.7 2571.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0 0.0 0.0 0.0 0.0

89.7 22735.7 2571.1 130.6 2.4 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.5 624.8 0.0 0.0 0.0 0.0 0.0

6.1 1558.5 176.2 9.0 0.2 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 42.8 0.0 0.0 0.0 0.0 0.0

1.1 1511.9 1380.5 714.6 939 97.8 6.8 3.9 0.4 0.1 0.0 0.0 0.3 144.6 0.0 0.1 0.0 0.0 0.0

1.1 1511.9 1380.5 714.6 93.9 97.8 6.8 3.9 0.4 0.1 0.0 0.0 0.3 144.6 0.0 0.1 0.0 0.0 0.0

0.1 205.5 1625.3 1010.4 105.3 106.3 7.1 4.0 0.4 0.1 0.0 0.0 0.3 41.6 0.0 0.1 0.0 0.0 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 66.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 86.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

0.6 714.6 463.1 539.9 222.5 385.8 107.2 86.3 46.0 30.6 1.5 0.0 0.1 53.7 0.0 0.2 0.2 0.5 0.0

0.5 579.6 332.2 298.4 89.3 130.3 21.1 14.5 3.4 1.2 0.0 0.0 0.1 43.2 0.0 0.1 0.1 0.0 0.0

0.5 579.6 332.2 298.4 89.3 130.3 21.1 14.5 3.4 12 0.0 0.0 0.1 43.2 0.0 0.1 0.1 0.0 0.0

0.0 146.1 933.3 1896.0 328.5 410.3 49.5 32.8 6.8 24 0.0 0.0 0.2 25.3 0.0 0.3 0.2 0.1 0.0

26156.0 478055 52.2 38.0 1.00 -518.5 18.28

26156.0 478055 64.4 43.4 1.00 -515.8 18.28

26156.0 478055 53.8 42.8 1.00 -518.6 18.28

1793.0 32771 22.0 38.4 1.00 -36.1 18.28

3956.0 115642 -42.5 39.6 0.00 -106.9 29.23

3956.0 115642 -53.9 25.2 0.17 -106.9 29.23

3106.5 111715 0.2 29.6 0.00 -83.9 35.96

2652.7 108401 -27.2 25.5 0.13 -81.6 40.86

2652.7 108401 16.0 24.8 0.34 -77.8 40.86

2652.7 108401 32.0 24.1 0.45 -76.0 40.86

1514.0 50136 -54.0 24.8 0.17 -43.0 33.11

1514.0 50136 -16.8 24.1 0.42 -41.2 33.11

3831.8 164887 33.2 23.8 0.00 -110.6 43.03

27.2 0.56 0.013 0.033 18.28 478055 524.2

29.9 0.57 0.013 0.035 18.28 478055 524.2

30.6 0.57 0.013 0.034 18.28 478055 524.2

31.3 0.57 0.012 0.030 18.28 32771 35.9

-

31.8 0.60 0.009 0.021 18.88 12847 13.6

-

28.1 0.55 0.010 0.023 19.57 6960 7.1

29.9 0.52 0.011 0.024 25.22 22986 18.3

31.1 0.52 0.011 0.024 28.25 33874 24.0

29.5 0.59 0.009 0.021 18.15 4667 5.2

28.6 0.53 0.010 0.023 21.83 13995 12.9

456.5 0.67 0.083 0.088 7.55 29 23 115642 253.3

506.5 0.62 0.113 0.097 9.96 31.38 102795 202.9

466.1 0.66 0.087 0.081 5.99 35.96 111715 239.7

565.9 0.57 0.168 0.091 11.77 44.16 101441 179.2

537.0 0.60 0.132 0.079 8.88 49.06 85415 159.1

527.0 0.61 0.120 0.074 7.93 51.27 74527 141.4

546.3 0.58 0.153 0.096 11.65 36.17 45469 83.2

534.7 0.59 0.135 0.089 9.99 41.40 36141 67.6

-

-—

--

™ --

—

—

—

—

Simulalioo Basis: Tram 3 - Salocted Option • 5% - C3 Mode Rev. 5A

—

Page 4 of 10

—

—

468.7 0.67 0.085 0.070 5.24 43.03 164887 3S1.8


OASCO Elhane Recovery Maximization


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP9I NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Meroaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Aclual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

104

109

110

111

112

113

115

116

117

118

119

120

121

0.0 146.1 933.3 1896.0 328.5 410.3 49.5 32.8 6.8 2.4 O.O 0.0 0.2 25.3 0.0 0.3 0.2 0.1 0.0

0.0 0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

1.1 1499.3 2339.6 561.0 24.4 17.7 0.5 0.2 0.0 0.0 0.0 0.0 0.5 138.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.0 2095.2 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

2.2 2606.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

3831.8 164887 44.9 23.8 0.17 -107.8 43.03

2689.3 142428 88.9 23.9 O.OO -83.1 52.96

4582.9 127791 2.5 23.7 1.00 -105.4 27.88

5433.5 131752 -19.3 23.3 1.00 -126.8 24.25

5433.7 131757 -11.0 22.9 1.00 -126.2 24.25

5433.7 131757 22.0 22.6 1.00 -123.9 24.25

5433.7 131757 86.9 52.5 1.00 -120.6 24.25

5433.6 131755 86.9 52.5 1.00 -120.6 24.25

0.0 1 86.9 52.5 1.00 0.0 24.25

5433.6 131755 49.8 51.9 1.00 -123.4 24.25

0.0 1 86.9 52.5 • 1.00 0.0 24.25

0.0 1 55.0 51.9 1.00 0.0 24.25

5433.7 131757 49.8 51.9 1.00 -123.4 24.25

36.2 0.55 0.010 0.021 27.88 127790 91.8

32.6 0.54 0.010 0.021 24.21 131139 108.5

30.2 0.52 0.010 0.021 24.25 131757 108.9

24.8 0.50 0.011 0.024 24.25 131757 108.9

47.6 0.57 0.014 0.034 24.25 131757 108.9

47.6 0.57 0.014 0.034 24.25 131755 108.9

47.6 0.57 0.014 0.034 24.25 1 0.0

56.3 0.59 0.013 0.030 24.25 131755 108.9

47.6 0.57 0.014 0.034 24.25 1 0.0

54.7 0.58 0.013 0.030 24.25 1 0.0

56.3 0.59 0.013 0.030 24.25 131757 108.9

468.2 0.67 0.088 0.080 6.04 36.63 1 0.0

484.5 0.64 0.098 0.089 7.62 34.35 613 1.3

43.1 0.58 0.011 0.022 36.38 23340 12.9 458.6 0.69 0.082 0.067 4.67 44.37 141547 308.6

SiTHjlation Basis: Train 3 • Selected Option • 5% - C3 Mode Rev. SA

440.9 0.75 0.076 0.055 2.99 52.96 142428 323.1

Page 5 of 10

o.o o.o o.o o.o o.o o.o

FLUOR Contraci AOWT Rev.2

QASCO Elhane Recovery Maximizalion


Stream Number Composilion (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP13B NBP182 H2S C02 CS2 M-Mercaplan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Row (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std G a s Flow ( M M S C F D )

124

125

126

127

128

129

130

131

132

141

142

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0,0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.8 1032.9 771.2 97.7 4.8 3.4 0.1 0.0 0.0 0.0 0.0 0.0 0.2 88 9 0.0 0.0 0.0 0.0 0.0

0.8 1032.9 771 2 97.7 4.8 3.4 0.1 0.0 0.0 0.0 0.0 0.0 0.2 88.9 0.0 0.0 0.0 0.0 0.0

0.0 0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

0.0 0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

o.o

265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

2.2 2806.1 2095.3 265.3 13.0 9.3 0.2 0.1 0.0 0.0 0.0 0.0 0.4 241.5 0.0 0.0 0.0 0.0 0.0

0.0 80.7 1287.6 392.6 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.0 0.0 0.0 0.3 0.3 0.5 0.0

0.0 0.0 121.5 1938.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.4 0.4 0.0 0.0

0.0 0.0 121.5 1938.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.4 0.4 0.0 0.0

5433.7 131757 27.5 51.5 1.00 -125.1 24.25

5433.7 131757 •6.0 51.2 0.86 -129.3 24.25

5433.7 131757 -21.9 51.0 0.51 •133.3 24.25

5433.7 131757 -30.6 50.7 0.32 -135.3 24.25

5433.7 131757 -55.7 50.5 O.OO -139.5 24.25

5433.7 131757 -56.8 39.5 0.02 -139.5 24.25

2000.0 48496 -21.9 51.0 0.51 -49.1 24.25

2000.0 48496 -47.6 50.7 0.00 -51.1 24.25

26B9.3 142428 75.8 18.0 0.16 -83.1 52.96

2689.3 142428 75.0 16.8 0.30 -82.0 52.96

2689.3 142428 74.2 16.5 0.31 -82.0 52.96

3649.2 182792 74.8 16.0 1.00 -98.5 50.09

3649.2 182792 59.8 22.5 0.00 -112.1 50.09

64.4 0.64 0.013 0.028 24.25 131757 108.9

82.9 0.86 0.012 0.027 23.50 110234 94.0

80.4 0.69 0.012 0.027 21.57 59344 55.1

79.3 092 0.012 0.027 20.57 35608 34.7

58.1 0.84 0.010 0.024 18.37 1805 2.0

80.4 0.89 0.012 0.027 21.57 21843 20.3

39.7 0.59 0.011 0.021 48.12 21163

37.0 0.58 0.010 0.021 48.66 39284 16.2

362 0.57 0.010 0.021 48.66 40228 16.6

36.4 0.56 0.010 0.021 50.09 182792 73.1

373.3 0.84 0.053 0.077 4.07 28.97 21523 57.7

376.7 0.84 0.053 0.081 4.78 26.99 72412 192.2

377.4 0.83 0.053 0.082 5.07 25.97 96148 254.8

409.8 0.77

376.7 0.84 0.053 0.081 4.78 26.99 26653 70.6

473.4 0.69 0.090 0.061 4.37 53.91 121265 256.2

480.8 0.68 0.094

482.6 0.68 0.094 0.062 4.78 54.87 102200 211.8

122 2.2 2806.1 2095.3

Hydrocarbon Uquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Aclual Volume Flow (m3/h) Waler Phase Mass Flow (kg/h)

Simulation Baale: Train 3 - Selectea Option + 5% • C3 Mode Rov. 5A

123

404.8 0.76 0.061 0.085 6.06 24.25 131757 . 325.5

Page 6ot10

0.062 0.085 6.23 24.36 129952 317.1

383.3 0.81 0.054 0.082 5.45 24.25 48496 126.5

0.062 4.69 54.81 103144 214.5

478.5 0.68 0.092 0.065 4.93 50.09 182792 382.0

FLUOft Contract AOWT Rev.2



Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kgm) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h) Water Phase Mass Row (kg/h)

ISO

151

152

153

501

502

503

504

505

507

600

601

602

14.1 3467.1 347.2 130.8 25.5 32.6 4.1 2.7 0.6 0.2 0.0 0.0 0.1 90.1 0.0 0.0 0.0 0.0 0.0

14.1 3467.1 347.2 130.8 25.5 32.6 4.1 2.7 0.6 0.2 0.0 0.0 0.1 90.1 0.0 0.0 0.0 0.0 0.0

1.1 1511.9 1380.5 714.6 93.9 97.8 6.8 3.9 0.4 0.1 0.0 0.0 0.3 144.6 0.0 0.1 0.0 0.0 0.0

1.0 882.5 190.4 22.4 1.0 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 43.7 0.0 0.0 0.0 0.0 0.0

0.2 629.4 1190.1 692.2 92.9 97.1 6.6 3.9 0.4 0.1 0.0 0.0 0.2 100.9 0.0 0.1 0.0 0.0 0.0

0.2 629.4 1190.1 692.2 92.9 97.1 6.8 3.9 0.4 0.1 0.0 0.0 0.2 100.9 0.0 0.1 0.0 0.0 0.0

0.2 629.7 1190.3 692.4 93.0 97.2 6.8 3.9 0.4 0.1 0.0 0.0 0.2 100.9 0.0 0.1 0.0 0.0 0.0

43.9 11119.8 1294.4 6S3.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

1.3 1920.2 1899.6 241.7 12.0 8.6 0.2 0.1 0.0 0.0 0.0 0.0 0.4 197.5 0.0 0.0 0.0 0.0 0.0

4115.0 80131 •11.9 60.7 1.00 -86.3 19.47

4115.0 80131 -30.3 60.2 0.94 -87.8 19.47

3956.0 115642 -43.2 24.6 0.29 -105.4 29.23

1141.8 22923 -43.2 24.6 1.00 -25.4 20.08

2614.2 92719 -43.2 24.6 0.00 -80.0 32.95

2814.2 92719 -44.3 23.3 0.02 -80.0 32.95

2815.2 92752 -44.3 23.3 0.02 -80.0 32.95

14023.5 299000 •13.3 60.9 0.B9 •306.4 21.32

4281.7 108549 •14.0 23.3 1.00 -101.2 25.35

73.2 0.76 0.012 0.029 19.47 80120 82.5

82.1 0.90 0.012 0.029 18.76 72451 77.4

31.1 0.57 0.010 0.021 20.08 22923 22.9

31.1 0.57 0.010 0.021 20.08 22923 22.9

31.1 0.57 0.010 0.021 20.08

29.4 0.56 0.009 0.021 20.10 941 0.9

29.4 0.56 0.009 0.021 20.10 951 0.9

74.1 0.77 0.012 0.029 19.40 241227 249.2

33.8 0.54 0.010 0.021 25.35 108549 85.8

476.5 0.62 0.101 0.079 7.49 36.75 11 0.0

435.4 0.67

507.3 0.62

507.3 0.62

0.081 0.080 6.61 30.38 7680 17.6

0.112 0.096 9.68 32.95 92719 182.8

0.112 0.096 9.68 32.95

507.3 0.62 0.112 0.096 9.68 32.95 92719 182.8

511.6 0.62 0115 0.097 9.93 33.16 91778 179.4

511.6 0.62 0.115 0.097 9.93 33.17 91801 179.4

474.6 0.63 0.100 0.079 7.46 36.34 57773 121.7

478.8 0.65 0.092 0.087 7.09 34.61 0 0.0

0.0 0.0 80.7 1287.6 392.5 602.1 41.4 18.9 0.3 0.0 0.0 0.0 0.0 0.0 0.0 0.3 0.3 0.0 0.0

0.0 0.0 0.0 0.0 o.i 2.5 93.5 85.8 49.4 31.9 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.5 0.0

0.0 0.0 0.0 0.0 0.1 2.5 93.5 85.8 49.4 31.9 1.5 0.0

0.0 0.0 0.5 0.0

0.0 0.0 0.0 0.0 0.1 25 93.5 85.8 49.4 31.9 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.5 0.0

2424.1 121424 59.8 22.5 0.00 -74.5 50.09

265.2 21004 160.5 16.3 0.00 -10.1 79.20

265.2 21003 82.0 15.6 0.00 -11.2 79.20

2652 21003 49.0 15.4 0.00 •11.6 79.20

478.5 0.68 0.092 0.065 4.93 50.09 121424 253.8

Simulation Basis: Train 3 • Selected Option . 5% • C3 Mode Rev. 5A

470.1 0.75 0.084 0 049 3.21 79.20 21004 44.7

o.o o.o o.o

584.9 0.61 0.156 0.077 10.21 79.20 21003 35.9

620.4 0.57 0.205 0.086 13.53 79.20 21003 33.9

Page 7 of 10




Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBPie2 H2S C02 CS2

504

605

606

607

0.1 205.5 1625.3 1010.4 105.3 106.3 7.1 4.0 0.4 0.1 0.0 0.0 0.3 41.6 0.0

0.0 0.0 121.5 1936.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0

0.1

0.4

0.0 0.0

o.o

0.4 0.0 0.0

0.0 0.0 121.5 1938.3 590.9 906.3 62.3 28.4 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.4 0.4 0.0 0.0

0.0 0.0 80.7 1287.6 392.5 602.1 41.4 18.9 0.3 0.0 0.0 0.0 0.0 0.0 0.0 0.3 0.3 0.0 0.0

3106.5 111715 0.2 27.0 0.00 -83.9 35.96

3649.2 182792 59.0 15.7 0.00 -112.2 50.09

3649.2 182792 59.0 15.5 0.00 -112.2 50.09

2424.1 121424 35.0 22.0 0.00 -76.4 50.09

466.1 0.66

476.3 0.68 0.093 0.066 5.00

476.3 0.68 0.093 0.066 5.00

50.09 182792 383.7

50.09 182792 383.7

518.9 0.62 0.116 0.075 7.51 50.09 121424 234.0

M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Row (kg/h)

0.087 0.081 5.99 35.96 111715 239.7

Simulation Bajii: Train 3 • Selactao Option - 5% • C3 Mode Rav. 5A

PageSol 10


GASCO Ettiane Recovery Maximization

LOW CONDENSATE CASE - C2 REJECTION MODE • REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Elhane Propane t-Bulane Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h)

200

201

202

203

204

205

206

207

208

210

213

220

701

148.7 7212.5 74.4

148.7 7212.5 74.4

148.7 7212.5 74.4

23.2 2687.5 42.9

23.2 2687.5 42.9

23.3 2685.4 44.6

23.3 2685.4 44.6

8.2 4174.2 196.8

8.2 4174.2 196.8

125.5 4524.9 31.4

125.5 4524.9 31.4

148.8 7210.4 76.0

42.1 2041.6 21.0

7435.5 326842 57.4 21.0 0.00 -205.9 43.96

7435.5 326842 49.2 20.3 0.00 -207.8 43.96

7435.5 326842 20.5 8.8 0.24 -207.8 43.96

2753.6 121704 21.1 8.8 0.00 -79.6 44.20

2753.6 121704 -9.2 3.6 0.20 -79.6 44.20

2753.3 121712 -8.2 3.6 1.00 -70.6 44.21

2753.3 121712 -8.5 3.5 1.00 -70.6 44.21

4379.1 195750 -8.2 3.6 0.00 -131.3 44.70

4379.1 195750 -7.6 3.6 0.50 -122.3 44.70

4681.9 205136 21.1 8.8 1.00 -117.8 43.82

4681.9 205138 20.5 8.5 1.00 -117.8 43.82

7435.2 326850 71.6 21.7 1.00 -182.7 43.96

2104,8 92519 54.5 19.8 0.00 -58.5 43.96

18.6 0.48 0.009 0.016 43.58 77530 35.7

16.7 0.48 O.OOS 0.016 43.82

7.8 0.41 0.007 0.013 43.88 24619 112

7.8 0.41 0.007 0.013 44.21 121712 55.2

7.6 0.40 0.007 0.013 44.21 121712 55.2

7.8 0.41 0.007 0.013 44.21

7.8 0.41 0.007 0.013 44.39 97201 43.9

18.7 0.48 0.009 0.016 43.82 205138 93.8

18.1 0.47 0.008 0.016 43.82 205138 93.8

45.2 0.61 0.011 0.022 43.96 326850 149.0

44.4 0.63 0.010 0.020

499.1 0.64 0.104 0.083 7.38 44.07 249312 499.5

498.9 0.64 0.104 0.083 7.35 44.20 121704 243.9

541.9 0.59 0.141 0.098 11.13 44.28 97085 179.2

542.6 0.59 0.142 0.098 11.10 44.70

542.6 0.59 0.142 0.098 11.10 44.70 195750 360.8

543.2 0.59 0.143 0.097 11.09 45.01 98549 181.4

498.9 0.64 0.104 0.083 7.35 44 20

47.7 0.66 0.010 0.021 43.56

432.3 0.77 0.072 0.065 3.28 43.96 326842 756.1

Slmulalion Baaia: Train 3 • SelectBd Option • 5% - C3 Moda Rev. 5A

450.9 0.72 0.078 0.069 4.12 43.96 326842 724.8

Page 9 otIO

43.56

438.4 0.75 0.074 0.066 3.57 43.96 92519 211.0



LOW CONDENSATE CASE • C2 REJECTION MODE • REFRIGERATION SYSTEMS

Stream Number Composition (kgmoia/h) Ethane Propane i-Butane Total Stream Molar Ftow (kgmole/h) Mass How (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h)

706

708

709

711

712

716

718

722

723

724

727

732

10.8 524.1 5.4

10.8 524.1 5.4

10.8 524.1 5.4

0.0 0.0 0.0

0.0 0.0 0.0

55.2 2679.5 27.6

21.4 1040.2 10.7

9.2 445.5 4.6

9.2 445.5 4.6

9.2 445.5 4.6

20.8 1011.1 10.4

76.1 3690.6 38.0

540.3 23751 18.1 19.2 0.00 -15.6 43.96

540.3 23750 14.5 7.6 0.03 -15.6 43.96

540.3 23750 16.0 7.6 1.00 -13.7 43.96

0.0 1 14.5 7.6 0.03 0.0 43.96

0.0 1 14.3 7.6 0.03 0.0 43.96

2762.4 121424 16.0 7.4 1.00 -69.8 43.96

1072.4 47140 18.1 19.2 0.00 -31.0 43.96

459.3 20190 -21.3 18,7 0.00 -13.7 43.96

459.3 20190 •25.0 2.2 0.03 •13.7 43.96

459.3 20190 -23.5 2.1 1.00 -11.8 43.96

1042.4 45821 -24.4 2.0 1.00 -26.8 43.96

3804.8 167245 76.3 20.3 1.00 -92.8 43.96

16.1 0.46 0.008 0.015

16.2 0.46 O.ooa 0.015 43.96 23750 10.8

16.1 0.46 0.008 0.015 4328 0 0.0

16.0 0.46 0.008 0.015 43.29 0 0.0

15.8 0.46 0.008 0.015 43.96 121424 55.'4

4.8 0.38 0.007 0.012 42.87 507 02

4.8 0.38 0.007 0.011 43.96 20190 9.2

4.6 0.38 0.007 0.011 43.96 45821 20.9

39.8 0.58 0.011 0.022 43.96 167245 76.3

507,4 0.63 0.110 0.086 8.06 43.98 1 0.0

507.7 0.63 0.110 0.086 8.08 43.98 1 0.0

469.6 0.63 0.105 0.086 8.00 44.35

43.28 6S9 0.3 505.8 0.63 0.107 O.OBS 7.62 43.96 23751 47.0

Simulation Basis: Train 3 - Selected Option + 5% - C3 Mode Rev. 5A

507.4 0.63 0.110 0.086 8.06 43.98 23090 45.5

Page 10 o l i o

505.8 0.63 0.107 0.085 7.62 43.96 47140 93.2

558.7 0.58 0.158 0.104 12.57 43.96 20190 36.1

560.3 0.58 0.163 0.106 13.07 43.99 19682 35.1

530.6 0.57 0.160 0.106 13.14 44.49


Ethane Recovery Maximization (ERM) Project Material Balance Max. Condensate Case - C2 Rejection Mode Rev.2


ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Material Balance Max. Condensate Case C2 Rejection Mode Revision 2

Rev.

Date

Description

13-Feb-04


4-Sep-03

Approved for Design

By

Chk.

Disc.

GS-L-FML046

'prsOPM

DTS


ED



MAX. CONDENSATE CASE - C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane 1-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weigh! Mass Flow (kg'h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) 0

10

11

20

22

23

24

104.6 24757.9 3193.1 1849.2 560.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 582.2 0.0 0.0 0.0 0.2 22.0

103 5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 12 0.0 0.6 582.2 0.0 0.0 0.0 0.2 0.0

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

1.1 557.9 226.0 286.4 147.4 269.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 00 0.0 89.1

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

43.6 10186.2 1248.9 657.8 182.5 279.1 57.7 44.3 19.4 11.1 0.5 0.0 0.2 245.0 0.0 0.0 0.0 0.1 0.0

43.6 10186.2 1246.9 657.8 182.5 279.1 57.7 44.3 19.4 11.1 0.5 0.0 0.2 245.0 0.0 0.0 0.0 0.1 0.0

59.9 14013.8 1718.2 905.0 251.0 363.9 79.4 61.0 26.8 15.2 0.7 0.0 0.3 337.1 0.0 0.0 0.0 0.1 0.0

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

32920.0 758433 58.0 66.5 1.00 -696.3 23.04

32920.0 758433 44.8 65.8 0.98 -704.4 23.04

32920.0 758433 27.0 6S.4 0.94 -716.3 23.04

30851.1 663517 27.0 65.3 1.00 -647.3 21.51

30829.1 663120 27.8 62.8 1.00 -645.1 21.51

1979.8 93309 27.0 65.3 0.00 -63.0 47.13

1979.8 93309 17.4 31.4 0.24 -63.0 47.13

89.1 1607 27.0 65.3 0.00 -6.1 18.02

1979.8 93309 49.2 30.7 0.37 -60.6 47.13

12976.5 279118 27.6 62.5 1.00 -271.5 21.51

12976.5 279118 -4.0 60.8 0.91 -279.4 21.51

17852.5 384000 27.6 62.5 1.00 -373.5 21.51

13900.8 299000 27.5 62.4 1.00 -290.9 21.51

66.2 0.63 0.014 0.034 23.04 758432 659.7

68.0 0.64 0.014 0.033 22.50 726421 647.0

70.5 0.67 0.014 0.032 21.51 663625 618.3

70.3 0.67 0.014 0.032 21.51 663517 618.3

66.7 0.65 0.013 0.032 21.51 663120 617.8

70.3 0.67 0.014 0.032 21.51

32.8 0.55 0.012 0.027 22.21 10542 9.5

70.3 0.67 0.014 0.032 21.51

35.5 0.54 0.013 0.028 27.01 19602 14.5

66.4 0.65 0.013 0.032 21.51 279118 260.0

71.4 0.73 0.013 0.030 19.90 235403 237.0

66.4 0.65 0.013 0.032 21.51 384000 357.8

66.3 0.65 0.013 0.032 21.51 299000 278.6

515.2 0.61 0.119 0.072 7.54 53.40 31069 60.3

499.6 0.61 0.112 0.073 7.32 47.11 93202 186.5

499.9 0.61 0.113 0.073 7.32 47.13

499.9 0.61

567.6 0.58 0.158 0.080 10.21 55.00 82763 145.8

499.9 0.61 0.113 0.073 7.32 47.13

543.3 0.61 0.131 0.073 8.32 58.77 73708 135.7

943

1606

Sftnulation Baeis: Train 3 - Mar Condensale + S% - C3 Mode Rev. 3A

0.113 0.073 7.32 47.13 93309 186.7

1607

Page 1 of 10

475.3 0.63 0.101 0.078 7.34 38.08 43715 92.0

FIUOR


Contract AOWT Rev. 2

MAX. CONDENSATE CASE • C2 REJECTION MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature CC) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Denslly (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg*)

25

•

26

28

29

30

31

32

33

34

36

37

38

43

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

13.3 3102.0 380.3 200.3 55.6 85.0 1 7.6 1 3.5 5.9 3.4 0.1 0.0 0.1 74.6 0.0 0.0 0.0 0.0 0.0

13.3 3102.0 380.3 200.3 55.6 85.0 17.6 13.5 5.9 3.4 0.1 0.0 0.1 74.6 0.0 0.0 0.0 0.0 0.0

59.9 14013.8 1718.2 905.0 251.0 383.9 79.4 61.0 26.8 15.2 0.7 0.0 0.3 337.1 0.0 0.0 0.0 0.1 0.0

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 562.2 0.0 0.0 0.0 0,2 0.0

101.1 22822.1 2376.8 919.4 177.7 225.4 26.3 17.2 3.3 1.0 0.0 0.0 0.5 516.6 0.0 0.0 0.0 0.0 0.0

69.8 15749.9 1640.3 634.5 122.6 155.5 18.1 11.9 2.3 0.7 0.0 0.0 0.3 356.5 0.0 0.0 0.0 0.0 0.0

69.8 15749.9 1640.3 634.5 122.6 155.5 18.1 11.9 2.3 0.7 0.0 0.0 0.3 356.5 0.0 0.0 0.0 0.0 0.0

16.0 3609.6 375.9 145.4 28.1 35.6 4.2 2.7 0.5 0.2 0.0 0.0 0.1 81.7 0.0 0.0 0.0 0.0 0.0

16.0 3609.6 375.9 145.4 28.1 35.6 4.2 2.7 0.5 0.2 0.0 0.0 0.1 81.7 0.0 0.0 0.0 0.0 0.0

101.1 22822.1 2376.8 919.4 177.7 225.4 26.3 17.2 3.3 1.0 0.0 0.0 0.5 516.6 0.0 0.0 0.0 0.0 0.0

99.3 21869.1 2006.0 599.6 84.2 89.8 6.1 3.4 0.3 0.0 0.0 0.0 0.4 471.5 0.0 0.0 o.o 0.0 0.0

99.3 21869.1 2006.0 599.6 84.2 89.8 6.1 3.4 0.3 0.0 0.0 0.0 0.4 471.5 0.0 0.0 o.o 0.0 0.0

13900.8 299000 -5.7 61.3 0.90 -299.8 21.51

3951.7 85000 27.5 62.4 1.00 -82.7 21.51

3951.7 85000 -21.8 60.9 0.83 -86.6 21.51

17852.5 384000 -15.9 60.8 0.86 -389.0 21.51

30829.1 663120 -11.0 60.7 0.88 -668.4 21.51

27187.4 630687 -11.0 60.7 1.00 -564.5 19.52

18762.4 366234 -11.0 60.7 1.00 -389.6 19.52

18762.4 366234 -31.0 60.2 0.93 -397.2 19.52

4300.0 83934 -11.0 60.7 1.00 -89.3 19.52

4300.0 83934 -30.9 60.2 0.93 -91.0 19.52

27187.4 530687 -30.7 60.2 0.93 -575.4 19.52

25229.7 471978 -30.7 60.2 1.00 -523.5 18.71

25229.7 471978 -49.0 39.6 0.95 -526.3 18.71

72.6 0.74 0.013 0.030 19.81 248878 251.8

66.3 0.65 0.013 0.032 21.51 85000 79.2

77.4 0.82 0.012 0.029 18.96 61915 65.4

75.0 0.78 0.012 0.029 19.26 295152 307.1

73.2 0.76 0.012 0.029 19.52 530652 544.8

73.3 0.76 0.012 0.029 19.52 530667 544.8

73.2 0.76 0.012 0.029 19.52 366178 376.0

82.4 0.92 0,012 0.029 18.69 324858 348.3

73.2 0.76 0.012 0.029 19.52 83922 86.2

82.3 0.92 0.012 0.029 18.70 74495 79.9

82.1 0.91 0.012 0.029 18.70 471765 505.5

82.4 0.91 0.012 0.029 18.71 471978 505.6

51.3 0.74 0.010 0.024 18.05 430893 478.4

472.7 0.63 0.099 0.078 7.29 37.53 50122 106.0

•— ----

459.7 0.64 0.093 0.080 7.17 33.65 23085 50.2

455.9 0.63 0.096 0.079 7.27 35.14 88848 190.7

470.4 0.63 0.098 0.079 7.33 36.37 132468 281.6

470.3 0.63 0.098 0.079 7.32 36.37 -

470.3 0.63 0.098 0.079 7.33 36.36 58 0.1

429.6 0.68 0.078 0.080 6.47 29.92 41376 96.3

470.3 0.63 0.098 0.079 7.33 36.36 13 0.0

429.8 0.68 0.079 O.OBO 6.4B 29.94 9439 22.0

430.4 0.68 0.079 0.080 6.49 30.00 58922 136.9

430.0 0.68 0 079 0.080 6.48 29.99 -

475.5 0.64 0.097 0.087 6.31 30.31 41084 86.4

SimuiaUm Basis: Train 3 - Max Condensale * 5% - C3 Mode Rev. 5A

Page 2 0110

FLUOR


Contract AOWT Rev.2


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Uquld Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) 0

50

52

53

54

56

57

58

70

72

73

75

76

77

2.4 1377.9 590.2 643.4 255.8 437.6 110.9 88.1 42.9 25.3 1.2 0.0 0.1 65.6 0.0 o.o 0.0 0.2 0.0

1.7 587.4 65.4 20.9 3.4 4.0 0.4 0.2 0.0 0.0 0.0 0.0 0.0 14.7 0.0 0.0 0.0 0.0 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 87.9 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

1.7 953.1 370.9 319.9 93.5 135.5 20.2 13.8 3.0 1.0 0.0 0.0 0.1 45.0 0.0 0.0 0.0 0.0 0.0

1.2 363.7 32.0 7.0 0.8 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 8.4 0.0 0.0 0.0 0.0 0.0

0.5 569.4 338.8 312.8 92.8 134.8 20.2 13.8 3.0 1.0

103.5 24200.1 2880.1 157.6 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

103.5 24200.0 2880.1 157.7 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

103.5 24200.0 2880.1 157.7 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

103.5 24200.0 2880.1 157.7 2.9 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.6 582.1 0.0 0.0 0.0 0.0 0.0

96.9 22646.3 2695.2

o.i 36.7 0.0 0.0 0.0 0.0 0.0

2.9 971.1 97.4 27.9 4.2 4.7 0.4 0.3 0.0 0.0 0.0 0.0 0.0 23.1 0.0 0.0 0.0 0.0 0.0

3641.7 132433 •11.0 60.7 0.00 •103.8 36.37

698.3 13489 •19.7 39.7 1.00 -14.5 19.32

2940.4 118944 -19.7 39.7 0.00 -89.3 40.41

1957.7 58710 -30.7 60.2 0.00 -51.8 29.99

433.9 7922 -422 39.7 1.00 -8.9 18.26

1523.8 50788 -42.2 39.7 0.00 -42.9 33.33

1132.2 21411 -27.9 39.7 1.00 -23.4 18.91

27928.1 510575 -55.3 39.5 1.00 -581.4 1828

27928.1 510578 -41.5 39.1 1.00 -576.0 18.28

0.0 0 22.6 38.6 1.00 0.0 18.26

27928.1 510578 -9.2 38.8 1.00 -565.6 18.28

27928.1 510578 22.6 38.6 1.00 -556.1 18.28

26135.1 477799 22.6 38.4 1.00 -520.4 18.28

73.3 0.76 0.012 0.029 19.52

44.6 0.62 0.011 0.026 19.32 13489 14.0

44.6 0.62 0.011 0.026 19.32

82.4 0.91 0.012 0.029 18.71

49.0 0.70 0.010 0.024 18.26 7922 8.7

49.0 0.70 0.010 0.024 18.26

45.8 0.65 0.011 0.025 18.88 21337 22.7

56.6 0.82 0.010 0.024 18.28 510573 559.7

47.8 0.69 0.010 0.024 18.28 510578 559.7

31.4 0.57 0.012 0.030 18.28

37.3 0.59 0.011 0.027 18.28 510578 559.7

31.4 0.57 0.012 0.030 18.28 510578 559.7

31.2 0.57 0.012 0.030 18.28 477799 523.7

470.3 0.63

525.9 0.59 0.130 0.085 9.59 40.41

525.9 0.59 0.130 0.085 9.59 40.41 118944

430.0 0.68 0.079 0.080 6.48 29.99 58710 136.5

497.4 0.62

497.4 0.62 0.111 0.087 9.00 33.33 50788 102.1

5178 0.60 0.125 0.086 9.51 37.92 74 0.1

416.2 0.74 0.066 0.086 6.43 25.00 2 0.0

0.098 0.079 7.32 36.37 132433 281.6

Simulation Basis: Train 3 • Max Condensate t 5% - C3 Mode Rev. 5A

226.2

0.111 0.087 9.00 33.33

PageSol 10

o.o 0.0

147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0


OASCO Ethane Recovery Maximization


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Penlane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Tolal Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kgm)

78

79

80

81

96.9 22646.3 26952 147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

96.9 22646.3 2695.2 147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

96.9 22646.3 2695.2 147.5 2.7 1.3 0.0 0.0 0.0 0.0 0.0 0.0 0.5 544.8 0.0 0.0 0.0 0.0 0.0

6.6 1553.7 184.9 10.1 0.2 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 37.4 0.0 0.0 0.0 0.0 0.0

26135.1 477799 52.4 38.0 1.00 •512.3 18.28

26135.1 477799 64.7 43.5 1.00 •509.5 18.28

26135.1 477799 54.0 42.8 1.00 -512.4 18.28

1793.0 32779 22.6 38.4 1.00 -35.7 18.28

27.2 0.57 0.013 0.033 18.28 477799 523.7

29.9 0.58 0.013 0.035 18.28 477799 523.7

30.7 0.57 0.013 0.034 18.28 477799 523.7

31.2 0.57 0.012 0.030 18.28 32779 35.9

Simulation Basis: Tram 3 • Max Condensale • 5% • C3 Mode Rev. 5A

90

91

92

93

94

95

96

103

1.3 1520.9 1439.3 775.7 100.2 103.8 6.7 3.8 0.3 0.1 0.0 0.0 0.3 124.2 0.0 0.0 0.0 0.0 0.0

1.3 1520.9 1439.3 775.7 100.2 103.8 8.7 3.8 0.3 0.1 0.0 0.0 0.3 124.2 0.0 0.0 0.0 0.0

0.1 208.4 1557.1 1159.9 114.4 114.2 7.0 3.9 0.3 0.1 0.0 0.0 0.3 35.3 0.0 0.0 0.0 0.0 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 879 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 87.9 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

0.7 790.5 524.8 622.5 252.3 433.6 110.5 87.9 42.9 25.3 1.2 0.0 0.1 50.9 0.0 0.0 0.0 0.2 0.0

0.5 569.4 338.8 312.8 92.8 134.8 20.2 13.8 3.0 1.0 0.0 0.0 0.1 36.7 0.0 0.0 0.0 0.0 0.0

0.5 569.4 338.8 312.8 92.8 134.8 20.2 13.8 3.0 1.0 0.0 0.0 0.1 36.7 0.0 0.0 0.0 0.0 0.0

0.1 157.4 919.6 2020.0 349.1 433.7 48.2 31.6 6.0 1.9 0.0 0.0 0.2 22.9 0,0 0.0 0.0 0.0 0.0

4076.3 120037 -40.9 39.6 0.00 -108.6 29.45

4076.3 120037 -52.2 25.2 0.17 •108.6 29.45

3201.0 116987 2.7 29.6 0.00 •86.6 36.55

2943.4 118944 •26.4 25.5 0.13 -89.3 40.41

2943.4 118944 14.0 24.8 0.33 -85.4 40.41

2943.4 118944 30.0 24.1 0.44 -83.4 40.41

1523.8 50788 •52.1 24.8 0.17 -42.9 33.33

1523.8 50788 •15.8 24.1 0.41 •41.2 33.33

3990.7 172250 33.9 23.8 0.00 •115.1 43.16

28.0 0 55 0.010 0.023 19.59 7747 7.9

29.8 0.52 0.011 0.024 24.94 24462 19.7

31.1 0.52 0.011 0.024 27.98 36473 26.1

29.2 0.59 0.009 0.021 18.19 4652 5.1

28.5 0.53 0.010 0.023 21.84 13645 12.5

560.6 0.57 0.163 0.091 11.56 43.64 111197 198.3

533.6 0.60 0.130 0.079 8.B4 48.14 94481 177.1

523.4 0.61 0.120 0,074 7.86 50.29 82471 157.6

544.1 0.58 0.152 0.096 11.57 36.38 46135 84.8

531.8 0.59 0.133 0.088 9.86 41.32 37142 69.8

o.o

31.5 0.60 0.009 0.021 18.91 13137 13.9 455.4 0.67 0.083 0.088 7.51 29.45 120037 263.6

Page 4 ol 10

504.6 0.62 0.113 0.097 9.88 31.61 106899 211.8

466.6 0.66 0.087 0.080 5.97 38.55 116987 250.7

468.2 0.67 0.085 0.070 5.25 43.16 172250 367.9


GASCO Elhana Recovery Maximization


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentana n-Hexane NBP91 NBP138 NBP1B2 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Row (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heal Capadty (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) n

104

109

110

0.1 157.4 919.6 2020.0 349.1 433.7 46.2 31.6 6.0 1.9 0.0 0.0 0.2

0.0 0.0 87.0 1405.3 430.6 661.7 137.2 105.3 46.2 26.3 1.2 0.0 0.0 0.0

1.3 1567.9 2333.5 689.7 28.9 20,9 0.5 0.2 0.0 0.0 0.0 0.0 0.5 122.8 0.0 0.0 0.0 0.0 0.0

22.9 0.0 0.0 0.0 0.0 0.0 3990.7 172250 46.0 23.8 0.17 •112.1 43.16

o.o 0.0 0.0 0.2 0.0 2901.0 152546 88.1 23.9 0.00 •89.3 52.58

43.2 0.58 0.011 0.022 36.60 24931 13.7 457.5 0.70 0.082 0.067 4.63 44.51 147319 322.0

Simulallon Basis: rrain 3 - Max Condensate -* 5% - C3 Mode Rev. 3A

439.3 0.75 0.076 0.055 2.95 52.58 152546 347.3

111 2.5 2880.7 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 O.O 0.4 211.7 0.0 0.0 0.0 0.0 0.0

112

113

115

116

117

118

119

120

121

2.5 2680.8 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

2.5 2880.8 2216.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

2.5 2880.7 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0

2.5 2880.7 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 00 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0

0.0

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2 0.1 0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 O.O 0.0

0.0 0.0 0.0 0.0 0.0

o.o 0.0

o.o o.o 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

4766.2 134139 5.3 23.7 1.00 •108.4 28.14

5642.5 137221 •17.5 23.3 1.00 -129.0 24.32

5642.6 137223 -11.0 22.9 1.00 •128.4 24.32

5642.6 137223 21.0 22.6 1.00 -126.1 24.32

5642.6 137223 85.4 52.5 1.00 -122.7 24.32

5642.5 137221 85.4 52.5 1.00 -122.7 24.32

0.0 1 85.4 52.5 1.00 0.0 24.32

5642.5 137221 47.7 51.9 1.00 -125.7 24.32

36.1 0.54 0.010 0.021 28.14 134139 95.5

32.5 0.54 0.010 0.021 24.29 136608 112.7

30.5 0.52 0.010 0.021 24.32 137223 113.1

25.1 0.50 0,011 0.024 24.32 137223 113.1

48.2 0.58 0.014 0.033 24.32 137223 113.1

48.2 0.58 0.014 0.033 24.32 137221 113.1

48.2 0.58 0.014 0.033 24.32 1

57.5 0.60 0.013 0.030 24.32 137221 113.1

468.6 0.67 0.088 0.080 6.01 37.27 0 0.0

482.8 0.65 0.095 0.089 7.51 34.58 613 1.3

Page 5 o f l 0

0.0

o.o 0.0 0.0 0.0 0.0 0.0

o.o 0.0 0.0 0.0 0.0 0.0

o.o o.o i 85.4 52.5 1.00 0.0 24.32 48.2 0.58 0.014 0.033 24.32 1 0.0

0.0 0.0

o.o o.o o.o o.o 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 1 55.0 51.9 1.00 0.0 24.32 55.1 0.59 0.013 0.030 24.32 1 0.0

5642.6 137223 47.7 51.9 1.00 -125.7 24.32 57.5 0.60 0.013 0.030 24.32 137223 113.1




StreamNumber Composition (kgmole/h) Nitrogen Methane Ethane propane I-Butane n-Butane i-Pentane

122

123

124

125

126

127

128

129

130

131

132

141

142

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

2.5 2880.8 2215.9 305.6 14.7 10.5 0.2

0.8 867.9 667.6 92.1 4.4 3.2 0.1

0.8 867.9 667.6 92.1 4.4 3.2 0.1

0.0 0.0 87.0 1405.3 430.6 661.7 137.2

0.0 0.0 87.0 1405.3 430.6 661.7 137.2

0.0 0.0 87.0 1405.3 430.6 661.7 1372

0.0 0.0 126.9 2048.8 627.6 961.2 65.7

0.0 0.0 126.9 2048.8 627.6 961.2 65.7

0.1

0.1

0.1

0.1

0.1

0.1

0.0

0.0

105.3

105.3

105.3

30.2

30.2

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.4 211.7 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.1 63.8 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.1 63.8 O.O 0.0 0.0 0.0 0.0

46.2 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

46.2 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

46.2 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

5642.6 137223 24.5 51.5 1.00 -127.6 24.32

5642.6 137223 -4,0 51.2 0.87 -131.5 24.32

5642.6 137223 -17.0 51.0 0.58 -134.9 24.32

5642.6 137223 -25.3 50.7 0.41 -136.9 24.32

5642.6 137223 -54.4 50.5 0.00 -142.3 24.32

5842.6 137223 -55.9 39.5 0.02 -142.3 24.32

1700.0 41342 -17.0 51.0 0.58 -40.6 24.32

1700.0 41342 -47.3 50.7 0.00 -42.6 24.32

2901.0 152546 75.0 18.0 0.16 -89.3 52.58

2901.0 152546 73.8 16.8 0.29 -88.3 52.58

2901.0 152546 73.1 16.5 0.30 -88.3 52.58

3861.2 193488 74.9 16.0 1.00 -104.2 50.11

3861.2 193488 59.9 22.5 0.00 -118.7 50.11

66.7 0.65 0.013 0.028 24.32 137223 113.1

82.4 0.85 0.012 0.027 23.58 115349 98.1

80.1 0.87 0.012 0.027 21.98 71818 65.5

78.6 0.89 0.012 0.027 21.01 48026 45.8

57.4 0.83 0.010 0.024 18.35 2577 2.8

80.1 0.87 0.012 0.027 21.98 21637 19.7

39.8 0.59 0.011 0.021 48.04 22767 9.5

37.0 0.58 0.010 0.021 48.50 40576 16.8

36.3 0.57 0.010 0.021 48.50 41599 17.2

36.4 0.58 0.010 0.021 50.11 193488 77.4

— -

371.0 0.85 0.053 0.076 3.96 29.17 21874

374.3 0.64 0.053 0.080 4.56 27.53 65405

376.4 0.83 0.053 0.081 4.90 26.58 89197

402.3 0.76 0.061 0.084 5.39 24.32 137223

409.2 0.76 0.062 0.085 6.22 24.47 134646

374.3 0.84 0.053 0.080 4.56 27.53 1970S

383.8 0.80 0.055 0.083 5.46 24.32 41342

471.7 0.69 0.089 0.061 4.34 53.47 129779

478.9 0.68 0.093 0.062 4.65 54.24 111970

480.6 0.68 0.094 0.062 4.74 54.30 110947

— -

478.4 0.68 0.092 0.065 4.92 50.11 193488

—

59.0

174.8

237.0

34t.1

329.0

52.7

107.7

275.1

233.8

230.8

—

404.5

n-Pentane

n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature C O Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Sld Gas Flow (MMSCFD) Hydrocartxm Uquld Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual V o l u m e ROW (m3m)

— -

Water Phase Mass Flow (kgm)

Simulalioo Basla: Train 3 - Max Conflonsala + 5% • C3 Moda Rev. 5A

Page6ot 10

— — — — -




Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane l-Butane n-Butane i-Peraane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

150

151

152

153

501

502

503

504

505

507

600

601

602

0.0 0.0 87.0 1405.3 430.5 659.3 45.1 20.7 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0 0.0

0.0 0.0 0.0 0.0 0.1 2.4 92.1 84.5 45.8 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

0.0 0.0 0.0 0.1 2.4 92.1 84.5 45.8 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0

15.3 3454.3 359.8 139.2 26.9 34.1 4.0 2.6 0.5 0.2 0.0 0.0 0.1 78.2 0.0 0.0 0.0 0.0 0.0

15.3 3454.3 359.8 139.2 26.9 34.1 4.0 2.6 0.5 0.2 0.0 0.0 0.1 78.2 0.0 0.0 0.0 0.0 0.0

1.3 1520.9 1439.3 775.7 100.2 103.8 6.7 3.8 0.3 0.1 0.0 0.0 0.3 124.2 0.0 0.0 0.0 0.0 0.0

1.1 881.4 198.9 24.7 1.1 0.7 0.0 0.0 0.0 0.0 0.0 0.0 0.0 37.7 0.0 0.0 0.0 0.0 0.0

0.2 639.5 1240.4 750.9 99.1 103.0 6.7 3.8 0.3 0.1 0.0 0.0 0.2 86.5 0.0 0.0 0.0 0.0 0.0

0.2 639.5 1240.4 750.9 99.1 103.0 6.7 3.8 0.3 0.1 0.0 0.0 0.2 86.5 0.0 0.0 0.0 0.0 0.0

0.2 639.9 1240.6 751.1 99.2 103.1 6.7 3.8 0.3 0.1 0.0 0.0 0.2 86.5 0.0 0.0 0.0 0.0 0.0

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

1.4 1999.3 2017.0 280.9 13.6 9.8 0.2 0.1 0.0 0.0 0.0 0.0 0.4 174.1 0.0

252.7 19833 80.3 15.6 0.00 -10.6 78.50

252.7 19833 49.0 15.4 0.00 •11.0 78.50

4115.0 80323 -11.0 60.7 l.OO -85.5 19.52

4115.0 80323 -29.2 60.2 0.94 -87.0 19.52

4076.3 120037 •41.7 24.6 0.28 -107.1 29.45

1145.6 23005 -41.7 24.6 1.00 -25.0 20.08

2930.8 97031 -41.7 24.6 0.00 -62.2 33.11

2930.8 97031 -42.8 23.3 0.02 -62.2 33.11

2931.8 97065 -42.8 23.3 0.02 -82.2 33.11

13900.8 299000 -14.1 60.9 0.87 -302.3 21.51

4497.0 114216 -12.5 23.3 1.00 -104.0 25.40

73.2 0.76 0.012 0.029 19.52 80311 82.5

81.4 0.90 0.012 0.029 18.77 72273 77.2

30.8 0.57 0.010 0.021 20.08 23005 23.0

30.8 0.57 0.010 0.021 20.08 23005 23.0

30.8 0.57 0.010 0.021 20.08

29.1 0.56 0.009 0.021 20.11 972 1.0

29.1 0.56 0.009 0.021 20.11 981 1.0

74.5 0.78 0.012 0.029 19.35 233213 241.5

33.6 0.54 0.010 0.021 25.40 114216 90.1

470.3 0.63 0.098 0.079 7.33 36.36 12 0.0

433.4 0.67 0.080 0.060 6.56 30.44 8050 18.6

504.9 0.62 0.111 0.096 9.57 33.11 97031 192.2

504.9 0.62 0.111 0.096 9.57 33.11

504.9 0.62 0.111 0.096 9.57 33.11 97031 192.2

509.1 0.62 0,114 0.097 9.82 33.33 96060 188.7

509.1 0.62 0.114 0.097 9.82 33.33 96083 188.7

467.2 0.63 0,097 0.079 7.28 35.55 65787 140.8

477.3 0.65 0.092 0.086 7.00 34.83 0 0.0

2648.3 132710 59.9 22.5 0.00 -81.4 50.11

478.4 0.68 0.092 0.065 4.92 50.11 132710 277.4

Simulation Basis: Train 3 • Max Contonsato + 5% • C3 Mode Rev. 5A

o.o 0.0 0.1 2.4 92.1 84.6 45.8 26.3 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.2 0.0 252.7 19836 159.2 16.3 0.00 -9.6 78.50

468.8 0.75 0.083 0.049 3.19 78.50 19836 42.3

584.2 0.61 0.156 0.077 10.25 78.50 19833 34.0

o.o

618.0 0.58 0.202 0.085 13.40 78.50 19833 32.1

Page7ol 10

o.o 0.0 0.0 0.0


GASCO Ethane Recoveiy Maximization


Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S

C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Row (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

604

605

606

607

0.1 208.4 1557.1 1159.9 114.4 114.2 7.0 3.9 0.3 0.1 0.0 0.0 0.3 35.3 0.0 0.0 0.0 0.0 0.0

0.0 0.0 126.9 2048.8 627 6 961.2 65.7 30.2 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

0.0 0.0 126.9 2048.8 627.6 961.2 65.7 30.2 0.5 0.0 0.0 0.0 0.0 0.1 0.0 0.0 0.0 0.0 0.0

0.0 0.0 87.0 1405.3 430.5 659.3 45.1 20.7 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

3201.0 116987 2.7 27.0 0.00 -86.6 36.55

3861.2 193488 59.1 15.7 0.00 -118.7 50.11

3861.2 193488 59.1 15.5 0.00 -118.7 50.11

2648 3 132710 35.0 22.0 0.00 -83.5 50.11

466.7 0.66 0.087 0.080 5.97 36.55 116987 250.7

476.2 0.68 0.093 0.066 4.99 50.11 193488 406.3

476.2 0.68 0.093 0.066 4.99 50.11 193488 406.3

518.9 0.62 0.116 0.075 7.51 50.11 132710 255.7

Stmulalron Basis: Train 3 - Max Condansata + 5% • C3 Moda Rav. 5A

PageSol 10

FLUOR Conirad AOWT Rev.2


MAX. CONDENSATE CASE - C2 REJECTION MODE - REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Elhane Propane I-Butane Total Stream Molar Row (kgmole/h) Mass Flow (kg/h) Temperature f C ) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume Flow (m3/h)

200

201

202

203

204

205

206

207

208

210

213

220

701

157.8 7652.4 78.9

157.8 7652.4 78.9

157.8 7652.4 78.9

22.5 2677.4 43.7

22.5 2677.4 43.7

22.5 2677.4 43.7

22.5 2677.4 43.7

7.8 4162.0 194.5

7.8 4162.0 194.5

135.3 4975.0 35.2

135.3 4975.0 35.2

157.8 7652.4 78.9

49.1 2383.7 24.6

7889.1 346778 57.4 21.0 0.00 -218.4 43.96

7889.1 346778 48.4 20.3 0.00 -220.7 43.96

7889.1 346778 19.6 8.6 0.24 -220.7 43.96

2743.6 121282 20.3 8.6 0.00 -79.4 44.21

2743.6 121282 -10.2 3.5 0.20 -79.4 44.21

2743.6 121281 -9.3 3.5 1.00 -70.4 44.21

2743.6 121281 -9.5 3.4 1.00 -70.4 44.21

4364.3 195070 -9.3 3.5 0.00 -131.0 44.70

4364.3 195070 -8.7 3.5 0.50 -122.0 44.70

5145.5 225496 20.3 8.6 1.00 -129.5 43.82

5145.5 225496 19.8 8.4 1.00 -129.5 43.62

7889.0 346777 71.6 21.7 1.00 •193.8 43.96

2457.4 108021 54.5 19.8 0.00 -68.3 43.96

18.2 0.47 0.008 0.016 43.58 81605 37.5

18.3 0.47 0.008 0.016 43.82

7.5 0.40 0.007 0.013 43.89 24519 11.2

7.6 0.40 0.007 0.013 44.21 121281 55.0

7.3 0.40 0.007 0.0)3 44.21 121281 55.0

7.6 0.40 0.007

7.6 0.40 0.007 0.013 44.39 96866 43.7

18.3 0.47 0.008 0.016 43.82 225496 103.1

17,8 0.47 0.008 0.016 43.82 225496 103.1

45.2 0.61 0.011 0.022 43.96 346777 158.1

44.4 0.63 0.010 0.020 43.56

500.4 0.64 0.105 0.084 7.49 44.07 265173 529.9

500.2 0.64 0.105 0.084 7.46 44.21 121262 242.4

543.2 0.59 0.142 0.099 11.26 44.29 96763 178.1

543.9 0.59 0.143 0.098 11.23 44.70

544.6 0.59 0.145 0.097 11.22 45.00 98205 180.3

500.2 0.64 0.105 0.084 7.46 44.21

47.7 0.66 O.OIO 0.021 43.58

432.3 0.77 0.072 0.065 3.28 43.96 346778 802.2

Simulabixi Basis: Train 3 • Max Condensata * 5% - C3 Mode Rav. 5A

452.8 0.72 0.079 0.069 4.21 43.96 346778 765.8

Page 9 ol 10

0.013 44.21

543.9 0.59 0.143 0.098 11.23 44.70 195070 358.6

436.4 0.75 0.074 0.066 3.57 43.96 108021 246.4



MAX. CONDENSATE CASE - C2 REJECTION MODE - REFRIGERATION SYSTEMS

Stream Number Composilion (kgmole/h) Ethane Propane i-Butane Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperalure (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h)

706

708

709

711

712

716

718

722

723

724

727

732

11.9

576.0 5.9

11.9 575.0 5.9

11.9 575.0 5.9

0.0 1.0 0.0

0.0 1.0 0.0

56.2 2725.5 28.1

22.5 1088.9 11.2

12.0 580.3 6.0

12.0 580.3 6.0

12.0 580.3 6.0

20.0 967.7 10.0

76.1 3693.2 38.1

593.8 26102 18.1 19.2 0.00 -17.1 43.96

5928 26058 14.5 7.6 0.03 •17.1 43.96

592.8 26058 16.0 7.6 I. 00 -15.0 43.96

1.0 44 14.5 7.6 0.03 0.0 43.96

1.0 44 14.3 7.6 0.03 0.0 43.96

2809.6 123511 17.4 7.4 1.00 -70.9 43.96

1122.6 49346 18.1 19.2 0.00 -32.4 43.96

598.2 26295 •21.3 18.7 0.00 -17.9 43.96

598.2 26295 -25.0 2.2 0.03 -17.9 43.96

598.2 26295 •23.5 2.1 1.00 •15.4 43.96

997.6 43852 •21.0 2.0 1.00 -25.6 43.96

3807.4 167362 77.9 20.3 1.00 -92.7 43.96

16.1 0.46 0.008 0.015 43.28 724 0.3

16.2 0.46

16.1 0.46 0.006 0.015 43.28 1 0.0

16.0 0.46 0.008 0.015 43.29 1 0.0

15.7 0.46 0.008 0.015 43.96 123511 56.3

4.8 0.38 0.007 0.012 42.87 661 0.3

4.8 0.38 0.007 0.011 43.96 26295 12.0

4.5 0.38 0.OO7 0.012

39.4 0.58 0.011 0.022 43.96 167362 76.3

507.4 0.63 0.110 0.086 8.06 43.98 43 0.1

507.7 0.63 0.110 0.086 8.08 43.98 43 0.1

467.1 0.63 0.103 0.085 7.84 44.35

505.8 0.63 0.107 0.085 7.62 43.96 26102 51.6

Simulallon Basis: Train 3 • Max Condensale • 5% - C3 Mode Rev. SA

507.4 0.63 0.110 0.086 8.06 43.98 25334 49.9

0.008

0.015 43.96 26058

II. 9

Page 10 o l i o

505.8 0.63 0.107 0.085 7.62 43.96 49346 97.6

558.7 0.58 0.158 0.104 12.57 43.98 26295 47.1

560.3 0.58 0.163 0.106 13.07 43.99 25634 45.8

43.96

43852 20.0 526.0 0.58 0.154 0.104 12.70 44.48


Ethane Recovery Maximization (ERM) Project Material Balance Low Condensate Case - C2 Recovery Mode Rev.2


ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Material Balance Low Condensate Case C2 Recovery Mode Revision 2

Approved Rev.

Date

Description

13-Feb-04


4-Sep-03

7-Aug-03

By

Chk.

Disc.

Proj.

GASCO

GS-L-FML046

Approved for Design

m

OPM

DTS

ED

Issued for Approval

OPM

DTS

ED

FLUOH Contract A O W T Rev. 2


LOW CONDENSATE CASE - C2 RECOVERY MODE

S t r e a m Number C o m p o s i l i o n (kgmole/h) Nitrogen Methane Elhane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 HSS C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total S t r e a m Molar Flow ( k g m o l e * ) M a s s Flow (kg/h) Temperalure ("C) Pressure (bara) Vapour Fraction Heat F l o w (Gcal/h) Molecular Weight Vapor P h a s e Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight M a s s Flow (kg/h) Std G a s F l o w ( M M S C F D ) Hydrocarbon Liquid P h a s e Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP)

1

10

11

20

22

23

24

0.0 0.0 0.0 0.0 0.0 0.0 0.0

39.5 10013.0 1165.5 5BB.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

39.5 10013.0 1165.5 588.2 162.9 249.7 55.6 43.1 20.5 13.1 0.6 0.0 0.2 275.2 0.0 0.1 0.1 0.2 0.0

56.3 14281.0 1662.3 838.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5 0.0 0.2 0.2 0.3 0.0

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

96.6 24733.6 3000.5 1639.8 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

96.6 24733.6 3000.5 1639.8 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0,6 690.4 0.0 0.4 0.4 1,5 110.5

96.6 24733.6 3000.5 1639.8 505.5 824.2 229.9 191.7 143.0 138.7 20.8 1.9 0.6 690.4 0.0 0.4 0.4 1.5 110.5

95.8 24294.1 2B27.B 1427.1 39S.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 21.9

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 0.0

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.8 439.5 172.7 212.6 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 87.7

0.8 439.5 172.7 2126 110.3 218.5 95.0 87.0 93.2 106.9 19.3 1.9 0.0 22.7 0.0 0.1 0.1 1.0 0.9

32330.0 732576 58.0 66.5 1.00 -686.7 22.66

32330.0 732576 44.4 65.8 0.98 -694.6 22.66

32330.0 732576 27.0 65.4 0.95 •705.4 22.66

30659.8 653637 27.0 65.3 1.00 -647.7 21.32

30637.9 653242 27.8 62.8 1.00 -645.5 21.32

1582.5 77358 27.0 65.3 0.00 -51.7 48.88

1582.5 77358 18.1 31.4 0.23 •51.7 48.88

87.7 1581 27.0 65.3 0.00 -6.0 18.02

1582.5 77358 50.2 30.7 0.35 -49.8 48.88

12627.7 269240 27.6 62.5 1.00 •266.1 21.32

12627.7 269240 -22.5 60.8 0.84 -278.4 21.32

18010.1 384000 27.6 62.5 1.00 -379.5 21.32

14023.5 299000 27.5 62.4 1.00 •295.5 21.32

64.4 0.62 0.014 0.034 22.66 732575 647.9

66.5 0.64 0.014 0.033 22.17 704689 637.1

69.3 0.66 0.014 0.032 21.32 653737 614.4

69.2 0.66 0.014 0.032 21.32 653637 614.4

65.6 0.65 0.013 0.032 21.32 653242 614.0

69.2 0.66 0.014 0.032 21.32

32.4 0.54 0.012 0.027 22.08 8149 7.4

69.2 0.66 0.014 0.032 21.32

34.8 0.54 0.013 0.028 25.74 14870 11.1

65.3 0.65 0.013 0.032 21.32 269240 253.1

77.6 0.82 0.012 0.029 18.95 201505 213.1

65.3 0.65 0.013 0.032 21.32 384000 360.9

65.2 0.65 0.013 0.032 21.32 299000 281.0

530.4 0.60 0.129 0.073 8.00 55.55 26936 50.8

513.4 0.60 0.121 0.074 7.70 48.87 77259 150.5

513.6 0.60

513.6 0.60 0.121 0.074 7.71 48.88 77358 150.6

577.8 0.57 0.168 0.081 10.59 57.04 69207 119.8

513.6 0.60

553.2 0.60 0.138 0.074 8.68 60.88 62488 113.0

951

1580

Thermal Conductivity (Kcal/m-hr-C) S u r f a c e T e n s i o n (dyne/cm) Molecular W e i g h t M a s s Flow (kg/h) A c l u a l V o l u m e Flow (m3/h) Water Phase M a s s Ftow ( M i )

Simulaiion Basis Train 3 - Selected Option • 5% - C2 Mode Rev. BA

0.121 0.074 7.71 48.88

P a g e 1 o l 10

o.o

0.121 0.074 7.71 48.88

465.0 0.64 0.096 0.080 7.31

33.95 67735 145.7

FLUOR Conlract AOWT Rev.2



Stream Number Composilion (kgmo!e/h) Nitrogen Methane Elhane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Uquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Ftow {m3/h) Water Phase Mass Flow (kg/h)

25

26

28

29

30

31

32

33

34

36

37

38

43

43.9 11119.8 1294.4 653.2 160.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9 0.0 0.0 0.0 0.1 0.0

12.5 3161.2 368.0 185.7 51.4 78.8 17.6 13.6 6.5 4.1 0.2 0.0 0.1 86.9 0.0 0.0 0.0 0.1 0.0

56.3 14281.0 1662.3 838.9 232.3 356.1 79.3 61.5 29.2 18.7 0.9 0.0 0.3 392.5 0.0 0.2 0.2 0.3 0.0

95.8 24294.1 2827.8 1427.1 395.2 605.7 134.9 104.6 49.7 31.9 1.5 0.0 0.6 667.7 0.0 0.3 0.3 0.5 0.0

92.6 22268.9 2025.3 660.0 114.6 139.2 15.9 10.3 2.0 0.6 0.0 0.0 0.4 555.7 0.0 0.1 O.t 0.0 0.0

62.6 15029.6 1366.9 445.4 77.3 94.0 10.7 6.9 1.3 0.4 0.0 0.0 0.3 375.0 0.0 0.1 0.0 0.0 0.0

62.5 15029.6 1366.9 445.4 77.3 94.0 10.7 6.9 1.3 0.4 0.0 0.0 0.3 375.0 0.0 0.1 0.0 0.0 0.0

15.4 3699.2 336.4 109.6 19,0 23.1 2.6 1.7 0.3 0.1 0.0 0.0 0.1 92.3 0.0 0.0 0.0 0.0 0.0

15.4 3699.2 336.4 109.6 19.0 23.1 2.6 1.7 0.3 0.1 0.0 0.0 0.1 92.3 0.0 0.0 0.0 0.0 0.0

92.6 22269.1 2025.4 660.0 114.6 139.3 15.9 10.3 2.0 0.6 0.0 0.0 0.4 555.7 0.0 0.1 0.1 0.0 0.0

90.3 20994.1 1624.6 390.5 47.6 48.1 3.1 1.7 0.1 0.0 0.0 0.0 0.3 490.2 0.0 0.0 0.0 0.0 0.0

90.3 20994.1 1624.8 390.5 47.6 48.1 3.1 1.7 0.1 0.0 0.0 0.0 0.3 490.2 0.0 0.0 0.0 0.0 0.0

14023.5 299000 -6.7 61.3 0.91 -304.5 21.32

3986.6 85000 27.5 62.4 1.00 -84.0 21.32

3986.6 85000 -35.3 60.9 0.75 -89.1 21.32

18010.1 384000 -21.6 60.8 0.85 -396.8 21.32

30637.9 653242 -22.0 60.7 0.84 -675.2 21.32

25865.7 491218 -22.0 60.7 1.00 •541.4 18.96

17470.6 331529 •22.0 60.7 1.00 •365,4 18.98

17470.6 331529 •41.5 60.2 0.92 -372.6 18.98

4300.0 81599 -22.0 60.7 1.00 -89.9 18.98

4300.0 81599 -44.0 60.2 0.90 -92.0 18.98

25886.0 491225 -42.2 60.2 0.91 -552.6 18.98

23691.0 432930 •42.2 60.2 1.00 •496.2 18.27

23691.0 432930 -59.5 40.6 0.93 -498.3 18.27

72.5 0.74 0.012 0.030 19.74 252750 256.6

65.2 0.65 0.013 0.032 21.32 85000 79.9

84.8 0.96 0.012 0.029 18.37 55242 60.3

77.1 0.82 0.012 0.029 19.00 289744 305.7

77.1 0.82 0.012 0.029 18.98 491188 518.7

77.2 0.82 0.012 0.029 18.98 491218 518.7

77.1 0.62 0.012 0.029 18.98 331481 350.1

90.9 1.10 0.012 0.029 18.30 294251 322.2

77.1 0.82 0.012 0.029 18.98 81587 86.2

93.5 1.16 0.012 0.030 18.20 70472 77.6

91.5 1.11 0.012 0.029 18.27 432670 474.6

91.8 1.12 0.012 0.029 18.27 432930 474.8

57.6 0.85 0.010 0.024 17.67 389966 442.3

443.9 0.66 0.085 0.080 6.79 30.39 29758 67.0

466.1 0.63 0.096 0.080 7.33 34.19 94256 2022

465.9 0.63 0.096 0.080 7.33 34.10 162054 347.8

465.8 0.63 0.096 0.080 7.33 34.09

465.8 0.63 0.096 0.080 7.33 34.09 49 0.1

402.6 0.73 0.067 0.078 5.76 26.82 37278 92.6

465.8 0.63 0.096 0.080 733 34.09 12 0.0

392.3 0.75 0.063 0.078 5.49 25.96 11126 28.4

399.9 0.73 0.066 0.078 5.69 26.57 58555 146.4

399.4 0.73 0.066 0.078 5.68 26.56

443.5 0.69 0.079 0.084 7.10 26.50 42964 96.9

479.5 0.62 0.103 0.079 7.49 37.98 46250 96.5

Simutation Basis: Train 3 - Selecled Oplion + 5% - C2 Mode Rev. 8A

Page 2 of 10


QASCO Ethane Recovery Maxtmization


Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Slream Molar Row (kgmole/h) Mass Flow (kg/h) Temperalure (°C) Pressure (bara) Vapour Fracilon Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density {kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

50

52

53

54

56

57

58

70

72

73

75

76

77

3.3 2025.2 802.5 767.2 280.6 466.5 119.0 94.3 47.8 31.2 1.5 0.0 0.2 112.0 0.0 0.2 0.2 0.5 0.0

22 806.1 73.3 18.9 2.7 3.0 0.3 0.2 0.0 0.0 0.0 0.0 0,0 21.5 0.0 00 0.0 0.0 0.0

1.0 1219.0 729.2 746,2 277.9 463.5 118.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0 0.2 0.2 0.5 0.0

2.3 1275.0 400.5 269.5 67.0 91.1 12.8 8.6 1.8 0.6 0.0 0.0 0.1 65.5 0.0 0.1 0.0 0.0 0.0

1.5 470.3 28.9 4.7 0.4 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 10.2 0.0 0.0 0.0 0.0 0.0

0.8 804.6 371.6 264.8 66.6 90.7 12.8 8.6 1.8 0.6 0.0 0.0 0.1 55.3 0.0 0.1 0.0 0.0 0.0

• 3.8 1276.4 102.2 23.6 3.1 3.4 0.3 0.2 0.0 0.0 0.0 0.0 0.0 31.7 0.0 0.0 0.0 0.0 0.0

95.8 24269.4 1722.0 105.2 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

95.8 24269.1 1722.0 105.2 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0

o.o o.o

95.8 24269.1 1722.0 105.2 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

95.8 24269.1 1722.0 1052 2.3 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 626.9 0.0 0.0 0.0 0.0 0.0

89.4 22646.8 1606.9 98.2 2.2 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0 0.0 o.o 0.0 0.0

4752.2 162024 -22.0 60.7 0.00 -133.8 34.09

928.3 17348 •31.3 40.7 1.00 -19.4 18.69

3823.9 144676 •31.3 40.7 0.00 •114.4 37.83

2195.0 58296 •42.2 60.2 0.00 -56.4 26.56

516.5 9163 -54.8 40.7 1.00 -10.7 17.74

1678.4 49133 -54.8 40.7 0.00 -45.8 29.27

1444.8 25511 •39.5 40.7 1.00 •30.0 18.35

26823.1 476258 •63.9 40.5 1.00 -563.3 17.76

26822.9 476258 -53.5 40.1 1.00 -559.0 17.76 .

0.0 0 21.9 39.6 1.00 0.0 17.76

26822.9 476258 -26.3 39.8 1.00 -550.2 17.76

26822.9 476258 21.9 39.6 1.00 •536.5 17.76

25029.9 444422 21.8 39.4 1.00 •500.7 17.76

77.2 0.82 0.012 0.029 18.98

47.7 0.66 0.011 0.025 18.69 17348 18.6

47.7 0.66 0.011 0.025 18.69

91.8 1.12 0.012 0.029 18.27

54.9 0.80 0.010 0.024 17.74 9163 10.4

54.9 0.80 0.010 0.024 17.74

49.6 0,69 0.010 0.025 18 32 26419 28.9

61.6 0.94 0.010 0.024 17.76 476258 537.5

52.8 0.76 0.010 0.024 17.76 476258 537.5

31.2 0.57 0.012 0.030 17.76

41.2 0.63 0.011 0.026 17.76 476258 537.5

3t.2 0.57 0.012 0.030 17.76 476258 537.5

31.1 0.57 0.012 0.030 17.76 444422 501.6

465.8 0.63 0.096 0.080 7.33 34.09 162024 347.8

523.0 0.59 0.129 0.087 9.66 37.83

523.0 0.59 0.129 0.087 9.66 37.83 144676 276.6

399.4 0.73 0.066 0.078 5.68 26.56 58296 145.9

472.4 0.65 0.095 0.086 8.07 29.27

472.4 0.65 0.095 0.086 8.07 29.27 49133 104.0

508.9 0.60 0.119 0.087 9.31 34.89 92 0.2

Simulation Basis: Train 3 - Salecled Oplion • 5% - C2 Mode Rev. 8A

Page 3 of 10

o.o o.o 0.0

o.o o.o o.o o.o o.o o.o 0.0 0.0 0.0 0.0



LOW CONDENSATE CASE • C2 RECOVERY MODE

StreamNumber Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2

78

79

80

81

89

90

91

92

93

94

95

96

103

89.4 22646.8 1606.9 98.2 2.2 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0

89.4 22646.8 1606.9 98.2 2.2 1.1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0

89.4 22646.8 1606.9 98.2 22 1-1 0.0 0.0 0.0 0.0 0.0 0.0 0.3 585.0 0.0

6.4 1622.3 115.1 7.0 0.2 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 41.9 0.0

2.5 1799.2 836.0 414.9 54.7 55.2 3.6 2.0 0.2 0.0 0.0 0.0 0.2 124.3 0.0

2.5 1799.2 836.0 414.9 54.7 55.2 3.6 2.0 0.2 0.0 0.0 0.0 0.2 124.3 0.0

0.1 367.2 1363.5 706.0 124.0 148.5 16.5 10.6 2.0 0.7 0.0 0.0 0.3 88.7 0.0

1.0 1219.0 729.2 748.2 277.9 463.5 116.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0

1.0 1219.0 729.2 748.2 277.9 463.5 118.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0

1.0 1219.0 729.2 748.2 277.9 463.5 118.7 94.2 47.8 31.2 1.5 0.0 0.2 90.6 0.0

0.8 804.6 371.6 264.8 66.6 90.7 12.8 8.6 1.8 0.6 0.0 0.0 0.1 55.3 0.0

0.8 804.6 371.6 264.8 66.6 90.7 12.8 8.6 1.8 0.6 0.0 0.0 0.1 55.3 0.0

0.1 303.4 1051.3 812.1 149.8 181.4 20.1 12.9 2.4 0.8 0.0 0.0 0.2 53.1 0.0

0.0

0.0

0.0

0.0

0.1

0.1

0.1

0.2

0.2

0.2

0.1

0.1

O.t

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.0 0.0 0.0

0.1 0.0 0.0

0.2 0.5 -0.0

0.2 0.5 0.0

0.2 O.S 0.0

o.o 0.0 0.0

o.o 0.0 0.0

o.i 0.0 0.0

25029.9 444422 52.9 39.0 1.00 -492.8 17.76

25029.9 444422 63.0 43.4 1.00 -490.6 17.76

25029.9 444422 53.8 42.8 1.00 -492.9 17.76

1793.0 31836 21.8 39.4 1.00 -35.9 17.76

3292.9 84658 -60.2 40.6 0.00 -85.9 25.71

3292.9 84658 -73.8 25.6 0.20 -85.9 25.71

2826.2 99984 -19.2 29.6 0.00 -80.6 35.35

3823.9 144676 -38.8 26.5 0.14 -114.4 37.83

3823.9 144676 3.4 25.8 0.37 -109.3 37.83

3823.9 144676 2.9 25.1 0.38 -109.3 37.83

1678.4 49133 -66.7 25.8 0.19 -4S.8 29.27

1678.4 49133 -28.2 25.1 0.52 -43.7 29.27

2587.8 96570 -10.9 24.8 0.00 -73.9 37.32

27.0 0.57 0.013 0.034 17.76 444422 501.6

29.0 0.58 0.013 0.035 17.76 444422 501.6

29.6 0.57 0.013 0.034 17.76 444422 501.6

31.1 0.57 0.012 0.030 17.76 31836 35.9

--

34.2 0.68 0.009 0.020 17.38 11269 13.0

--

30.0 0.57 0.010 0.022 18.78 10362 11.1

30.4 0.52 0.011 0.024 23.47 33494 28.6

29.6 0.52 0.011 0.024 23.50 33997 29.0

32.6 0.65 0.009 0.020 17.51 5441 6.2

30.0 0.55 0.010 0.022 20.73 18140 17.5

33.2 0.53 0.010 0.022 24.21 1 0.0

~ ~ --

433.4 0.71 0.073 0.084 6.79 25.71 84658 195.3

492.3 0.64 0.106 0.093 9.35 27.75 73389 149.1

494.4 0.63 0.101 0.089 7.97 35.35 99964 202.2

561.4 0.57 0.166 0.093 11.84 41.05 134314 239.3

538.8 0.59 0.135 0.082 9.36 46.39 111182 206.3

540.6 0.59 0.137 0.083 9.47 46.56 110679 204.7

526.3 0.60 0.135 0.094 10.76 31.94 43692 83.0

531.1 0.S9 0.132 0.092 10.20 38.58 30992 58.4

495.8 0.63 0.104 0.086 7.83 37.32 96570 194.8

M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature CC) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heal Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume How (m3*) Water Phase Mass Flow (kg/h)

Simulation Baals: Train 3 - Selected Option + 5% - C2 Mode Rev. 8A

~ — — -

---

— -

PagB4oM0

FIUOR


Contract AOWT Rev.2


Stream Numbar Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 HSS C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/Vg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg/h) Std Gas Row (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heal Capacity (kcal/Kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weighl Mass Flow (kg/h) Actual Volume Row (m3/h) Water Phase Mass Flow (kg/h) 0

104

109

110

111

112

113

115

116

117

118

119

120

121

0.1 303.4 1051.3 812.1 149.8 181.4 20.1 12.9 2.4 0.8 0.0 0.0 0.2 53.1 0.0 0.1 0.1 0.0 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 0.5 0.0

1.1 1561.8 987.1 132.3 9.0 7.4 0.3 0.2 0.0 0.0 0.0 0.0 0.2 138.5 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 02 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

42 3798,0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

1.7 1552.3 339.6 43.3 2.6 2.0 0.1 0.0 0.0 0.0 0.0 0.0 0.1

93.7 0.0 0.0 0.0 0.0 0.0

0.4 374.3 81.9 10.4 0.6 0.5 0.0 0.0 0.0 0.0 0.0 0.0 0.0 22.6 0.0 0.0 0.0 0.0 0.0

1.7 1552.3 339.6 43.3 2.6 2.0 0.1 0.0 0.0 0.0 0.0 0.0 0.1 93.7 0.0 0.0 0.0 0.0 0.0

2.1 1871.4 409.5 52.2 3.1 2.4 0.1 0.0 0.0 0.0 0.0 0.0 0.1 113.0 0.0 0.0 0.0 0.0 0.0

2.1 1871.4 40S.5 52.2 3.1 2.4 0.1 0.0 0.0 0.0 0.0 0.0 0.1 113.0 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

2587.8 96570 8.3 24.8 0.16 -71.9 37.32

3815.1 176993 50.0 24.9 0.00 -115.1 46.39

2838.0 67697 -18.0 24.7 1.00 -66.9 23.85

4980.1 101475 -41.7 24,3 1.00 -113.6 20.38

4980.1 101475 •27.0 23.9 1.00 -112.8 • 20.38

4980.1 101475 22.0 23.6 1.00 -110.2 20.38

4980.1 101475 88.8 52.5 1.00 -107.2 20.38

2035.5 41475 88.8 52.5 1.00 -438 20.38

490.8 10000 88.8 52.5 1.00 -10.6 20.38

2035.5 41475 5.4 51.9 1.00 •45.8 20.38

2453.9 50000 88.8 52.5 1.00 -52.8 20.38

2453.9 50000 55.0 51.9 1.00 -53.8 20.38

4980.1 101475 37.5 51.9 1.00 -110.2 20.38

33.8 0.54 0.010 0.021 23.85 67697 56.9

30.7 0.56 0.010 0.021 20.34 101062 99.6

27.4 0.53 0.010 0.022 20.38 101475

21.0 0.51 0.012 0.027 20.38 101475

37.8 0.57 0.014 0.037 20.38 101475 99.8

37.8 0.57 0.014 0.037 20.38 41475 40.8

37.8 0.57 0.014 0.037 20.38 10000 9.8

55.9 0.62 0.012 0.028 20.38 41475 40.8

37.8 0.57 0.014 0.037 20.38 50000 49.2

42.7 0.57 0.013 0.033 20.38 50000 49.2

46.4 0.58 0.013 0.031 20.38 101475 99.8

36.9 0.54 0.011 0.022 28.05 11956 8.5 480.7 0.65 0.094 0.078 6.31 39.14 84614 176.0

Simulallon Basis: Train 3 - Solaclsd OpUon + 3% • C2 Mode Rev. 8A

467.8 0.68 0.085 0.065 4.73 46.39 176993 378.4

516.2 0.61 0.117 0.096 9.84 33.96 413 0.8

Pags 5 of 10




Stream Number Composition (kgmole/h) Nilrogen Methane Ethane Propane i-Butane n-Butane l-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 HZS C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Tolal Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/Vg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Row (kg*) Sld Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

122

123

124

125

126

127

128

129

130

131

132

141

142

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 .0.2 0.1 0.0 00 0.0 0.0 0.2 229.4 0.0 0.0 00 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

4.2 3798.0 831.0 105.9 6.3 4.8 0.2 0.1 0.0 0.0 0.0 0.0 0.2 229.4 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 O.S 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 0.5 0.0

0.0 24.9 1105.9 1322.0 392.9 604.6 134.9 104.6 49.7 31.9 1.5 0.0 0.2 40.8 0.0 0.3 0.3 0.5 0.0

0.0 25.6 1136.4 1358.5 403.6 619.5 82.4 48.1 8.2 2.7 0.0 0.0 0.3 41.9 0.0 0.3 0.3 0.1 0.0

0.0 25.6 1136.4 1358.5 403.6 619.5 82.4 48.1 8.2 2.7 0.0 0.0 0.3 41.9 0.0

4980.1 101475 37.3 51.5 1.00 -110.2 20.38

4980.1 101475 -22.5 51.2 1.00 -114.0 20.38

4980.1 101475 •41.5 51.0 0.85 •116.5 20.38

4980.1 101475 -41.7 50.7 0.85 -116.5 20.38

4980.1 101475 -60.4 50.5 0.28 -120.8 20.38

4980.1 101475 -68.3 40.5 0.38 -120.8 . 20.38

0.0 0 •41.5 51.0 0.85 0.0 20.38

0.0 0 -41.5 51.0 0.85 0.0 20.38

3815.1 176993 45.5 22.0 0.06 -115.1 46.39

3815.1 176993 47.5 20.8 0.16 -113.8 46.39

3815.1 176993 52.8 20.5 0.30 -111.8 46.39

3727.7 166257 71.8 19.5 1.00 -96.7 44.60

3727.7 166257 29.5 26.0 0.00 -111.9 44.60

46.0 0.58 0.013 0.031 20.38 101475 99.8

69.8 0.76 0.012 0.027 20.38 101475 99.8

80.0 0.98 0.011 0.027 19.48 82197 84.5

79.3 0.97 0.011 0.027 19.48 82105 84.5

89.7 1.45 0.011 0.027 17.96 24594 27.5

64.9 1.04 0.010 0.024 17.61 33429 38.0

80.0 0.98 0.011 0.027 19.48

80.0 0.98 0.011 0.027 19.48

40.0 0.56 O.011 0.021 37.29 8138 4.4

38.2 0.55 0.011 0.021 38.12 23519 12.4

38.2 0.56 0.011 0.021 39.36 44424 22.6

39.5 0.57 0.011 0.022 44.60 166253 74.7

388.8 0.60 0.055 0.082 5.56 25.31 19278 49.6

390.2 0.80 0.055 0.082 5.59 25.34 19371 49.7

334.6 1.01 0.041 0.075 4.12 21.29 76881 229.8

384.6 0.64 0.052 0.079 5.17 22.06 68046 176.9

388.8 0.80 0.055 0.082 5.56 25.31

388.8 0.80 0.055 0.082 5.56 25.31

480.1 0.67 0.090 0.067 5.24 46.95 16B8S5 351.7

484.0 0.66 0,093 0.067 5.40 47.99 153474 317.1

484.0 0.66 0.094 0.066 5.35 49.35 132569 273.9

478.3 0.66 0.093 0.062 4.68 53.48 4 0.0

Simulation Basia: Train 3 - Selected Option + 5*. - C2 Mo
Page 6 of 10

o.o 0.0 0.0 0.0 0.0

o.o 0.0 0.0

o.o 0.0 0.0 0.0 0.0 0.0

o.o o.o 0.0

o.o 0.0

o.o 0.0 0.0 0.0

0.3 0.3 0.1 0.0

492.3 0.64 0.097 0.070 5.84 44.60 166257 337.7

FLUOR Conlract AOWT Rev.2



Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Tamperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h) Water Phase Mass Flow (kg/h)

150

151

152

153

501

502

503

504

505

507

600

601

602

0.0 24.9 1105.9 1322.0 3927 602.9 80.2 46.8 8.0 2.6 0.0 0.0 0.2 40.8 0.0 0.3 0.3 0.1 0.0

0.0 0.0 0.0 0.0 0.1 1.7 54.7 57.8 41.7 29.2 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.4 0.0

0.0 0.0 0.0 0.0 0.1 1.7 54.7 57.8 41.7 29.2 1.5 0.0

0.4 0.0

0.0 0.0 0.0 0.0 0.1 1.7 54.7 57.8 41.7 29.2 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.4 0.0

14.7 3540.0 322.0 104.9 18.2 22.1 2.5 1.6 0.3 0.1 0.0 0.0 0.1 88.3 0.0 0.0 0.0 0.0 0.0

14.7 3540.0 322.0 104.9 18.2 22.1 2.5 1.6 0.3 0.1 0.0 0.0 0.1 88.3 0.0 0.0 0.0 0.0 0.0

2.5 1799.2 836.0 414.9 54.7 55.2 3.6 2.0 0.2 0.0 0.0 0.0 0.2 124.3 0.0 0.1 0.0 0.0 0.0

2.2 1201.8 131.3 13.0 0.5 0.3 0.0 0.0 0.0 0.0 0.0 0.0 0.0 42.7 0.0 0.0 0.0 0.0 0.0

0.3 597.4 704.7 401.9 54.2 54.9 3.6 2.0 0.2 0.0 0.0 0.0 0.1 81.6 0.0 0.0 0.0 0.0 0.0

0.3 597.4 704.7 401.9 54.2 54.9 3.6 2.0 0.2 0.0 0.0 0.0 0.1 81.6 0.0 0.0 0.0 0.0 0.0

1.0 1401.6 1076.1 666.6 120.7 145.6 16.3 10.5 2.0 0.7 0.0 0.0 0.2 136.8 0.0 0.1 0.1 0.0 0.0

43.9 11119.8 1294.4 653.2 180.9 277.3 61.8 47.9 22.8 14.6 0.7 0.0 0.3 305.6 0.0 0.1 0.1 0.2 0.0

2.0 2596.2 699.7 92.9 5.8 4.5 0.2 0.1 0.0 0.0 0.0 0.0 0.1 186.6 0.0 0.0 0.0 0.0 0.0

3627.7 161797 29.5 26.0 0.00 •108.9 44.60

187.3 15196 177.4 19.8 0.00 •7.0 81.11

187.3 15193 49.9 19.1 0.00 -8.3 81.11

187.3 15193 49.9 18.9 0.00 •8.3 81.11

4115.0 78088 -22.0 60.7 1.00 -86.1 18.98

4115.0 78088 -43.3 60.2 0.91 •88.0 18.98

3292.9 84658 -58.2 25.3 0.42 -84.0 25.71

1392.0 25798 -58.2 25.3 1.00 -29.9 18.53

1900.8 58860 -58.2 25.3 0.00 -54.1 30.97

1900.8 58860 -59.1 24.3 0.01 •54.1 30.97

3578.3 107964 -46.0 24.3 0.28 -97.7 30.17

14023.5 299000 -17.3 60.9 0.87 -307.6 21.32

3588.1 75677 •35.9 24.3 1.00 •83.8 21.09

77.1 0.82 0.012 0.029 18.98 78076 82.5

92.9 1.15 0.012 0.030 18.23 67945 74.7

32.1 0.61 0.009 0.021 18.53 25798 27.9

32.1 0.61 0.009 0.021 18.53 25798 27.9

32.1 0.61 0.009 0.021 18.53

30.8 0.60 0.009 0.020 18.53 491 0.5

30.1 0.57 0.009 0.021 19.58 19297 19.8

75.5 0.79 0.012 0.029 19.20 233775 244.0

31.0 0.55 0.010 0.021 21.09 75677 71.9

455.8 0.63 0.096 0.080 7.33 34.09 11 0.0

394.9 0.74 0.064 0.078 5.56 26.17 10143 25.7

509.1 0.62 0.115 0.097 10.12 30.97 58860 115.6

509.1 0.62 0.115 0.097 10.12 30.97

509.1 0.62 0.115 0.097 10.12 30.97 58860 115.6

512.6 0.62 0.117 0.098 10.33 31.14 58370 113.8

523.1 0.60 0.125 0.096 10.41 34.20 88666 169.5

470.6 0.63 0.098 0.080 7.40 35.28 65225 138.6

o.o o.o o.o o.o o.o

62.3 0.73 0.012 0.027 77.75 0 0.0

492.3 0.64 0.097 0.070 5.84 44.60 181797 328.6

Simulation Baaia: Train 3 • Selecteo Option * 5% - C2 Mono Rev. SA

447.3 0.79 0.076 0.041 2.33 81.11 15196 34.0

626.4 0.57 0.212 0.086 13.83 81.11 15193 24.3

626.4 0.57 0.212 0.086 13.83 81.11 15193 24.3

Page 7 of 10




Stream Number Compoaition (kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass How (kgm)

804

605

606

607

0.1 367.2 1363.5 706.0 124.0 1485 16.5 10.6 2.0 0.7 0.0 0.0 0.3 68.7 0.0 0.1 0.1 0.0 0.0

0.0 25.6 1136.4 1358.5 403.6 619.5 82.4 48.1 8.2 2.7 0.0 0.0 0.3 41.9 0.0 0.3 0.3 0.1 0.0

0.0 25.6 1136.4 1358.5 403.6 619.5 82.4 48.1 8.2 2.7 0.0 0.0 0.3 41.8 0.0 0.3 0.3 0.1 0.0

0.0 24.9 1105.9 1322.0 392.7 602.9 80.2 46.8 8.0 2.6 0.0 0.0 0.2 40.8 0.0 0.3 0.3 0.1 0.0

2828.2 99984 -19.2 28.0 0.00 -80.8 35.35

3727.7 166257 50.5 19.2 0.44 -105.2 44.60

3727.7 166257 26.9 19.0 0.00 -112.0 44.60

3627.7 161797 20.0 25.5 0.00 -109.9 44.60

36.5 0.55 0.011 0.021 39.95 65411 32.8 494.4 0.63 0.101 0.089 7.97 35.35 99984 202.2

Simulallw Basis: Train 3 - Salaclar) OpUon » 5% - C2 Modo Rav. 8A

479.5 0.67 0.092 0.067 5.31 48.24 100846 210.3

491.3 0.65 0.098 0.071 5.91 44.60 166257 338.4

508.7 0.63 0.108 0.075 6.87 44.60 161797 318.1

Pags8 of 10


GASCO Elhana Recovery Maximization

LOW CONDENSATE CASE - C2 RECOVERY MODE - REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Ethane Propane i-Butane Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/mS) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Row (m3/h)

203

204

205

206

207

208

210

701

202

220

201

213

200 151.9 7367.4 76.0

151.9 7367.4 76.0

151.9 7367.4 76.0

23.0 2688.2 43.2

23.0 2668.2 43.2

23.0 2688.3 43.1

23.0 2688.3 43.1

8.1 4182.8 190.3

8.1 4182.8 190.3

128.9 4679.2 32.7

128.9 4679.2 32.7

151.9 7367.6 75.8

90.5 4387.3 45.2

7595.3 333863 57.4 21.0 0.00 •210.3 43.96

7595.3 333863 49.9 20.3 0.00 -212.1 43.96

7595.3 333863 20.5 8.8 0.24 •212.1 43.96

2754.4 121745 21.1 8.8 0.00 •79.6 44.20

2754.4 121745 -9.2 3.6 0.20 -79.6 44.20

2754.4 121744 -8.3 3.6 I. 00 -70.6 44.20

2754.4 121744 -8.5 3.5 1.00 -70.6 44.20

4381.2 195752 -8.3 3.6 0.00' -131.3 44.68

4381.2 195752 -7.7 3.6 0.50 -122.3 44.68

4840.8 212116 21.1 8.8 1.00 -121.6 43.82

4840.8 212118 20.5 8.5 1.00 -121.8 43.82

7595.3 333861 71.5 21.7 1.00 -186.6 43.96

4522.9 198814 54.5 19.8 0.00 -125.6 43.96

18.6 0.48 0.009 0.016 43.59 80960 37.2

18.7 0.48 0.009 0.016 43.82

7.8 0.41 0.O07 0.013 43.88 24629 11.3

7.8 0.41 0.007 0.013 44.20 121744 55.2

7.6 0.40 0.007 0.013 44.20 121744 55.2

7.8 0.41 0.007 0.013 44.20

7.8 0.41 0.007 0.013 44.38 97222 43.9

18.7 0.48 0.009 0.016 43.82 212118 97.0

18.1 0.47 0.008 0.016 43.82 212118 97.0

45.3 0.61 0.011 0.022

44.4 0.63 0.010 0.020

43.96

43.56

499.l" 0.64 0.104 0.083 7.38 44.08 252903 506.7

498.9 0.64 0.104 0.083 7.35 44.20 121745 244.0

541.9 0.59 0.141 0.098 11.13 44.28 97116 179.2

542.6 0.59 0.142 0.098 II. 10 44.68

543.2 0.59 0.143 0.097 11.09 44.98 98530 181.4

498.9 0.64 0.104 0.083 7.35 44.20

47.7 0.66 0.010 0.021 43.58

432.3 0.77 0.072 0.065 3.28 43.96 333863 772.3

Simulation Baaia: Train 3 - Selecled Option • 5% • C2 Moda Rev. flA

449.6 0.72 0.078 0.069 4.05 43.96 333863 742.6

Page 9 o l 10

542.6 0.59 0.142 0.098 11.10 44.68 195752 360.8

333861 152.2 438.4 0.75 0.074 0.066 3.57 43-96 198814 453.5

FLUOR Conlracl AOWT Rev.2


LOW CONDENSATE CASE - C2 RECOVERY MODE • REFRIGERATION SYSTEMS

Slream Number Composition (kgmole/h) Elhane Propane i-Butane Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weighl Vapor Phase Density (kg/m3) Heat Capaciiy (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kca!/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weighl Mass Flow (kg*) Actual Volume Flow (m3/h)

709

711

712

716

718

722

723

724

727

732

708

43.1 2090.6 21 6

5.4 263.9 2.7

5.4 263.9 2.7

37.7 1826.7 18.8

37.7 1826.7 18.8

70.4 3412.4 35.2

20.1 974.8 10.0

15.1 731.1 7.5

15.1 731.1 7.5

15.1 731.1 7.5

20.1 974.8 10.0

90.5 4387.3 45.2

2155.3 94738 18.1 19.2 0.00 -62.2 43,96

272.0 11957 14.5 7.6 0.03 -7.9 43.96

272.0 11957 16.0 7.6 1.00 •6.9 43.96

1883.282781 14.5 7.6 0.03 -54.4 43.96

18832 B2761 16.0 7.6 l.OO -47.6 43.96

3518.0 154638 15.5 7.4 1.00 •86.9 43.96

1005.0 44176 18.1 19.2 0.00 -29.0 43.96

753.7 33132 -21.3 18.7 0.00 -22.5 43.96

753.7 33132 -25.0 2.2 0.03 -22.5 43.96

753.7 33132 -23.5 2.1 1.00 -19.4 43.96

1005.0 44176 -24.1 2.0 1.00 -25.9 43.96

4522.9 198814 75.2 20.3 1.00 -110.4 43.96

16.1 0.46 0.008 0.015 43.28 332 0.2

16.2 0.46 O.OOB 0.015 43.96 11957 5.5

16.1 0.46 0.008 0.015 43.28 2299 1.1

16.2 0.46 0.008 0.015 43.96 62781 37.7

15.8 0.46 0.008 0.015 43.96 154638 70.5

4.8 0.38 0.007 0.012 42.87 833 0.4

4.8 0.38 0.007 0.011 43.96 33132 15.1

4.5 0.38 0.007 0.011 43.96 44176 20.1

40.1 0.58 0.011 0.022

706

505.8 0.63 0.107 0.085 7.62 43.96 94738 187.3

Simulallon Basis: Train 3 • SaKctad Option • 5% • C2 Moda Rev. SA

507.4 0.63 0.110 0.086 8.06 43.98 11625 22.9

470.6 0.63 0.105 0.086 8.06 44.35

507.4 0.63 0.110 0.086 8.06 43.98 80482 158.6

Page 10 of 10

505.8 0.63 0.107 O.OBS 7.62 43.96 44176 87.4

558.7 0.58 0.158 0.104 12.57 43.96 33132 59.3

560.3 0.58 0.163 0.106 13.07 43.99 32299 57.6

530.1 0.57 0.159 0.105 13.10 44.49

43.96

198814 90.6


Ethane Recovery Maximization (ERM) Project Material Balance Max. Condensate Case - C2 Recovery Mode Rev. 2


ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Material Balance Max. Condensate Case C2 Recovery Mode Revision 2

Rev.

Date

Description

13-Feb-04


4-Sep-03

Approved for Design

By

m OPM

Chk.

DTS

Disc.


2>

GS-L-FML046

ED


QASCO Ethane Recovery Maximization

MAX. CONDENSATE CASE - C2 RECOVERY MODE

Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane I-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S

C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Row (kgmole/h) Mass Flow (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weighl Mass Row (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Ftow (kg/h) Aclual Volume Row (m3/h) Water Phase Mass Fiow (kg/h)

1

10

11

20

22

23

24

0.0

43.6 10186.2 1248.9 657.8 182.5 279.1 57.7 44.3 19.4 11.1 0.5 0.0 0.2 245.0 0.0 0.0 0.0 0,1 0,0

43.6 101882 1248.9 657.8 182.5 279.1 57.7 44.3 19.4 11.1 0.5 0.0 0.2 245.0 0.0 0.0 0.0 0.1 0.0

59.9 14013.8 1718.2 905.0 251.0 383.9 79.4 61.0 26.8 15.2 0.7 0.0 0.3 337.1 0.0 0.0 0.0 0.1 0.0

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

0.0 0.0 0.0 0.6 112.2

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 18.4 1.7 0.6 607.0 0.0 0.0 0.0 0.6 112.2

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 582.2 0.0 0.0 0.0 0.2 22.0

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 582.2 0.0 0.0 0.0 0.2 0.0

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

0.0 0.0 0.0 0.0 0.0 0.0 0.0 89.1

1.1 557.9 226.0 286.4 147.4 289.9 116.0 104.8 102.3 103.0 17.3 1.7 0.1 24.7 0.0 0.0 0.0 0.4 1.1

32920.0 758433 58.0 66.5 1.00 -696.3 23.04

32920.0 758433 45.5 65.8 0.98 -704.0 23.04

32920.0 758433 27.0 65.4 0.94 •716.3 23.04

30851.1 663518 27.0 65.3 1.00 -647.3 21.51

30829.1 663121 27.8 62.8 1.00 -645.1 21.51

1979.7 93308 27.0 65.3 0.00 -63.0 47.13

1979.7 93308 17.7 32.1 0.24 -63.0 47.13

89.1 1607 27.0 65.3 O.OO •6.1 18.02

1979.7 93308 49.4 31.4 0.36 •60.7 47.13

12976.5 279119 27.6 62.5 1.00 -271.5 21.51

12976.5 279119 -19.5 60.8 0.84 -283.8 21.51

17852.5 364000 27.6 62.5 1.00 -373.5 21.51

13900.8 299000 27.5 62.4 1.00 -290.9 21.51

66.2 0.53 0.014 0.034 23.04 758432 659.7

67.9 0.64 0.014 0.033 22.53 728403 647.8

70.5 0.67 0.014 0.032 21.51 663625 618.3

70 3 0.67 0.014 0.032 21.51 663518 618.3

66.7 0.65 0.013 0.032 21.51 663121 617.8

70.3 0.67 0.014 0.032 21.51

33.5 0.55 0.012 0.027 22.17 10320 9.3

70.3 0.67 0.014 0.032 21.51

36.3 0.54 0.013 0.028 26.92 19236 14.3

66.4 0.65 0.013 0.032 21.51 279119 260.0

76.3 0.81 0.012 0.029 19.08 207832 218.3

66.4 0.65 0.013 0.032 21.51 384000 357.8

66.3 0.65 0.013 0.032 21.51 299000 278.6

516.1 0.61 0.120 0072 7.55 53.68 29122 56.4

499.6 0.61 0.112 0.073 7.32 47.11 93202 186.5

499.9 0.61 0.113 0.073 7.32 47.13

499.9 0.61 0.113 0.073 7.32 47.13 93308 186.7

566.2 0.58 0.157 0.080 10.13 54.81 82984 146.6

499.9 0.61 0.113 0.073 7.32 47.13

541.8 0.61 0.130 0.073 6.25 58.55 74072 136.7

907

1606

104.6 24757.9 3193.1 1849.2 580.9 952.9 253.1 210.1 148.5 129.3 16.4 1.7 0.6

607.0

Simulation Basis'. Train 3 • Max Condensata . 5% - C2 Mode Rev. 8B

—

o.o 0.0 0.0 0.0 0.0 0.0 0.0 0.0

o.o o.o

1607

Paget otIO

462.4 0.64 0.094 0.080 7.22 34.25 71287 154 2



MAX. CONDENSATE CASE • C2 RECOVERY MODE

Slream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature ( X ) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular WeigM Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg*) Sld Gas Row (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg*) Actual Volume Row (m3*) Water Phase Mass Row (kg*)

25

26

28

29

30

31

32

33

34

36

37

38

43

46.7 10911.8 1337.9 704.7 195 5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

13.3 3102.0 380.3 200.3 55.6 85.0 17.6 13.5 5.9 3.4 0.1 0.0 0.1 74.6 0.0 0.0 0.0 0.0 0.0

13.3 3102.0 380.3 200.3 55.6 85.0 17.6 13.5 5.9 3.4 0.1 0.0 0.1 74.6 0.0 0.0 0.0 0.0 0.0

59.9 14013.8 1718.2 905.0 251.0 383.9 79.4 61.0 26.8 15.2 0.7 0.0 0.3 337.1 0.0 0.0 0.0 0.1 0.0

103.5 24200.0 2967.1 1562.8 433.5 663.0 137.2 105.3 46.2 26.3 1.2 0.0 0.6 582.2 0.0 0.0 0.0 0.2 0.0

99.8 22094.2 2106.8 715.6 124.7 151.6 16.2 10.4 1.8 0.5 0.0 0.0 0.4 482.1 0.0 0.0 0.0 0.0 0.0

67.2 14889.0 1419.7 482.2 84.0 102.1 10.9 7.0 1.2 0.4 0.0 0.0 0.3 324.9 0.0 0.0 0.0 0.0 0.0

67.2 14889.0 1419.7 4822 84.0 102.1 10.9 7.0 1.2 0.4 0.0 0.0 0.3 324.9 0.0 0.0 0.0 0.0 0.0

16.6 3681.8 351.1 119.2 20.8 25.3 2.7 1.7 0.3 0.1 0.0 0.0 0.1 80.3 0.0 0.0 0.0 0.0 0.0

16.6 3681.8 351.1 119.2 20.8 25.3 2.7 1.7 0.3 0.1 0.0 0.0 0.1 80.3 0.0 0.0 0.0 0.0 0.0

99.8 22094.2 2106.8 715.6 124.7 151.6 16.2 10.4 1.8 0.5 0.0 0.0 0.4 482.1 0.0 0.0 0.0 0.0 0.0

97.4 20857.3 1693.7 423.7 51.7 52.2 3.1 1.7 0.1 0.0 0.0 0.0 0.3 426.5 0.0 0.0 0.0 0.0 O.O

97.4 20657.3 1693.7 423.7 51.7 52.2 3.1 1.7 O.t 0.0 0.0 0.0 0.3 426.5 0.0 0.0 0.0 0.0 0.0

13900.8 299000 -5.7 61.3 0.90 -299.8 21 51

3951.7 85000 27.5 62.4 1.00 -82.7 21.51

3951.7 85000 -33.6 60.9 0.74 -87.8 21.51

17852.5 384000 -20.3 60.8 0.84 -390.8 21.51

30829.1 663121 -20.0 60.7 0.84 -674.6 21.51

25804.0 491577 -20.0 60.7 1.00 -534.5 1905

17388.9 331266 -20.0 60.7 1.00 -360.2 19.05

17388.9 331266 -39.5 60.2 0.92 -367.3 19.05

4300.0 81917 -20.0 60.7 1.00 -89.1 19.05

4300.0 81917 -41.7 60.2 0.90 -91.1 19.05

25804.0 491577 -40.2 60.2 0.91 -545.6 19.05

23607.8 432134 -40.2 60.2 1.00 -489.4 18.30

23607.8 432134 -57.5 40.6 0.94 -491.6 18.30

72.6 0.74 0.013 0.030 19.81 248867 251.8

66.3 0.65 0.013 0.032 21.51 85000 79.2

83.5 0.94 0.012 0.029 18.40 54086 58.9

76.6 0.81 0.012 0.029 19.03 283775 298.8

76.3 0.81 0.012 0.029 19.05 491550 517.1

76.4 0.81 0 012 0.029 19.05 491577 517.1

76.3 0.81 0.012 0.029 19.05 331213 348.4

88.8 1.05 0.012 0.029 18.33 293157 320.5

76.3 0.81 0.012 0.029 19.05 81904 86.2

90.9 1.11 0.012 0.029 18.24 70795 77.8

89.3 1.07 0.012 0.029 18.30 431890 472.9

89.6 1.07 0.012 0.029 18.30 432134 473.1

56.4 0.83 0.010 0.024 17.70 390756 442.5

442.4 0.66 0.085 0.080 6.77 30.55 30914 69.9

461.5 0.64 0.094 0.080 7.21 34.04 100225 217.2

462.2 0.64 0.094 0.080 7.22 34.14 171571 371.2

462.1 0.64 0.094 0.080 7.22 34.14 --

462.1 0.64 0.094 0.080 7.22 34.13 53 0.1

406.4 0.72 0.059 0.079 5.87 27.31 38109 93.8

462.1 0.64 0.094 0.080 7.22 34.13 13 0.0

398.1 0.73 0.066 0.078 5.66 26.56 11122 27.9

404.0 0.72 0.068 0.079 5.81 27.08 59687 147.7

403.6 0.72 0.068 0 079 5.80 27.07

447.8 0.68 0.082 0.085 7.29 27.11 41379 92.4

472.7 0.63 0.099 0.078 7.29 37.53 50133 106.1

Simulation Basis: Train 3 - Max Condansata + 5% - C2 Moda Rav. SB

— — -

Page 2 of 10

FLUOR Conlracl AOWT Rev. 2

QASCO Elhane Recovery Maximization


Slream Number Composition (Kgmole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan

E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperalure ( C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivily (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conduclivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h) 0

50

52

53

54

56

67

58

70

72

73

75

76

77

3.7 2105.8 860.3 847.3 308.8 511.4 121.0 94.9 44.4 25.8 1.2 0.0 0.2 100.1 0.0 0.0 0.0 0.2 0.0

2.6 843.8 81.2 22.0 3.2 3.6 0.3 0.2 0.0 0.0 0.0 0.0 0.0 19.7 0.0 0.0 0.0 0.0 0.0

1.2 1262.0 779.1 825.2 305.6 507 9 120.7 94.7 44.3 25.8 12 0.0 0.2 80.4 0.0 0.0 0.0 0.2 0.0

2.4 1236.9 413.1 291.8 73.0 99.4 13.0 8.7 1.7 0.5 0.0 0.0 0.1 55.5 0.0 0.0 0.0 0.0 0.0

1.6 460.7 30.5 5.2 0.5 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 8.9 0.0 0.0 0.0 0.0 0.0

0.8 776.2 382.5 286.6 72.5 99.0 13.0 8.7 1.7 0.5 0.0 0.0 0.1 46.6 0.0 0.0 0.0 0.0 0.0

4.2 1304.5 111.7 27.3 3.7 4.0 0.3 0.2 0.0

103.5 24158.6 1857.6 132.7 3.1 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.3 544.5 0.0 0.0 0.0 0.0 0.0

0.0 0.0

28.7 0.0 0.0 0.0 0.0 0.0

103.5 24158.5 1857.7 132.7 3.1 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.3 544.5 0.0 0.0 0.0 0.0 0.0

103.5 24158.6 1857.6 132.7 3.1 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.3 544.5 0.0 0.0 0.0 0.0 0.0

96.6 22542.4 1733.3 123.8 2.9 1.4 0.0 0.0 0.0 0.0 0.0 0.0 0.3 508.1

0.0 0.0 0.0 0.0 0.0

103.5 24158.6 1857.6 132.7 3.1 1.5 0.0 0.0 0.0 0.0 0.0 0.0 0.3 544.5 0.0 0.0 0.0 0.0 0.0

5025.1 171545 -20.0 60.7 0.00 -140.1 34.14

976.6 16321 -292 40.7 1.00 -20.2 18.76

4048.4 153224 -29.2 40.7 0.00 -119.9 37.85

2196.2 59442 -40.2 60.2 0.00 -562 27.07

508.0 9034 •52.5 40.7 1.00 -10.4 17.78

1688.3 50409 -52.5 40.7 0.00 -45.8 29.86

1484.6 27354 -36.9 40.7 1.00 •30.6 18.43

26802.0 476433 -61.8 40.5 1.00 -556.3 17.78

26801.9 476429 -51.9 40.1 1.00 -552.3 17.78

0.0 0 23.1 39.6 1.00 0.0 17.78

26B01.9 476429 -24.4 39.8 1.00 -543.4 17.78

26801.9 476429 23.1 39.6 1.00 -530.0 17.78

25008.9 444557 23.0 39.4 1.00 -494.5 17.78

76.4 0.81 0.012 0.029 19.05

47.3 0.66 0.011 0.025 18.76 18321 19.6

47.3 0.66 0.011 0.025 18.76

89.6 1.07 0.012 0.029 18.30

53.8 0.78 O.OtO 0.024 17.78 9034 10.2

53.8 0.78 0.010 0.024 17.78

48.9 0.68 0.010 0.025 18.39 27257 29.7

60.2 0.90 0.010 0.024 17.78 476433 537.1

52.1 0.76 0.010 0.024 17.78 476429 537.1

31.1 0.57 0.012 0.030 17.78

40.7 0.62 0.011 0.026 17.78 476429 537.1

31.1 0.57 0.012 0.030 17.78 476429 537.1

31.0 0.57 0.012 0.030 17.78 444557 501.2

462.1 0.64 0.094 0.080 7.22 34.14 171545 371.3

519.0 0.60 0.126 0.086 9.52 37.65

519.0 0.60 0.126 0.086 9.52 37.85 153224 295.2

403.8 0.72 0.068 0.079 5.80 27.07 59442 147.3

474.8 0.64 0.097 0 086 8.19 29.86

474.8 0.64 0.097 0.086 8.19 29.86 50409 106.2

507.7 0.61 0.119 0.087 9.27 35.28 97 0.2

Simulation Basis: Train 3 - Max Condansala 4 5% - C2 Mode Rev. BB

Page 3 of 10

o.o o.o o.o o.o

o.o o.o 0.0 0.0 0.0 0.0 0.0

o.o 0.0 0.0 0.0

o.o

0.0

0.0 0.0 0.0 0.0

FIUOR Contract AOWT Rev.2

QASCO Elhane Recovery Maximization


StreamNumber Composition (kgrnole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg*) Temperature (°C) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Fiow (MMSCFD) Hydrocarbon Uquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (CP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Row (kg*) Actual Volume Flow (m3*) Water Phase Mass Flow (kg*)

78

79

80

81

89

90

91

92

93

94

95

96

103

96.6 22542.4 1733.3 123.8 2.9 1.4 0.0 0.0 00 0.0 0.0 0.0 0.3 508.1 0.0 0.0 0.0 0.0 0.0

96.6 22542.4 1733.3 123.8 2.9 1.4 0.0 0.0 0.0 0.0 0.0 0.0 0.3 508.1 0.0 0.0 0.0 0.0 0.0

96.6 22542.4 1733.3 123.8 2.9 1.4 0.0 0.0 0.0 0.0 0.0 0.0 0.3 508.1 0.0 O.O 0.0 0.0 0.0

6.9 1616.2 124.3 8.9 02 0.1 0.0 0.0 0.0 0.0 0.0 0.0 0.0 36.4 0.0 0.0 0.0 0.0 0.0

2.4 1614.5 805.9 443.3 59.9 60.6 3.6 2.0 0.2 0.0 0.0 0.0 0.1 96.9 O.O 0.0 0.0 0.0 0.0

2.4 1614.5 805.9 443.3 59.9 60.6 3.6 2.0 0.2 0.0 0.0 0.0 0.1 96.9 0.0 0.0 0.0 0.0 0.0

0.1 362.0 1283.1 750.2 134.9 162.0 16.8 10.7 1.9 0.6 0.0 0.0 0.2 67.0 0.0 0.0 0.0 0.0 0.0

1.2 1262.0 779.1 825.2 305.6 507.9 120.7 94.7 44.3 25.8 1.2 0.0 0.2 80.4 0.0 0.0 0.0 0.2 0.0

1.2 1262.0 779.1 825.2 305.6 507.9 120.7 94.7 44.3 25.8 1.2 0.0 0.2 80.4 0.0 0.0 0.0 02 0.0

12 1262.0 779.1 825.2 305.6 507.9 120.7 94.7 44.3 25.8 1.2 0.0 0.2 80.4 0.0 0.0 0.0 0.2 0.0

0.8 776.2 382.5 286.6 72.5 99.0 13.0 8.7 1.7 0.5 0.0 0.0 0.1 46.6 0.0 0.0 0.0 0.0 0.0

0.6 776.2 382.5 286.6 72.5 99.0 13.0 8.7 1.7 0.5 0.0 0.0 0.1 46.6 0.0 0.0 0.0 0.0 0.0

0.1 304.8 980.0 846.9 160.1 194.3 20.1 12.9 2.2 0.6 0.0 0.0 0.2 43.3 0.0 0.0 0.0 0.0 00

25008.9 444557 53.2 39.0 1 00 -486.8 17.78

25008.9 444557 63.5 43.5 1.00 -484.6 17.78

250OB.9 444557 54.0 42.9 1.00 -487.0 17.78

1793.0 31872 23.0 39.4 1.00 -35.5 17.78

3089.5 81451 -58.0 40.6 0.00 -79.9 26.36

3089.5 81451 -71.3 25.6 0.19 -79.9 26.36

2789.4 99891 -17.7 29.6 0.00 -78.8 35.81

4048.4 153224 -36.6 26.5 0.14 -119.9 37.85

4048.4 153224 2.9 25.8 0.36 -114.8 37.85

4048.4 153224 2.3 25.1 0.36 -114.8 37.85

1688.3 50409 -64.0 25.8 0.18 -45.8 29.86

1688.3 50409 -26.2 25.1 0.50 -43.7 29.86

2565.6 96861 -10.0 24.8 0.00 -73.1 37.75

27.0 0.57 0.013 0.034 17.78 444557 501.2

29.1 0.58 0.013 0.035 17.78 444557 501.2

29.7 0.58 0.013 0.034 17.78 444557 501.2

31.0 0.57 0.012 0.030 17.78 31672 35.9

-

33.5 0.67 0.009 0.020 17.42 10448 12.0

--~ -

29.7 0.57 0.010 0.023 18.86 10907 11.6

30.3 0.53 0.011 0.024 23.33 33555 28.8

29.5 0.52 0.011 0.024 23.37 34096 29.2

32.1 0.64 0.009 0.021 17.57 5401 6.2

29.8 0.55 0.010 0.022 20.80 17416 16.8

438.6 0.70 0.077 0.08S 7.01 26.36 81451 185.7

496.0 0.64 0.110 0.094 9.60 28.52 71003 143.1

494.1 0.63 0.103 0.088 7.99 35.81 99891 202.2

556.9 0.57 0.162 0.093 11.65 41.01 142317 255.5

535.2 0.59 0.133 0.082 928 45.85 119669 223.6

537.1 0.59 0.135 0.083 9.39 46.01 119128 221.8

527.3 0.60 0.137 0.095 10.86 32.59 45008 85.4

528.4 0.59 0.131 0.091 10.05 38.78 32993 62.4

Simulation Basis: Tram 3 • Max Ccxittensate • 5% - C2 Moda Rev. 88

— — ---

— — — -

— — --

— — ~ -

—

—

—

—

Page 40(10

497.0 0.63 0.105 0.086 7.92 37.75 96861 194.9




Stream Number Compoaition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S

C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Row (rn3/h) Water Phase Mass Flow (kg/h)

117

118

119

120

121

1.9 1555.9 369.8 53.9 3.3 2.6 0.1 0.0 0.0 . 0.0 0.0 0.0 0.1 80.3 0.0 0.0 0.0 0.0 0.0

0.3 220.2 52.3 7.6 0.5 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0 11.4 0.0 0.0 0.0 0.0 0.0

1.9 1555.9 369.8 53.9 3.3 2.6 0.1 0.0 0.0 0.0 0.0 0.0 0.1 80.3 0.0 0.0 0.0 0.0 0.0

2.2 1835.0 436.1 63.5 3.9 3.0 0.1 0.0 0.0 0.0 0.0 0.0 0.1 94.7 0.0 0.0 0.0 0.0 0.0

2.2 1835.0 436.1 63.5 3.9 3.0 0.1 0.0 0.0 0.0 0.0 0.0 0.1 94.7 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4799.1 98396 88.2 52.5 1.00 -101.0 20.50

2067.8 42396 88.2 52.5 1.00 -43.5 20.50

292.6 6000 88.2 52.5 1.00 -6.2 20.50

2067.8 42396 7.1 51.9 1.00 -45.5 20.50

2438.7 50000 88.2 52.5 1.00 -51.3 20.50

2438.7 50000 55.0 51.9 1.00 -52.3 20.50

4799.1 98396 35.9 51.9 1.00 -104.0 20.50

38.2 0.57 0.014 0.037 20.50 98396 962

38.2 0.57 0.014 0.037 20.50 42396 41.4

38.2 0.57 0.014 0.037 20.50 6000 5.9

56.1 0.63 0.012 0.029 20.50 42396 41.4

38.2 0.57 0.014 0.037 20.50 50000 48.9

43.2 0.57 0.013 0.033 20.50 50000 48.9

47.3 0.58 0.013 0.031 20.50 98396 96.2

104

109

110

111

112

113

115

0.1 304.8 980.0 846.9 160.1 194.3 20.1 12.9 2.2 0.6 0.0 O.O 0.2 43.3 0.0 0.0 0.0 0.0 0.0

0.0 41.6 1109.5 1430.1 430.4 661.5 137.2 105.3 46.2 26.3 1.2 0.0 0.2 37.7 0.0 0.0 0.0 0.2 0.0

1.2 1582.8 953.0 145.5 10.2 8.4 0.3 0.2 0.0 0.0 0.0 0.0 02 109.7 0.0 0.0 0.0 0.0 0.0

4.3 3611.1 858.1 125.0 7.7 6.0 02 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

256S.6 96861 9.8 24.8 0.16 -71.1 37.75

4027.3 186692 50.0 24.9 0.00 -121.1 46.36

2811.5 66452 •16.8 24.7 1.00 -64.2 23.64

4799.0 98392 -37.9 24.3 1.00 -107.0 20.50

4799.1 98396 -23.0 23.9 1.00 -106.2 20.50

4799.1 98396 22.0 23.6 1.00 -103.9 20.50

33.2 0.54 0.010 0.021 23.64 66452 56.3

30.3 0.56 0.010 0.021 20.47 98039 96.0

27.0 0.53 0.010 0.022 20.50 98396 96.2

21.2 0.52 0.012 0.027 20.50 99396 962

36.5 0.54 0.011 0.022 27.99 11424 8.2 481.1 0.65 0.095 0.078 6.34 39.60 85437 177.6

Simulaiion Baals: Train 3 - Max Condansata • 5% - C2 Moda Rav. 8B

466.9 0.68 0.085 0.065 4.75 46.36 186692 399.9

514.3 0.61 0.118

0.095 9.79 34.65 353 0.7

P a g e S o l 10

116




Slream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmola/h) Mass Row (kg/h) Temperature ("C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Sld Gas Flow (MMSCFD) Hydrocarbon Uquld Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Water Phase Mass Flow (kg/h)

122

123

124

125

128

127

128

129

130

131

132

141

142

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 01 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

4.3 3611.2 858.2 125.1 7.7 6.0 0.2 0.1 0.0 0.0 0.0 0.0 0.2 186.3 0.0 0.0 0.0 0.0 0.0

0.0 0.0 0.0 0.0 0.0

o.o o.o o.o o.o o.o o.o o.o

0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0 0.0

0.0

o.o

o.o o.o 0.0 0.0

0.0 0.0 0.0 0.0 0.0 0.0

0.0 41.6 1109.5 1430.1 430.4 661.5 137.2 105.3 46.2 26.3 1.2 0.0 0.2 37.7 0.0 0.0 0.0 0.2 0.0

0.0 41.6 1109.5 1430.1 430.4 661.5 137.2 105.3 46.2 26.3 1.2 0.0 0.2 37.7 0.0 0.0 0.0 0.2 0.0

0.0 41.6 1109.5 1430.1 430.4 661.5 137.2 105.3 46.2 26.3 1.2 0.0 0.2 37.7 0.0 0.0 0.0 0.2 0.0

0.0 42.7 1136.3 1467.2 441.4 677.0 85.5 49.0 7.6 2.3 0.0 0.0 0.2 38.7 0.0 0.0 0.0 0.0 0.0

0.0 42.7 1138.3 1467.2 441.4 677.0 85.5 49.0 7.6 2.3 0.0 0.0 0.2 38.7 0.0 0.0 0.0 0.0 0.0

4799.1 98396 35.7 51.5 1.00 •104.0 20.50

4799.1 96396 -19.5 51.2 1.00 -107.4 20.50

4799.1 98396 -39.5 51.0 0.83 -110.0 20.50

4799.1 98396 -39.7 50.7 0.83 •110.0 20.50

4799.1 98396 -58.9 50.5 0.30 -114.1 20.50

4799.1 96396 -66.8 40.5 0.40 -114.1 20.50

0.0 0 -39.5 51.0 0.83 0.0 20.50

0.0 0 -39.5 51.0 0.83 0.0 20.50

4027.3 166692 45.7 22.0 0.06 -121.1 46.36

4027.3 186692 47.3 20.8 0.15 •119.9 46.36

4027.3 186692 52.5 20.5 0.28 -117.9 46.36

3949.9 176937 72.2 19.5 1.00 -102.4 44.80

3949.9 176937 29.6 26.0 0.00 -118.6 44.80

46.9 0.58 0.013 0.031 20.50 98396 96.2

69.1 0.75 0.012 0.027 20.50 98396 96.2

78.2 0.95 0.011 0.027 19.46 77545 79.9

77.6 0.94 0.011 0.027 19.45 77474 79.8

87.3 1.36 0.011 0.027 17.94 25563 28.6

63.6 1.00 0.010 0.024 17.61 33496 38.1

78.2 0.95 0.011 0.027 19.46

78.2 0.95 0.011 0.027 19.46

39.7 0.56 0.011 0.021 37.13 8322 4.5

38.0 0.55 0.011 0.021 37.99 22731 12.0

38.2 0.56 0.011 0.021 39.26 43487 22.2

39.7 0.58 0.011 0.022 44.80 176937 79.2

389.1 0.79 0.056 0.082 5.53 25.60 20851 53.8

390.4 0.79 0.057 0.082 5.57 25.63 20922 53.6

340.0 0.97 0.043 0.076 4.24 21.59 72833 214.2

388.0 0.82 0.055 0.080 5.31 22.40 64899 167.2

389.1 0.79 0.056 0,082 5.53 25.60

389.1 0.79 0.056 0.082 5.53 25.60

479.0 0.67 0.090 0.067 5.24 46.90 178370 372.4

482.5 0.66 0.092 0.067 5.38 47.82 163961 339.8

482.1 0.67 0.093 0.066 5.32 49.05 143205 297.1

Simulation Basis: Train 3 - Max Conoansats . 5% - CZ Modo Rev. BB

Page 6 otIO

0.0

o.o

493.1 0.64 0.098 0.071 5.95 44.80 176937 358.8

FLUOR Contraci AOWT Rev.2



Stream Number Composition (kgrnole/h) Nitrogen Methane Ethane Propane I-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Msrcaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/mS) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivily (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h) Waler Phase Mass Flow (kg/h)

150 0.0 41.6 1109.5 1430.1 430.2 659.8 83.4 47,8 7.4 2.2 0.0 0.0 0.2 37.7 0.0 0.0 0.0 0.0 0.0 3849.9 172458 29.6 26.0 0.00 -115.6 44.80

493.1 0.64 0.098 0.071 5.95 44.80 172458 349.7

SlmulaUon Basis: Train 3 • Max condansata + 5% - C2 Mode Rev. 88

151 0.0 0.0 0.0

o.o 0.1 1.6 53.8 57.5 38.8 24.1 1.2 0.0 0.0 0.0 0.0 0.0

o.o 0.1 0.0 177.4 14234 175.7 19.8 0.00 -6.6 80.26

446.0 0.79 0.075 0.041 2.30 80.26 14234 31.9

601

602

1.0 1293.5 1049.8 713.7 131.8 159.1 16.6 10.7 1.9 0.6 0.0 0.0 0.2 107.8 O.O 0.0 0.0 0.0 0.0

46.7 10911.8 1337.9 704.7 195.5 298.9 61.9 47.5 20.8 11.9 0.5 0.0 0.3 262.5 0.0 0.0 0.0 0.1 0.0

2.2 2514.4 719.7 109.0 7.1 5.6 0.2 0.1 0.0 0.0 0.0 0.0 0.1 150.5 0.0 0.0 0.0 0.0 0.0

1799.3 57287 •54.6 24.3 0.01 •50.6 31.84

3486.6 107666 -42.0 24.3 0.27 -94.3 30.88

13900.8 299000 -16.2 60.9 0.86 -303.0 21.51

3508.8 74228 -32.7 24.3 1.00 -79.6 21.15

31.5 0.60 0.009 0.021 18.73

30.2 0.59 0.009 0.021 18.73 454 0.5

29.7 0.56 0.010 0.021 19.76 18284 18.5

75.3 0.79 0.012 0.029 19.24 229110 238.6

30.6 0.55 0.010 0.021 21.15 74228 70.3

509.4 0.62 0.116 0.097 10.10 31.84 57287 112.5

512.9 0.61 0.119 0.096 10.31 32.02 56833 110.8

521.3 0.60 0.125 0.096 10.27 34.90 89382 171.5

465.3 0.63 0.096 0.079 7.26 35.03 69890 150.2

153

501

502

503

504

505

507

0.0 0.0 0.0 0.0 0.1 1.6 53.8 57.6 38.8 24.1 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.1 0.0

0.0 0.0 0.0 0.0 0.1 1.6 53.6 57.6 38.8 24.1 1.2 0.0 0.0 0.0 0.0 0.0 0.0 0.1 0.0

15.9 3523.4 336.0 114.1 19.9 24.2 2.6 1.7 0.3 0.1 0.0 0.0 0.1

15.9 3523.4 336.0 114.1 19.9 24.2 2.6 1.7 0.3 0.1 0.0 0.0 0.1 76.9 0.0 0.0 0.0

2.4 1614.5 805.9 443.3 59.9 60.6 3.6 2.0 0.2 0.0 0.0 0.0 0.1 96.9 0.0 0.0 0.0 0.0 0.0

2.1 1096.7 138.4 16.1 0.7 0.4 0.0 0.0 0.0 0.0 0.0 0.0 0.0

35.7 0.0 0.0 0.0 0.0 0.0

0.2 517.7 667.5 427.2 59.3 60.2 3.6 2.0 0.2 0.0 0.0 0.0 0.1 61.2 0.0 0.0 0.0 0.0 0.0

0.2 517.7 667.5 427.2 59.3 60.2 3.6 2.0 0.2 0.0 0.0 0.0 0.1 61.2 0.0 0-0 0.0 0.0 0.0

177.4 14237 49.1 19.1 0.00 -7.8 80.26

177.4 14237 49.1 18.9 0.00 -7.8 80.26

4115.0 78392 -20.0 60.7 1.00 •85.2 19.05

4115.0 78392 •41.5 60.2 0.90 -87.1 19.05

3089.5 81451 •53.8 25.3 0.42 -78.0 26.36

1290.2 24164 •53.8 25.3 1.00 •27.4 18.73

1799.3 57287 -53.8 25.3 0.00 •50.6 31.84

76.3 0.81 0.012 0.029 1905 783B0 82.5

90.7 1.10 0.012 0.029 18.25 67954 74.6

31.5 0.60 0.009 0.021 18.73 24164 25.9

31.5 0.60 0.009 0.021 18.73 24164 25.9

462.1 0.64 0.094 0.080 7.22 34,13 12 O.O

399.0 0.73 0.066 0.078 5.68 26.64 10438 26.2

509.4 0.62 0.116 0.097 10.10 31.84 57287 112.5

509.4 0.62 0.116 0.097 10.10 31.84

152

624.3 0.57 0.210 0.086 13.75 80.26 14237 22.8

624.3 0.57 0.210 0.086 13.75 80.26 14237 22.8

76.9 0.0 0.0 0.0 0.0 0.0

Page 7 ol 10

o.o 0.0

600




Stream Number Composition (kgmole/h) Nitrogen Methane Ethane Propane i-Butane n-Butane i-Pentane n-Pentane n-Hexane NBP91 NBP138 NBP182 H2S C02 CS2 M-Mercaptan E-Mercaptan nPMercaptan H20 Total Stream Molar Flow (kgmola/h) Mass Flow (kg*) Temperature CC) Pressure (bara) Vapour Fraction Heat Row (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Uquld Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surtace Tension (dyne/cm) Molecular Weight Mass Row (kg/h) Actual Volume Flow (m3/h) Waler Phase

604

607

605

0.1 362.0 1283.1 750.2 134.9 162.0 16.8 10.7 1.9 0.6 0.0 0.0 0.2 67.0 0.0 0.0 0.0 0.0 0.0

0.0 42.7 1138.3 1467.2 441.4 677.0 65.5 49.0 7.6 2.3 0.0 0.0 0.2 38.7 0.0 0.0 0.0 0.0 0.0

0.0 42.7 1138.3 14672 441.4 677.0 85.5 49.0 7.6 2.3 0.0 0.0 0.2 38.7 0.0 0.0 0.0 0.0 0.0

0.0 41.6 1109.5 1430.1 430.2 659.B 83.4 47.8 7.4 2.2 0.0 0.0 0.2 37.7 0.0 0.0 0.0 0.0 0.0

2789.4 99891 -17.7 28.0 0.00 -78.8 35.81

3949.9 176937 50.5 19.2 0.41 •111.8 44.80

3949.9 176937 28.9 19.0 0.00 -118.7 44.80

3849.9 172458 20.0 25.5 0.00 -116.6 44.80

492.0 0.65 0.098 0.071 6.02 44.80 176937 359.6

509.3 0.62 0.109 0.076 6.98 44.80 172458 338.6

36.5 0.55 • 0.011 0.021 39.89 64502 32.4 494.1 0.63 0.103 0.088 7.99 35.81 99891 202.2

478.9 0.67 0.092 0.067 5.30 48.19 112438 234.B

Mass Flow (kg*)

Simulaiion Basis: Train 3 - Max Condensate • 5% - C2 Mode hev. 8

Pages ot 10


GASCO Ethana Racovety Maximization

MAX. CONDENSATE CASE - C2 RECOVERY MODE - REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Ethana Propane i-Butane Total Stream Molar Flow (kgmole/h) Mass Row (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosily (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas How (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Suriace Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h)

200

201

202

203

204

205

206

207

208

210

213

220

701

181.4 7826.1 80.7

181.4 7826.1 80.7

161.4 7826.1 80.7

22.3 2677.7 44.0

22.3 2677.7 44.0

22.4 2677.6 44.1

22.4 2677.6 44.1

7.8 4161.2 195.8

7.8 4161.2 195.8

139.1 5148.4 36.6

139.1 5148.4 36.6

161.4 7826.0 80.7

91.6 4444.7 45.8

8068.1 354647 57.4 21.0 0.00 -223.4 43.96

8068.1 354647 48.6 20.3 0.00 •225.7 43.96

8068.1 354647 19.6 8.6 0.24 -225.7 43.96

2744.0 121307 20.3 8.6 0.00 -79.4 44.21

2744.0 121307 •10.2 35 0.20 •79.4 44.21

2744.0 121308 -9.3 3.5 1.00 -70.4 44.21

2744.0 121308 •9.5 3.4 1.00 -70.4 44.21

4364.9 195115 -9.3 3.5 0.00 -131.0 44.70

4364.9 195115 •8.7 3.5 0.50 -122.0 44.70

5324.1 233340 20.3 8.6 1.00 -134.0 43.83

5324.1 233340 19.9 8.4 1.00 •134.0 43.83

8068.1 354648 71.5 21.7 1.00 -198.2 43.96

4582.0 201400 54.5 19.8 0.00 •127.3 43.96

18.2 0.47 0.008 0.016 43.58 84287 38.8

18.3 0.47 0.008 0.016 43.83

7.5 0.40 0.007 0.013 43.89 24527 11.2

7.6 0.40 0.007 0.013 44.21 121308 55.0

7.3 0.40 0.007 0.013 44.21 121308 55.0

7.6 0.40 0.007 0.013 44.21

7.6 0.40 0.007 0.013 44.39 96884 43.7

18.3 0.47 0.008 0.016 43.83 233340 106.7

17.9 0.47 0.008 0.016 43.83 233340 106.7

45.3 0.61 0.011 0.022 43.96 354648 161.7

44.4 0.63 0.010 0.020 43.56

500.4 0.64 0.105 0.064 7.49 44.08 270361 540.3

500.2 0.64 0.105 0.084 7.46 44.21 121307 242.5

543.2 0.59 0.142 0.099 11.26 44.29 96781 178.2

543.9 0.59 0.143 0.098 11.23 44.70

543.9 0.59 0.143 0.098 11.23 44.70 195115 358.7

544.6 0.59 0.145 0.097 11.22 45.01 98231 180.4

500.2 0.64 0.105 0.084 7.46 44.21

47.7 0.66 0.010 0.021 43.58

432.3 0.77 0.072 0.065 328 43.96 354647 820.4

Simutation Baals: Train 3 - Max ConOonsata + 5% • C2 Mode Rev. BB

452.2 0.72 0.079 0.069 4.18 43.96 354647 784.2

Page 9ot 10

438.4 0.75 0.074 0.066 3.57 43.96 201400 459.4

FLUOR Conlract AOWT Rsv. 2

GASCO Elhana Racovery Maximization

MAX. CONDENSATE CASE - C2 RECOVERY MODE - REFRIGERATION SYSTEMS

Stream Number Composition (kgmole/h) Ethane Propane I-Butane Total Stream Molar Flow (kgmole/h) Mass Flow (kg/h) Temperature (°C) Pressure (bara) Vapour Fraction Heat Flow (Gcal/h) Molecular Weight Vapor Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Molecular Weight Mass Flow (kg/h) Std Gas Flow (MMSCFD) Hydrocarbon Liquid Phase Density (kg/m3) Heat Capacity (kcal/kg-C) Viscosity (cP) Thermal Conductivity (Kcal/m-hr-C) Surface Tension (dyne/cm) Molecular Weight Mass Flow (kg/h) Actual Volume Flow (m3/h)

706

708

709

711

712

716

718

722

723

724

727

732

43.9 2129.6 22.0

5.8 281.1 2.9

5.8 281.1 2.9

38.1 1846.5 19.1

38.1 1848.5 19.1

71.5 3469.8 35.8

20.1 974.8 10.0

15.1 731.1 7.5

15.1 731.1 7.5

15.1 731.1

7.5

20.1 974.8 10.0

91.6 4444.7 45.8

2195.0 96510 18.1 19.2 0.00 •63.4 43.96

289.8 12740 14.5 7.6 0.03 -8.4 43.96

289.8 12740 16.0 7.6 1.00 -7.3 43.96

1906.0 83770 14.5 7.6 0.03 -55.0 43.96

1906.0 83770 16.0 7.6 1.00 •48.1 43.96

3577.0 157200 15.5 7.4 1.00 •90.4 43.96

1005.0 44180 18.1 19.2 0.00 -29.0 43.96

753.7 33130 -21.3 18.7 0.00 •22.5 43.96

753.7 33130 -25.0 22 0.03 -22.5 43.96

753.7 33130 -23.5 2.1 1.00 -19.4 43.96

1005.0 44180 -24.1 2.0 1.00 -25.9 43.96

4582.0 201400 75.1 20.3 1.00 -111.9 43.96

16.1 0.46 0.008 0.015 43.28 354 0.2

16.2 0.46 0.008 0.015 43.96 12740 5.8

16.1 0.46 0.008 0.015 43.28 2326 1.1

18.2 0.46 0.008 0.015 43.96 83770 38.2

15.8 0.46 0.008 0.015 43.96 157200 71.7

4.8 0.38 0.007 0.012 42.87 833 0.4

4.8 0.38 0.007 0.011 43.96 33130 15.1

4.5 0.38 0.007 0.011 43.96 44180 20.1

40.1 0.58 0.011 0.022 43.96 201400 91.8

505.8 0.63 0.107 0.085 7.62 43.96 96510 190.8

Simulation Basis: Train 3 • Max Condensale + 511.-02 Mode Rev. fl

507.4 0.63 0.110 0.086 8.06 43.98 12380 24.4

470.6 0.63

507.4 0.63 0.110 0.086 8.06 43.98 81440 160.5

0.105 0.086 8.06 44.35

Page 10 of 10

505.8 0.63 0.107 0.085 7.62 43.96 44180 87.4

558.7 0.58 0.158 0.104 12.57 43.96 33130 59.3

560.3 0.58 0.163 0.106 13.07 43.99 32300 57.6

530.1 0.57 0.159 0.105 13.10 44.49


7.0



UTILITY REQUIREMENTS The impact ofthe E R M Project on the existing utility systems is minor. Because the existing systems have sufficient capacity to support the incremental requirements, the utilities scope of work was limited to electrical modifications and tie-ins to the following systems: •

Instrument Air - required for new control valves and the refrigeration compressor motor pressurization system

•

Plant Air - required for the new utility stations

•

Nitrogen - required for the refrigeration compressor seal system and equipment purging

•

Low Pressure Steam - used for heat tracing only

Electrical power is supplied to the new Refrigeration Package (44ME-201), Propane Condenser (44E-203) and Cold Demethanizer Bottoms Pumps (44P-302 A/B).

CHAPTER 1

10



8.0


CHEMICALS AND CONSUMABLES The new chemical requirements associated with the E R M Project are summarized below. Propane for Refrigeration Package (44-ME-201) Type: 97% propane Initial Fill: Approx. 60 m Supply Method: Transfer from 45-V-502 3

Lube Oil for Propane Compressor, Gear, and Motor Type: Mineral Oil (ISO Grade 46) Initial Fill: Approx. 10 m Supply Method: Drums 3

Seal Fluid for Cold Demethanizer Bottoms Pumps (44-P-302 A/B) Type: Methanol Initial Fill: Approx. 0.02 m per seal pot (0.04 m total) Supply Method: Drums 3

CHAPTER 1

3

11




CHAPTER 2

PROCESS DESCRIPTION

CONTENTS

SECTION 1.0

2.0

GENERAL

2

1.1 1.2 1.3

2 2 2

4.0

Integration of the Unit in the Overall Plant References Principles of Operation and General Description

DETAILED PROCESS DESCRIPTION 2.1 2.2 2.3 2.4 2.5 2.6 2.7 2.8 2.9

3.0

PAGE

4

Preparation of the Feed Gas Gas Dehydration Recovery Tower and Expander-Recompressor Demethanizer and Recycle Compressor Debutanizer Existing Propane Refrigeration System E R M Refrigeration System Unit 44 Isolations Flare and Blowdown Valves

4 4 4 8 10 12 12 17 17

ELEMENTS OF PROCESS CONTROL PHILOSOPHY

18

3.1 3.2

18 19

Existing Controls Modified for E R M Operation New Controls Added for ERM Operation

DCS SCREEN DISPLAYS

CHAPTER 2

22



1.0

GENERAL

1.1

Integration of the Unit in the Overall Plant


The E R M Project does not impact the interfaces between Unit 44 and the rest of the OGD-I facilities.

1.2

References This section ofthe manual should be reviewed in conjunction with the following drawings: Process Flow Diagrams:

44-00-20-001 to 44-00-20-006A. Included in Chapter 1.

Material Balances:

44-00-20-010 to 44-00-20-013. Included in Chapter 1.

Piping & Instrument Diagrams: 44-00-30-018 to 44-00-30-041. Included in Chapter 10.

The new equipment items added in Unit 44 for the E R M Project are: Tag Number

Description

44-V-205

Propane Receiver

44-V-206

High Pressure KO Drum

44.V-207

Low Pressure KO Drum

44-V-308

Cold Demethanizer

44-C-202

Propane Compressor

44-E-203

Propane Condenser

44-E-318

2 Feed Chiller

44.E-406

Debutanizer Trim Condenser

44-E-407

N G L Subcooler

44-P-302 A/B

Cold Demethanizer Bottoms Pumps

nd

Refer to the Equipment List (NM-AOWT-44-00-06-001) in Chapter 9 for additional information.

1.3

Principles of Operation and General Description Principles of Operation The operational objective for Unit 44 after implementation of the E R M Project is unchanged from the original design. The unit will produce sweet, dry sales gas and recover N G L and condensate. The only difference is the quantity of ethane contained in the NGL.

CHAPTER 2




Addendum for the E R M Project - Rev. 1

In order to increase the ethane recovery, new equipment is added and operating conditions are adjusted. The required modifications are described in detail in Section 2.0 of Chapter 2. General Description The description of Unit 44 has been divided into the following sub-sections: Preparation of the Feed Gas Dehydration Recovery Tower and Expander-Recompressor Demethanizer and Recycle Compressor Debutanizer Propane Refrigeration Each of these sections is described below.

CHAPTER 2


2.0



DETAILED PROCESS DESCRIPTION This section describes the new ERM operating mode. The adequacy of the existing equipment for the new ERM conditions has been evaluated in detail during the engineering phase of the project. Refer to the following study reports for more information:

A

Subject

2.1

Document Number

Relief System

RPT-AOWT-44-06-006

Utility and Offsites Systems

RPT-AOWT-44-06-007

Recycle Gas Compressor

RPT-AOWT-44-06-008

Equipment, Instruments and Piping

RPT-AOWT-44-06-010

Cold Design Temperatures

RPT-AOWT-44-06-011

Preparation of the Feed Gas This section of the unit was not modified for the E R M Project. Refer to the existing Operating, Maintenance and Safety Manual for a detailed description of the following equipment items: 44-E-309: 44-E-310: 44-V-101: 44-F-101 A/B:

2.2

Wet Feed / Residue Gas Exchanger Wet Feed Chiller Gas Dehydration Separator Inlet Gas Filters

Gas Dehydration The existing gas dehydration system is not impacted by the E R M Project. The existing system produces a dry gas with water dewpoint of-100 C or lower. This is adequate for the new operating conditions. Refer to the existing Operating, Maintenance and Safety Manual for a detailed description of the following equipment items: o

44-V-102/3/4/5: 44-F-102 A/B: 44-F-103: 44-ME-101-HI: 44-E-101: 44-V-102:

2.3

Gas Dehydrators Outlet Gas Filters Regeneration Gas Filters Regeneration Gas Heater Regeneration Gas Cooler Regeneration Gas Separator

Recovery Tower and Expander-Recompressor The E R M Project does not impact the majority ofthis section. Therefore, only the modifications and key changes to the operation conditions are described below. Refer to the

CHAPTER 2





existing Operating Manual or the Addendum from the C2 Enhancement Project for additional information. 2.3.1

First Stage Dehydrated Feed Gas Chilldown The dry feed gas from 44-F-102 A/B is split into the following three streams:

A

•

41% to the 1st Stage X-Exchanger (44-E-301) where heat is exchanged with the residue gas.

•

13% to the 1 st Stage Liquid / Feed Exchanger (44-E-313) where heat is exchanged with the liquid from 44-V-303.

•

46% to the Feed Chiller (44-E-306) where propane refrigerant from the existing refrigeration system is used to chill the feed gas.

The first two flow paths are unchanged. In the third flow path, a new exchanger is added downstream of 44-E-306. This new exchanger, the 2nd Feed Chiller (44-E-318), further cools the feed gas using the low level refrigerant from the new refrigeration system. This enables higher ethane recovery. The feed gas from 44-E-306 enters the tube side of 44-E-318 at about - 7 C and is cooled to -17 C. A temperature indicator (44-TI-5120) is provided for the outlet stream. The liquid level on the shell side of 44-E-318 is maintained with a level control valve (44-LV-2111) located upstream of the exchanger, which expands the refrigerant to 1.0 barg and -26°C. Relief valves (44-PS V-8110 A/B - one operating, one spare) are provided to protect the shell side of 44-E-318 in the event of a tube rupture or fire. The vaporized propane returns to the Low Pressure Knockout Drum (44-V-207) as described in Section 2.7.5 of this Chapter. 0

0

The shell side of 44-E-318 is insulated and equipped with the following other instruments: Description Level Gauge Level Indicator Pressure Gauge Thermowell

Tag Number LG-2110 LI-2111 PG-4110 TW-5310

The exchanger and level instruments are manually drainable to the CDC. The new relief valves discharge to the Cold Flare. The chilled feed gas from 44-E-318 is combined with the feed gas from 44-E-301 and 44-E313 and sent to the 1st Stage KO Drum (44-V-301). After this modification, 44-V-301 will operate at -22 C compared to -9 C in the C2 Enhancement Project. 0

A

0

The temperature of 44-V-301 is controlled as follows: 1. The new refrigeration system is base loaded and the temperature of 44-V-301 is controlled with the existing refrigeration system. In this configuration, the set point for the 44-E-318 level controller remains fixed, and the 44-E-318 tube bundle remains completely submerged. The temperature of 44-V-301 is controlled by adjusting the speed of the 44-C-201. This is similar to the current control approach.

CHAPTER 2





This control strategy is recommended due to the flexibility of the existing steam turbine driver. An alternate temperature control mode for V-301 is also available to the operators. In the alternate mode, the existing refrigeration system is base loaded and the temperature of V-301 is controlled with the new refrigeration system. In this configuration, the set point for the 44C-201 speed controller would remain fixed. The temperature of 44-V-301 would be controlled by adjusting the propane level in 44-E-318 (44-TIC-5056 to LIC-2111 cascade control). A new Hand Switch (44-HS-5056) is provided to allow the operators to select which control strategy will be used. The alternate control mode is recommended only during the initial start-up phase of the ERM refrigeration system and when the existing refrigeration system is not operational.

A

The vapor from 44-V-301 is sent to the Second Stage Chilldown section. Liquid is sent to the l ' Stage Liquid Flash Drum (44-V-303) on level control via LV-2035. The lower operating temperature of 44-V-301 results in the condensation of more liquid. In order to handle the additional liquid, the capacity of LV-2035 was increased in the E R M Project by replacing the disk stack. 5

A

The temperature of the 44-V-303 should be monitored closely in conjunction with the temperature of 44-V-301. 44-V-303 is constructed of LTCS and has a cold design temperature of-45 C. The expected temperature in C2 recovery mode is -31°C. NOTE: This temperature should be maintained above -35°C to ensure that the temperature at the outlet ofthe 44- V-303 level control valve (44-L V-2040) does not fall below -45 C. A new temperature indicator (44-TI-5131) with a low temperature alarm has been provided at the outlet of 44-LV-2040 to alert the Operators of low temperatures. A new ESD valve (44-XV9080) has also been provided downstream of 44-LV-2040 to protect the downstream piping and 44-E-313 from low temperatures. The low-low temperature trip (44-TALL-5130) will also shut-off the supply of refrigerant to 44-E-318 by closing 44-LV-2 111. This will cause 44-V-301 and 44-V-303 to warm-up. The new ESD valve can be manually reset once the temperature of 44-V-301 increases to at least -15°C. 0

0

The existing feed gas bypass line around the First Stage Chilldown section is re-routed to between 44-E-306 and 44-E-318. High pressure drops across E-306 have been experienced in the past. Ifthe pressure drop on the feed gas side of 44-E-306 is much higher than the design valve, this will limit the flow through 44-E-306. The relocated bypass ensures that the new feed chiller can always be fully loaded by mixing warm feed gas from dehydration section with the outlet from 44-E-306. Manual valve 44-M-052 can be used to adjust the flow if required. The other existing flow control schemes used upstream of 44-V-301 will not be modified.

A

2.3.2

Second Stage Dehydrated Feed Gas Chilldown The vapor from 44-V-301 is also split into three streams. There are no process flow changes to this section of Unit 44. The existing control scheme is also unchanged. The 2nd Stage Feed K O Drum (44-V-302) will operate at -42 C compared to - 3 r C in the C2 Enhancement Project. 0

nd

Liquid from 44-V-302 is sent to the 2 Stage Liquid Flash Drum (44-V-304) on level control. The liquid from 44-V-304 is used to chill the feed gas in hairpin exchanger 44-E-314. 44-V304, the piping to 44-E-314, and 44-E-314 have cold design temperatures of-100 C and are o

CHAPTER 2




constructed of stainless steel. The outlet piping from 44-E-314 has a cold design temperature of -45 C and LTCS metallurgy. In normal operation, the shell side inlet temperature will be -67 C and the outlet temperature will be -28 C. In the event that the flow of gas on the hot side of 44-E-314 is reduced or stops, the shell side outlet temperature will decrease. The original design configuration depended on the feed gas to heat the cold side fluid to a safe temperature which allowed the change in metallurgy (SS to LTCS). However, in the event of a loss of flow on the hot side of E-314 due to a malfunction of the associated controller (TIC/TV-5067) or an inadvertent closure of a block valve, the shell side outlet piping can be exposed to temperatures below its cold design temperature. This condition could then lead to a potential brittle fracture. 0

0

0

To remedy this existing problem, new protection features are being added as a part of the E R M Project. The existing DCS temperature indicator (TI-5068) is being converted to a controller. A new minimum select is also being added to the V-304 level control loop. Ifthe shell side outlet temperature of E-314 begins to fall and approach system limits, the temperature controller will begin to throttle back the flow of cold liquid from V-304. This control configuration is similar to what was used previously for a similar low temperature problem area (V-306 overhead temperature) during the C2 Enhancement Project. An extra level of protection above and beyond the approach used during the C2 Enhancement Project is also provided for 44-E-314. As shown in the attached diagram, a vent solenoid (44LY-2044C) is being added to move the 44-V-304 level control (LV-2044) to its safe position (closed) in the event of low-low temperature at the outlet of the shell side of E-314. 44TALL-5126 activates the shutdown ifthe temperature falls to -43 C . In order to ensure reliability of the shutdown action, the signal comes from the ESD system, not the DCS. In addition, the LV-2044 bypass valve will be locked closed to ensure that the shutdown action cannot be circumvented. 0

NOTE: Ifthe LV-2044 bypass valve will be operated manually, the temperature downstream of 44-E-314 must be monitored carefully and continuously via 44-TI-S068. If the low temperature alarm set point is reached (-35C) the bypass valve should be closed immediately. 2.3.3

Turbo-expander / Recompressor This section of the unit was not modified for the E R M Project. Refer to the existing Operating, Maintenance and Safety Manual for a detailed description of the following equipment items: 44-EC-301: 44-E-311:

Expander Recompressor Residue Gas Aftercooler

Vapor from 44-V-302 is sent to the Turbo-expander (44-EC-301). Due to the increased feed chilling, the expander outlet temperature is reduced from -52 C in the C2 Enhancement design to -60 C. 0

o

2.3.4

Joule Thomson Operation JT operation is not significantly impact by the E R M Project. Because additional chilling is available from the new refrigeration package, higher product recoveries will be possible.

CHAPTER 2



2.3.5


Recovery Tower Aside from the colder operating temperatures, there are no changes to the Recovery Tower (44-V-305) portion of Unit 44. The existing process flow configuration and control schemes are unchanged. The new operating conditions for 44-V-305 are expected to be:

Pressure, barg Temperature, °C

Top

Bottom

39.5 barg

39.6 barg

0

-64 C

o

-60 C

As in current operation, the Recovery Tower reboiler is not in operation. The Recovery Tower should be operated at the lowest possible pressure to maximize ethane and propane recovery. The position of the pressure control valve in the residue gas outlet line (PV-3046A) should be monitored closely. The valve should be operated nearly wide open with minimum AP. It is not efficient to waste pressure drop across the control valve. Ifthe pressure drop across the control valve is excessive, the set point of PIC-3046 should be lowered. This will lower the operating pressure of the Recovery Tower and improve product recoveries.

2.4

Demethanizer and Recycle Compressor

2.4.1

Demethanizer The metallurgy ofthe existing Demethanizer (44-V-306) currently limits ethane recovery. This constraint was eliminated in the E R M Project by adding a small, new stainless steel Cold Demethanizer (44-V-308) to the unit. This new tower acts as an extension of 44-V-306 and allows colder temperatures in the important sections of the unit.

A

The Cold Demethanizer has 8 trays and a demister. The feed to the top tray consists ofthe cold stream from the Recovery Tower Bottoms Flash Drum (44-V-307) and the cold stream from the 2 Stage Liquid / Feed Exchanger (44-E-314). The bottom feed is the overhead vapor from the existing Demethanizer. The expected operating conditions for 44-V-308 are: nd

Pressure, barg 0

Temperature, C

Top

Bottom

23.3 barg

23.5 barg

0

-36 C

o

-20 C

44-V-308 is insulated and provided with the following instrumentation: Description Level Gauge Level Indicator Low-Low Level Shutdown

CHAPTER 2

Tag Number LG-2125 LI-2126 LALL-2127



Description Pressure Gauge Pressure Indicator Pressure Differential Temperature Indicator Thermowells


Tag Number PG-4115 (Below Tray 1) PI-3081 (Above Tray 8) PDI-3082 TI-5125 (Bottom Liquid) TW-5316 (Tray 8 Liquid) TW-5317 (Tray 5 Liquid)

The column and level instruments are manually drainable to the OD/CDC networks. The new tower will be in service during all modes of operation and cannot be isolated from the upstream reliefvalves at 44-V-306 (44-PSV-8029A/B/C) and the downstream relief valves at the core exchangers (44-PSV-8023A/B). Both sets of relief valves are set at 28 barg.

A The liquid from the bottom of 44-V-308 is returned to the top of 44-V-306 by the new Cold Demethanizer Bottoms Pumps (44-P-302 A/B) on level control (44-LV-2126). One pump is normally operating. A minimum flow bypass control loop (44-FV-1070) is provided for pump protection. Pressure gauges are provided in the suction (44-PG-4111 A/B) and discharge (44-PG-4112 A/B) of each pump. A DCS pressure indicator is provided in the common discharge line upstream of the level control valve. FI-1070 measures the flow in the common discharge line. The pumps are equipped with Hand/Off/Auto switches and remote Start/Stop buttons. A continuous vent line equipped with an orifice (FO-1071 A/B) allows proper degassing ofthe stand-by pump so that the pump can be started quickly in the event o f a failure ofthe main pump. The pump seal system (API Plan 53B) includes pressure gauges (PG-4117 A/B) and indicators (PI-3084 A/B). In the event of low-low seal pressure, the associated pump is tripped. Low-low level in 44-V-308 will also initiate a shutdown ofthe pumps. A unit or zone shutdown will also trip the pumps.

A

The deluge system covering 44-V-306 is extended to cover 44-V-308 and 44-P-302 A/B. Two new flammable gas detectors (GA-6025 and GA-6026) are provided in the seal area of the new Cold Demethanizer Bottoms Pumps. The suction line of the Cold Demethanizer Bottoms Pumps is equipped with an ESD valve. If the new gas detectors located near the pumps indicate the presence of hydrocarbon due to seal failure or some other problem, the DCS operator will activate XS-9081 A/B. This will close XV-9081 and trip both pumps. The overhead vapor from the Cold Demethanizer will be mixed with the vapor from 44-V307 and recycled to the Recovery Tower (44-V-305). This modification will change the molecular weight and flow rate ofthe recycle gas stream. The overhead pressure of 44-V-308 will be controlled by adjusting the speed ofthe Recycle Gas Compressor (44-C-301). This approach is identical to the existing control scheme. The heat input to the existing Demethanizer (44-V-306) will be reduced in order to hold the additional ethane. The T' Stage liquid from 44-E-313 will not be further pre-heated in 44-E315. The duty ofthe Bottom Reboiler (44-E-308) will also be decreased from 7.0 Gcal/h in

CHAPTER 2




the C2 Enhancement Project to 6.2 Gcal/h. As in the C2 Enhancement configuration, the condensation pressure for the steam side of 44-E-308 may be as low as 1 bara. The draw-off pumps added during the C2 Enhancement Project will continue to be required. In addition, in order to maintain the proper temperature at the bottom of the tower, it will be necessary to increase the steam condensate level in 44-E-308 to further reduce heat transfer. 2.4.2

Recycle Compressor As discussed above, the recycle gas from 44-C-301 will be bypassed around 44-E-315 to reduce the heat input to the Demethanizer (44-V-306). As in the C2 Enhancement configuration, the flow rate through the Recycle Trim Cooler (44-E-316) will be maintained at its design value. The flow of recycle gas through 44-E-307 will be varied to maintain the proper temperature profile in the Demethanizer (44-V-306).

/l\

As mentioned above, the Recovery Tower Reboiler (44-E-303) is not used in C2 recovery mode. In order to reduce the pressure drop in the recycle loop, a new bypass is added for 44E-303. This new bypass is located close to 44-E-302/4. The flow in the recycle loop will increase as a result ofthe E R M Project. To allow proper controllability, the capacity of PV-3058 was increased. Aside from the two new bypasses and control valve modification, the remaining flow, temperature, and pressure controls in the recycle loop will remain unchanged. Refer to the existing Operating, Maintenance and Safety Manual for addition information.

2.5

Debutanizer The E R M Project does not impact the majority ofthe Debutanizer section. Therefore, only the modifications and key changes operation conditions are described below. Refer to the existing Operating Manual or the Addendum from the C2 Enhancement Project for additional information. The N G L from the Demethanizer is sent to the NGL Fractionation section of Unit 44. The NGL is pre-heated in a feed/bottoms exchanger (44-E-401) and a steam heated exchanger (44-E-405). The partially vaporized feed enters the Debutanizer (44-V-401) above tray 23. The expected operating conditions for 44-V-401 are:

Pressure, barg

Top

Bottom

18.5 barg

18.8 barg

0

0

Temperature, C

0

72 C

177 C

The existing air-cooled condenser (44-E-402) cannot totally condense the ethane rich overhead product. A new trim condenser is required. This new exchanger, the Debutanizer Trim Condenser (44-E-406), condenses the overhead stream using the high level refrigerant from the new refrigeration system. The partially condensed stream from 44-E-402 enters the tube side of 44-E-406 at about 51 C and is cooled to 29 C. The liquid level on the shell side of 44-E-406 is maintained with a level control valve (44-L V-2116) located upstream of the exchanger, which expands the refrigerant to 6.4 barg and 16 C. The temperature of the NGL 0

0

0

CHAPTER 2

10




leaving 44-E-406 is monitored with TI-5127 and can be controlled by adjusting the set point of the level controller. The shell side of 44-E-406 is insulated and equipped with the following other instruments: Description Level Gauge Level Indicator Pressure Gauge Thermowell

Tag Number LG-2115 LI-2116 PG-4116 TW-5312

The exchanger and level instruments are manually drainable to the CDC. 44-E-406 is located at grade. In this configuration, the pressure at the exchanger will be higher than the pressure in the Overhead Accumulator (44-V-402). Therefore, the NGL leaving 44-E-406 must be subcooled to prevent vaporization in the drum. The Debutanizer pressure control scheme must be modified. Tower pressure will be controlled using the hot vapor bypass instead ofthe valve in the air cooler outlet line. The new control scheme works as follows: •

If the tower pressure falls, the hot vapor bypass will open. The hot vapor will warm-up the surface of the liquid in the accumulator, increasing the vapor pressure in the drum. This will cause liquid to accumulate in the trim condenser. Once enough surface area has been flooded with liquid, the system will reach a new equilibrium and the bypass will close.

•

If the tower pressure is too high, the bypass will close. The pressure in the accumulator will fall and liquid will move out of the exchanger into the drum. This will expose more surface area and the tower pressure will reduce.

The liquid from the accumulator is sent to the Debutanizer Overhead Pumps (44-P-401 A/B). A portion of the overhead product is returned to the tower on flow control as reflux. The required reflux rate is less than the C2 Enhancement design case. The remaining product liquid is sent to a new shell & tube exchanger. This new exchanger, the N G L Subcooler (44-E-407), cools the NGL product stream using the high level refrigerant from the new refrigeration system. The stream from 44-P-401 A/B enters the tube side of 44E-407 at about 29 C and is cooled to 20 C. The liquid level on the shell side of 44-E-407 is maintained with a level control valve (LV-2121) located upstream ofthe exchanger, which expands the refrigerant to 6.4 barg and 16 C. Temperature indication for the outlet NGL stream is provided (TI-5121). The flow controller downstream of 44-E-407 is reset by the accumulator level controller. 0

o

0

The shell side of 44-E-407 is insulated and equipped with the following other instruments: Tag Number LG-2120 LI-2121

Description Level Gauge Level Indicator

CHAPTER 2

11




Tag Number TW-5320

Description Thermowell

The exchanger and level instruments are manually drainable to the CDC. A common set of relief valves (44-PS V-8112 A/B - one operating, one spare) is provided to protect the shell sides of 44-E-406 and 44-E-407 in the event of a fire. The new relief valves discharge to the Cold Flare. The vaporized propane from these exchangers returns to the High Pressure Knockout Drum (44-V-206) as described in Section 2.7.4 of this Chapter.

2.6 A

Existing Propane Refrigeration System Other than the control modification described in Section 2.3.1, the E R M Project does not impact the equipment in the existing propane refrigeration system. Refer to the existing Operating Manual for a process description of the following existing equipment items: 44-V-201 44-V-202 44-V-203 44-V-204 44-E-201 44-E-202 44-C-201

2.7

Refrigerant Surge Drum Refrigerant Flash Drum First Stage Suction Drum Second Stage Suction Drum Refrigerant Condenser Refrigerant Subcooler C3 Refrigeration Compressor

ERM Refrigeration System A new closed-loop propane refrigeration system is installed as a part ofthe E R M Project. The new system provides the following two levels of refrigerant to the process: 0

•

Low level at about -26 C and 1.0 barg to 44-E-318 for chilling the feed gas

•

High level at about 16 C and 6.4 barg to 44-E-406/7 for condensing and subcooling the N G L product

0

The system has been designed for 110% ofthe normal requirements. The system includes a propane surge drum, knockout drums for each pressure level, subcooling exchangers for each pressure level, an air-cooled condenser, and centrifugal compressor. 2.7.1

Propane Receiver, 44-V-205 3

The Propane Receiver, 44-V-205, has a storage capacity of 53 m or about 110% ofthe liquid inventory in the system. Propane supply and make-up are provided from the existing Propane Storage Drum and Transfer Pumps in Unit 45. The Propane Receiver is filled manually using a globe valve. 0

The expected operating conditions are 55 C and 18.5 barg. The pressure ofthe drum is controlled by PIC-3410A acting on the hot vapor bypass (PV-341 OA) around the Propane Condenser (44-E-203). A pressure controlled vent to flare (PV-341 OB) is also provided at the

CHAPTER 2

12





drum. Light components in the receiver can be purged to the flare as required using PIC3410B. The Propane Receiver is provided with the following instrumentation: Description Level Gauge Level Indicator Pressure Gauge Pressure Indicator Pressure Safety Valves

Tag Number LG-2413 LI-2403 PG-4403 PI-3410 PSV-8403 A/B (fire case)

The vessel and level instruments are manually drainable to the CDC/OD networks. The new relief valves discharge to the Cold Flare. The deluge system protecting 44-V-201 is extended to cover 44-V-205. 2.7.2

High Temperature Subcooler, 44-E-204 The liquid from 44-V-205 is routed to the High Temperature Subcooler (44-E-204). A slipstream of the liquid is letdown in pressure across a level control valve (LV-2404) and sent to the shell side of 44-E-204 at 6.4 barg and 16 C to provide cooling for the remaining refrigerant liquid from the receiver that is sent to the tube side of 44-E-204. The refrigerant liquid on the tube side is cooled from 55 C to 18 C. The majority of the subcooled refrigerant leaving 44-E-204 is then sent to the Debutanizer Trim Condenser (44-E-406) and N G L Subcooler (44-E-407) for process cooling. Subcooling the refrigerant ensures that there is no vaporization of the liquid upstream of the level control valves at the remote evaporators. The level on the shell side of 44-E-204 is controlled via LIC-2404 to maintain the tube bundle submerged. 0

0

0

44-E-204 is insulated and provided with the following instrumentation:

A

Tube Side Inlet Thermowell

44-TW-5332

Tube Side Outlet Thermowell Temperature Indicator Pressure Indicator Flow Indicator

44.TW-5333 44-TI-5411 44-PI-3411 44-FI-1411 (Flow to 44-E-406/7)

Shell Side Level Indicator

44-LIC-2404

Poor exchanger performance or wanner than expected temperatures may be signs of accumulation of heavy hydrocarbons in the exchanger. 44-E-204 has a low point drain that can be used to remove heavy hydrocarbons from the system. This drain is connected to the cold closed drain system.

CHAPTER 2

13




2.7.3


Low Temperature Subcooler, 44-E-205 The remaining portion ofthe subcooled refrigerant from 44-E-204 is sent to the Low Temperature Subcooler (44-E-205). A slipstream ofthe subcooled liquid is letdown in pressure across a level control valve (LV-2405) and sent to the shell side of 44-E-205 at 1.0 barg and -26 C to provide cooling for the remaining liquid refrigerant from the High Temperature Subcooler that is sent to the tube side of 44-E-205. The refrigerant liquid on the tube side is cooled from 18 C to -24 C. The subcooled refrigerant is then sent to 44-E-318 for process cooling. The level on the shell side of 44-E-205 is controlled via LIC-2405 to maintain the tube bundle submerged. 0

0

0

44-E-205 is insulated and provided with the following instrumentation: Tube Side Inlet

A

Thermowell

44-TW-5330

Tube Side Outlet Thermowell Temperature Indicator Pressure Indicator Flow Indicator Shell Side Level Indicator

44-TW-5331 44-TI-5412 44-PI-3412 44-FI-1412 (Flow to 44-E-318) 44-LIC-2405

Poor exchanger performance or warmer than expected temperatures may be signs of accumulation of heavy hydrocarbons in the exchanger. 44-E-205 has a low point drain that can be used to remove heavy hydrocarbons from the system. This drain is connected to the cold closed drain system. 2.7.4

High Pressure Knockout Drum, 44-V-206 The vaporized propane from process exchangers 44-E-406/7 is sent to the High Pressure Knockout Drum (44-V-206). The pressure and temperature of this returning stream are measured using 44-PI-3413 and 44-TI-5413 respectively. A n automated isolation valve (XV7401) is provided in this line to allow separation of the process exchangers from the refrigeration system. 44-V-206 is mounted directly above the High Temperature Subcooler. Vapor from the shell side of 44-E-204 flows to 44-V-206 and mixes with the vapor from 44-E-406/7. The High Pressure Knockout Drum operates at about 6.4 barg and 16 C. The combined vapor stream exits the drum and flows to side load connection of the Propane Compressor (44-C-202). 0

Any liquid entrained from the remote evaporators (44-E-406/7) or from excess quenching will end up in the knockout drum. This liquid will fall into the High Temperature Subcooler and be vaporized. This configuration eliminates the need to have a vaporization coil in the High Pressure Knockout Drum or a drain pump. There is normally no liquid level in 44-V-206. The High Pressure Knockout Drum is insulated and provided with the following instrumentation:

CHAPTER 2

14



Description Level Gauge High Level Alarm Pressure Safety Valves


Tag Number LG-2414 LAHH-2401 PSV-8401 A/B (fire case)

The vessel and level instruments are manually drainable to the CDC/OD networks. The new relief valves discharge to the Cold Flare. 2.7.5

Low Pressure Knockout Drum, 44-V-207 The vaporized propane from process exchanger 44-E-318 is sent to the Low Pressure Knockout Drum (44-V-207). The pressure and temperature of this returning stream are measured using 44-PI-3414 and 44-TI-5414 respectively. An automated isolation valve (XV7402) is provided in this line to allow separation of the process exchangers from the refrigeration system. 44-V-207 is mounted directly above the Low Temperature Subcooler. Vapor from the shell side of 44-E-205 flows to 44-V-207 and mixes with the vapor from 44-E-318. The Low Pressure Knockout Drum operates at about 1.0 barg and -26 C. The combined vapor stream exits the drum and flows to the Propane Compressor (44-C-202). 0

Any liquid entrained from the remote evaporator (44-E-318) or from excess quenching will end up in the knockout drum. This liquid will fall into the Low Temperature Subcooler and be vaporized. This configuration eliminates the need to have a vaporization coil in the High Pressure Knockout Drum or a drain pump. There is normally no liquid level in 44-V-207. The Low Pressure Knockout Dmm is insulated and provided with the following instrumentation: Description Level Gauge High Level Alarm Pressure Safety Valves

Tag Number LG-2415 LAHH-2402 PSV-8402 A/B (fire case)

The vessel and level instruments are manually drainable to the CDC/OD networks. The new relief valves discharge to the Cold Flare. 2.7.6

Propane Compressor, 44-C-202 The Propane Compressor (44-C-202) is a two-suction machine driven by a fixed speed, 5.8 M W motor. Each compressor suction line is provided with the following instrumentation: Description Low Pressure Alarm (with trip) Pressure Indicator Pressure Gauge

CHAPTER 2

st

1 Stage Suction PALL-3405 PI-3403 PG-4405

15

Side Load PALL-3404 PI-3402 PG-4406



Pressure Control Valve Differential Pressure Gauge

PV-3402B PDG-4400 Tl-5403 TI-5405 TG-6405 FI-1403

Temperature Indicator Temperature Gauge Flow Indicator

GASCO Project Nol: 13522102 Doc. No.: PP-AOWT-44-00-001

PV-3402A PDG-4401 TI-5402 TI-5404 TG-6406 FI-1402

Pressure control valves in each suction line are provided to ensure that the load on the compressor does not increase above the capacity ofthe motor. The valves are also used during hot start-up. The performance controller PIC-3402 modulates these valves. The performance controller is a part of the anti-surge system. Refer to the information from the anti-surge vendor (CCC) for a more detailed description. 0

The compressor discharge conditions are approximately 75 C and 19.5 barg. The discharge line contains the following instrumentation: Description High Pressure Alarm (with trip) Pressure Indicator Pressure Gauge High Temperature Alarm (with trip) Temperature Indicator Flow Indicator Pressure Safety Valves

Tag Number PAHH-3400 PI-3401 PG-4402 TAHH-5400 TI-5401 FI-1400 PSV-8400 A/B (blocked discharge)

An automated isolation valve (XV-7400) is provided in the discharge line of the compressor. This valve, in conjunction with XV-7401 and XV-7402, allow the compressor system to be isolated from the remaining equipment. A depressurization valve (XV-7405) located upstream of XV-7400 is provided to allow the isolated system to be safely depressurized to the cold flare system. The deluge system protecting 44-C-201 is extended to cover 44-C-202. Two new flammable gas detectors (GA-6023 and GA-6024) are located in the seal area of the new compressor.

A

The compressor is supplied with dedicated seal gas, buffer gas, and lube oil systems. In addition, since the compressor motor is operating in a classified area, it is provided with an air purge and pressurization system. Refer to the vendor manual for a description of these systems. 2.7.7

Anti-Surge Protection Each compression stage is protected with a recycle (anti-surge) line and control valve to prevent surge. The recycle valves can send a portion of the compressor discharge vapor back to the suction of each stage (FV-1403 and FV-1402 for the first and second stage respectively). The subcooled refrigerant from 44-E-205 is used to remove the heat of compression. The addition of quench liquid is temperature controlled at each suction drum (TV-5404 for 44-V-206 and TV-5405 for 44-V-207). A high level override is provided to

CHAPTER 2

16




prevent the temperature controllers from continuing to add quench liquid if the levels in the knockout drums are high. 2.7.8

Propane Condenser, 44-E-203 The compressed propane vapor is condensed in an air-cooled exchanger. The propane liquid leaving the Propane Condenser (44-E-203) free drains to the Propane Receiver (44-V-205). Non-condensables can be vented to the cold flare from the high points of Propane Condenser via a HIC and control valve (HIC-9092 and HV-9092). The vent valve has been specified as Tight Shut Off to minimize propane losses to the flare. The condenser has been designed for an air temperature of 46 C. Manually operated louvers (HIC-9091) are provided to reduce airflow on cold days. 0

As discussed in Section 2.7.1, the pressure in 44-V-205 is maintained using a condenser bypass. If the pressure starts to fall in the receiver, the bypass opens. This increases the pressure in the receiver and causes the liquid to accumulate in the condenser. Once enough air cooler surface has been flooded with liquid, the system will reach a new equilibrium and the bypass will close. The performance of 44-E-203 can be monitored using: Description

Tag Number TI-5400 (inlet) TI-5410 (outlet) TG-6400 (outlet)

Temperature Indicator Temperature Gauge

2.8

Unit 44 Isolations The E R M Project does not impact the battery limit isolation valves in Unit 44.

2.9

Flare and Blowdown Valves A brief summary of the new valves is provided in the table below. VALVE NUMBER

P&ID NUMBER

OUTLET

INLET

XV-7405

22717-104

Cold Flare

44-C-202 Discharge

PV-341 OB

22717-101

Cold Flare

44-V-205

HV-9092

44-00-30-041

Cold Flare

Inlet line to 44-E-203

CHAPTER 2

17

USE Depressurization of 44-C-202 Pressure control of 44-V-205 Depressurization of 44-E-203


3.0



ELEMENTS OF PROCESS CONTROL PHILOSOPHY Unit 44 can be operated in either C2 recovery mode or C2 rejection mode. As the objective ofthe E R M Project is to recover additional C2, the design case is the C2 recovery mode of operation. However, the design of the new equipment will allow the unit to be switched back to C2 rejection mode of operation without demerits to existing performance. The plant has also been designed with the flexibility to operate at any point between the maximum C2 recovery case and the C2 rejection case. The Chapters below define the controller set points and actions required to adjust the ethane recovery level to the desired level.

3.1

Existing Controls Modified for ERM Operation 44-LV-2035: Due to the additional chilling, the amount of liquid condensed in 44-V-301 will increase. The capacity of the existing level control valve (44-LV-2035) is not adequate for the new conditions. The disk stack of the valve is modified to increase the capacity ofthe valve (larger Cv). 44-PV-3058: The new operating conditions will change the molecular weight and flow characteristics ofthe recycle gas. The capacity of the existing Recovery Tower reflux valve (44-PV-3058) is not adequate for the new conditions. The valve trim is modified to increase the capacity of the valve (larger Cv). 44-XV-9080: In some of off-design and failure cases, the temperature downstream of 44-V303 level control valve (44-LV-2040) may fall below the temperature rating (-45°C) of the downstream piping and heat exchanger (44-E-313). A new ESD valve is provided to protect the shell side of E-313 from exposure to low temperatures. TALL-5130 will close this valve if the temperature approaches the limits. 44-PIC-3064: The Debutanizer pressure control scheme is modified to work with the new Debutanizer Trim Condenser (44-E-406). The new scheme works as follows: •

Ifthe tower pressure falls, PV-3064 will open. The hot vapor will warm-up the surface of the liquid in 44-V-402, increasing the vapor pressure in the drum. This will cause liquid to accumulate in 44-E-406. Once enough surface area has been flooded with liquid, the system will reach a new equilibrium and the bypass will close.

•

If the tower pressure is too high, the bypass will close. The pressure in 44-V-402 will fall and liquid will move out of 44-E-406 into the drum. This will expose more surface area and the tower pressure will reduce.

TIC-5056/44-HS-5056: A new hand switch is added which allows the operator to select which refrigeration system will be used to control the temperature of 44-V-301. There are two options for the hand selector: 1. The signal from 44-TIC-5056 is cascaded to the performance controller (44-PIC-3630) of the existing refrigeration compressor 44-C-201. In this mode, the temperature of 44-V301 is controlled by varying the speed of 44-C-201 which adjusts the heat transfer in the existing Feed Chiller (44-E-306). The new 2 Feed Chiller (44-E-318) operates in a base loaded condition with a fixed level setpoint. nd

CHAPTER 2


2.



nd

The signal from 44-TIC-5056 is cascaded to the level controller (44-LIC-2111) of the 2 Feed Chiller. In this mode, the temperature of 44-V-301 is controlled by varying the level of propane on the shell side of 44-E-318. This adjusts the heat transfer/duty of 44-E-318. The cooling duty provided by the existing Feed Chiller (44-E-306) is constant as the Refrigeration Compressor (44-C-201) will have a fixed speed setpoint.

44-TIC-5068/44-LY-2044A: The existing DCS temperature indicator (TI-5068) is being converted to a controller. A new minimum select (44-LY-2044A) is also being added to the V-304 level control loop. If the shell side outlet temperature of E-314 begins to fall and approach the system limits, the temperature controller will begin to throttle back the flow of cold liquid from V-304. 44-LY-2044C: In some failure scenarios, the shell side outlet temperature of 44-E-314 will fall below its design temperature. A new vent solenoid is added in the LIC-2044 control loop to close LV-2044 if the temperature approaches the limits. The new TALL-5126 imitates the trip. The trip signal comes from the new Triconex. 44-FIC-1048: The NGL product from 44-P-401 A/B is further cooled in the new NGL Subcooler (44-E-407). Due to this, the existing temperature indicator (44-TI-5105) used by the existing flow controller (44-FIC-1048) no longer reports the temperature of the NGL sent to storage. A new temperature indicator (44-TI-5121) located downstream of 44-E-407 will be used as a correction for the existing flow controller.

3.2

New Controls Added for ERM Operation

3.2.1

Cold Demethanizer System 44-LIC-2126: This new controller is used to maintain the level in the Cold Demethanizer. The controller modulates a valve (44-LV-2126) in the discharge line from the Cold Demethanizer Bottoms Pumps. 44-FIC-1070: This controller provides minimum flow protection for the Cold Demethanizer Bottoms Pumps. If the flow from the pumps decreases below the minimum flow setpoint, the controller will open FV-1070 and liquid will be recycled back to the Cold Demethanizer. 44-LALL-2127: This trip function shuts down the Cold Demethanizer Bottoms Pumps if the level in the Cold Demethanizer falls to the low-low setpoint. 44-PALL-3084A/B: This trip function shuts down the Cold Demethanizer Bottoms Pumps if the level in the pressure in the pump seal pot falls to the low-low setpoint. 44-XS-9081: This push button closes the ESD valve in the liquid outlet line from the Cold Demethanizer. The trip action also stops the Cold Demethanizer Bottoms Pumps. The ESD valve is intended to prevent the large liquid inventory in the bottom ofthe Cold Demethanizer from being released in the event of a seal failure or fire. Gas detectors located by the pumps would alert the operator of such a hazardous condition.

CHAPTER 2

19


3.2.2



New Process Chillers nd

44-LIC-2111: This controller is used to maintain the level of propane in the 2 Feed Chiller (44-E-318). The controller can operate in cascade mode with the 44-V-301 temperature controller (44-TIC-5056). The controller modulates a valve (44-LV-2111) in the propane supply line. 44-LIC-2116: This controller is used to maintain the level of propane in the Debutanizer Trim Condenser (44-E-406). The controller can operate in cascade mode with the 44-V-402 temperature controller (44-TIC-5127). The controller modulates a valve (44-LV-2116) in the propane supply line. 44-LIC-2121: This controller is used to maintain the level of propane in the NGL Subcooler (44-E-407). The controller modulates a valve (44-LV-2121) in the propane supply line. 3.2.3

E R M Refrigeration System A brief description of the new ERM Refrigeration controls is provided in this section. Refer to the attached vendor narrative for more information. The controls for the compressor auxiliary systems (lube oil, seal gas, motor cooling and purging) are described in the vendor narrative. 44-PIC-3410A: This controller is used to maintain the pressure in the Propane Receiver (44V-205). The controller modulates the 44-E-203 hot vapor bypass valve (44-PV-3410A). The hot vapor from the discharge of the Propane Compressor (44-C-202) warms the surface of the liquid and raises the pressure in 44-V-205. 44-PIC-3410B: This controller provides high pressure protection for 44-V-205. The controller will open 44-PV-3410B before the reliefvalves lift. 44-LIC-2404: This controller is used to maintain the level of propane in the High Temperature Subcooler (44-E-204). The controller modulates a valve (44-LV-2404) in the propane supply line. 44-LIC-2405: This controller is used to maintain the level of propane in the Low Temperature Subcooler (44-E-205). The controller modulates a valve (44-LV-2405) in the propane supply line. 44-TIC-5404: This controller is used to maintain the Propane Compressor side load suction temperature. The controller modulates a quench valve (44-TV-5404) in the propane supply line. Subcooled propane from 44-E-205 is used for quenching. The TIC-5404 control loop includes a minimum select block (44-TY-5404A). Ifthe level in the High Pressure Knockout Drum (44-V-206) is high, the signal from 44-LIC-2404 will be selected and the flow of quench will be reduced. This will prevent the compressor from tripping on high-high level in 44-V-206. st

44-TIC-5405: This controller is used to maintain the Propane Compressor 1 stage suction temperature. The controller modulates a quench valve (44-TV-5405) in the propane supply line. Subcooled propane from 44-E-205 is used for quenching. The TIC-5405 control loop includes a minimum select block (44-TY-5405A). Ifthe level in the Low Pressure Knockout Drum (44-V-207) is high, the signal from 44-LIC-2405 will be selected and the flow of

CHAPTER 2

20




quench will be reduced. This will prevent the compressor from tripping on high-high level in 44-V-207. 44-FIC-1402: This controller is part of the CCC anti-surge control package. The controller opens the recycle valve to keep the compressor operating a safe distance from the surge. 44-FIC-1403: This controller is part of the CCC anti-surge control package. The controller opens the recycle valve to keep the compressor operating a safe distance from the surge. 44-PIC-3402A/B: These controllers are also part of the CCC anti-surge control package. The controllers modulate the valves in the 1 stage suction and side load suction lines. The valves are used during hot start-up to prevent the motor from tripping on over-current. The controllers are also active during normal operation. If the load on the compressor approaches the power limit of the motor, the valves begin to close. This will increase the pressure and the evaporation temperature in the chillers. The increased temperature will result in reduced heat transfer in the chillers. This will then decrease the load on the compressor. st

44-HIC-9091: This controller adjusts the louvers on the Propane Condenser (44-E-203). During very cool ambient conditions, it may be necessary to partially close the louvers to reduce the cooling duty of the exchanger. NOTE: Ifthe hot vapor bypass (44-PV-3410A) is completely open and the pressure of the Propane Receiver falls to the low alarm point, the hand controller should be used to partially close the louvers. 44-HIC-9092: This controller is used to open the high point vent on the Propane Condenser (44-E-203). High compressor discharge pressure or poor aircooler performance may be a sign of a build up of non-condensables in the system. The hand controller is used to vent the noncondensables to the Cold Flare system.

CHAPTER 2


4.0


DCS SCREEN DISPLAYS The new and modified DCS graphics are included in this section.

("AS-BUILT" GRAPHICS TO BE INSERTED WHEN AVAILABLE)

CHAPTER 2

22



Ethane Recovery Maximization (ERM) Project Operating, Maintenance and Safety Manual - Unit 44 Addendum for the ERM Project-Rev. 1


CHAPTER 3

INITIAL START-UP

CONTENTS

SECTION 1.0

2.0

PAGE

GENERAL. 1.1

Phase 1: Initial Start-up after the Scheduled Shutdown of the Existing Unit

3

1.2

Phase 2: Initial Start-up ofthe New Extension

3

PREPARATION PRIOR TO INITIAL PHASE 1 OPERATION nd

3.0

2.1 Preparation of the 2 Feed Chiller 2.2 Preparation of the HP Recycle Gas Circuit 2.3 Preparation of the Cold Demethanizer 2.4 Preparation of the Debutanizer Trim Condenser and NGL Subcooler 2.5 Preparation of the Cold Demethanizer Bottoms Pumps 2.6 Preparation of the E R M Refrigeration Package PHASE 1 PURGING 3.1 3.2 3.3 3.4

4.0

PHASE 1 COMMISSIONING OF UTILITY SYSTEMS 4.1 4.2 4.3 4.4 4.5 4.6 4.7 4.8

5.0

nd

2 Feed Chiller HP Recycle Gas Circuit Cold Demethanizer Debutanizer Trim Condenser and N G L Subcooler

Instrument Air Plant Air Nitrogen Saturated Low Pressure Steam Utility Water Fire Deluge Cold Flare and Acid Gas Flare Closed Drain Cryogenic

FINAL PREPARATION IN PHASE 1 PRIOR TO FEED-IN 5.1 5.2 5.3

Dehydration Section N G L Recovery Section Refrigeration Section

5 5 5 6 7 8 8 9 9 9 9 9 10 10 11 11 12 12 12 13 13 14 14 14 14

6.0

PHASE 1 START-UP

7.0

PREPARATION PRIOR TO INITIAL PHASE 2 OPERATION

17

7.1 7.2

17 18

CHAPTER 3

Preparation of the E R M Refrigeration System Preparation of the Cold Demethanizer Bottoms Pumps

15


8.0



PHASE 2 PURGING

20

8.1

E R M Refrigeration System

20

8.2


21

9.0

FINAL PREPARATION IN PHASE 2 PRIOR TO START-UP

22

10.0

9.1 Pressurization of the E R M Refrigeration Section 9.2 Filling 44-V-205 9.3 Pressurization of Cold Demethanizer Bottoms Pumps 9.4 Liquid Fill the Cold Demethanizer and the Bottoms Pumps 44-P-302A/B PHASE 2 START-UP

22 24 24 24 26

10.1 Cold Demethanizer Bottoms Pumps Start-up 10.2 Propane Compressor Start-up 10.3 Transition to E R M Mode

26 27 30

CHAPTER 3


1.0



GENERAL The new E R M equipment, piping and instruments will be started-up in two phases. The first phase will occur during scheduled shutdown of OGD-I Train 3. During the shutdown, all the E R M tie-ins will be made in Unit 44. At the end ofthe shutdown period, the existing unit will be restarted. At this time, a portion of the E R M related piping and equipment must be completely commissioned. This equipment and piping will be fully integrated with the existing system and will be "live" after the restart. In Phase 2, the remaining elements (ERM Refrigeration Package and the Cold Demethanizer Bottoms Pumps) will be commissioned and phased into the existing unit to achieve the required ethane production rate. Prior to the initial start-up of both phases, all pre-commissioning activities must have been completed. Pre-commissioning covers those activities required to bring the new systems to a "ready for start-up" condition from original construction. In general, it consists of inspection, checking and testing operations required to ensure that all components of the project are properly installed and mechanically complete. Pre-commissioning will be performed by the construction team in close coordination with the operations and commissioning teams. Check lists will be used document the completion of the pre-commissioning activities. It is not in the scope of this document to provide full details of the pre-commissioning activities. These activities are described and defined in the. Mechanical Completion, Pre-Commissioning and Commissioning Manuals.

1.1

Phase 1: Initial Start-up after the Scheduled Shutdown of the Existing Unit In order to make the tie-ins to connect the new E R M expansion to the existing plant, the existing unit must be shutdown, blinded off and purged to make safe tie-ins possible. After all tie-ins and connecting piping work is completed, the existing unit can be restarted. Major parts ofthe new E R M extension will also be purged and commissioned with the restart of the existing unit. The modifications implemented in Phase 1 do not change the operation of the existing unit. Since the new refrigeration system is not commissioned at this stage, the new E R M equipment and lines will be part ofthe process flow, but will not have any impact on the process. In other words, the unit will not be operated in high ethane recovery mode after the Phase 1 start-up. Blinds need to be in place as per the marked P&ID's in the Pre-commissioning Manual. These blinds ensure a separation between the part that is live at the restart and the part not yet ready for commissioning. These blinds are so called "red tag" blinds and can only be removed with a proper permit signed by Fluor's Commissioning Manager.

1.2

Phase 2: Initial Start-up of the New Extension The start up of the remaining part of the new E R M extension will take place after all the remaining pre-commissioning work on the Propane Compressor and the Cold Demethanizer Bottoms Pumps is completed. Purging of these parts has to take place according to the procedure in Sections 7.0 and 8.0 of this Chapter and as described in the Pre-commissioning

CHAPTER 3




Manual. Once the E R M systems have been properly purged, they can be commissioned and Unit 44 can be transitioned to the ERM mode of operation.

CHAPTER 3



2.0


PREPARATION PRIOR TO INITIAL PHASE 1 OPERATION The following procedures outline a suggested method for air purging the new sections and commissioning the relevant utility systems. There are other suitable options. The procedures given here should be used only as a guide and subject to further development at site.

2.1

Preparation of the 2

nd

Feed Chiller

This section includes 44-E-318. Check and ensure that the following essential equipment is in the correct position/status: •

A l l vents, drains, and purging connections are closed

•

A l l instruments and bridle block valves are open

•

The relevant valves have been locked open or closed according to their nonnal positions shown on the P&ID's

•

The relevant manual valves are open or closed. See Table 2.1.1.

•

A l l bypasses of control valves and safety valves are closed.

•

A l l control valves are in manual mode. See Table 2.1.2 for the conect position of the valves

•

A l l on-off shutdown valves are closed

Table 2.1.1 A l l manual valves are in their normal operating position except for the following: VALVE NO.

FUNCTION 44-LV-2111 upstream

LINE NUMBER 44-2007-RF-4"31170-C

P&ID NUMBER 44-00-30019-2

POSITION Closed

P&ID NUMBER 44-00-30019-2

POSITION Closed

Table 2.1.2 The positions ofthe control valves are as follows: VALVE NO. 44-LV-2111

2.2

FUNCTION 44-E-318 Level

LINE NUMBER 44-2007-RF-4"31170-C

Preparation ofthe HP Recycle Gas Circuit New bypasses have been added in the HP recycle gas loop around 44-E-303 and 44-E-315. The positions of the valves are as follows: VALVE NO. 44.M-4405

FUNCTION 44-E-315 Bypass

44-M-4406

44-E-315 Inlet

CHAPTER 3

LINE NUMBER 44-2020-HC-10"61010-C 44-2020-HC-10"-

P&ID NUMBER 44-00-30024

POSITION Closed

44-00-30024

Open


VALVE NO.


FUNCTION 44-E-303 Bypass

2.3

LINE NUMBER 61010-C 44-2002-HC-10"63030-C


P&ID NUMBER

POSITION

44-00-30023-4

Closed

Preparation ofthe Cold Demethanizer This section includes 44-V-308. Check and ensure that the following essential equipment is in the correct position/status: •


•


•

The relevant valves have been locked open or closed according to their normal positions shown on the P&ID's. Refer to Table 2.3.1.

•


•


•

A l l control valves are in manual mode. See Table 2.3.3 for the correct position of the valves.

•


Table 2.3.1 A l l locked valves are in their nonnal operating position except for the following: VALVE NO. M-4401 M-4402 M-4403 M-4404

FUNCTION 44-E-314 Shell Side Outlet 44-E-314 Shell Side Outlet 44-FV-1204 downstream 44-E-314 Outlet

LINE NUMBER 44-2012-HC-6' 31170-C 44-2012-HC-6"31170-C 44-2013-HC-8"33450-C 44-2013-HC-8"33450-C :

P&ID NUMBER 44-00-30020

POSITION Open

44-00-30020

Closed

44-00-30023-1

Open

44-00-30023-1

Closed


FUNCTION 44-P-302A suction 44-P-302B suction 44-P-302A/B vent 44-LV-2126

CHAPTER 3

LINE NUMBER 44-2014-HC-12" 33450-C 44-2014-HC-3"33450-C 44-2015-HC-2' 33450-C 44-2015-HC-8":

P&ID NUMBER 44-00-30023-4

POSITION Closed

44-00-30023-4

Closed

44-00-30023-4

Closed

44-00-30023-4

Closed



VALVE NO.

FUNCTION downstream 44-FV-1070 downstream

LINE NUMBER 33450-C 44-2016-HC-4"33450-C


P&ID NUMBER

POSITION

44-00-30023-4

Closed

P&ID NUMBER 44-00-30023-4

POSITION Closed

44-00-30023-4

Open

Table 2.3.3 The positions of the control valves are as follows:

2.4

VALVE NO. 44-LV-2126

FUNCTION 44-V-308 Level

44-FV-1070

P-302A/B Min Flow Bypass

LINE NUMBER 44-2015-HC-8"31170-C 44-2016-HC-4"33450-C

Preparation ofthe Debutanizer Trim Condenser and NGL Subcooler This section includes 44-E-406 and 44-E-407. Check and ensure that the following essential equipment is in the correct position/status: •


•


•

The relevant valves have been locked open or closed according to their normal positions shown on the P&ID's

•


•


•

A l l control valves are in manual mode. See Table 2.4.2 for the correct position ofthe valves.

«



FUNCTION 44-LV-2116 upstream 44-LV-2121 upstream

LINE NUMBER 44-2024-RF-6' 31170-C 44-2034-RF-3' 31170-C :

P&ID NUMBER 44-00-30028-1

POSITION Closed

44-00-30028-3

Closed

P&ID NUMBER 44-00-30028-1

POSITION Closed

Table 2.4.2 The positions of the control valves are as follows: VALVE NO. 44-LV-2116

CHAPTER 3

FUNCTION 44-E-406 Level

LINE NUMBER 44-2024-RF-6"-



2.5

VALVE NO.

FUNCTION

44-LV-2121

44-E-407 Level

LINE NUMBER 31170-C 44-2034-RF-3"31170-C


P&ID NUMBER

POSITION

44-00-30028-3

Closed

Preparation of the Cold Demethanizer Bottoms Pumps 44-P-302 A/B will not be used in the Phase 1 start-up. The pumps should be completely and positively isolated from the sections of the unit that will be live after the re-start of Unit 44.

2.6

Preparation of the ERM Refrigeration Package This section includes 44-V-405,44-V-206, 44-V-207, 44-E-203, 44-E-204, 44-E-205 and 44C-202. This equipment will not be used in the Phase 1 start-up. The E R M Refrigeration Package should be completely and positively isolated from the sections of the unit that will be live after the re-start of Unit 44.

CHAPTER 3





3.0


PHASE 1 PURGING The procedure defined in Chapter 3, Section 3.0 of the existing Operating, Maintenance and Safety Manual should be followed for purging the new E R M equipment. The existing procedures should be augmented by the procedures by contained in the E R M PreCommissioning and Commissioning Manual.

3.1

2

nd

Feed Chiller st

nd

The tube side of 44-E-318 is purged with the section including the 1 Stage and 2 Stage Feed K O Drums. Refer Chapter 3, Section 3.4 of the existing manual for a description ofthe procedure and isolation points. The shell side of 44-E-318 is pressurized using the 2" utility connection on the exchanger. Depressurization is performed using the 2" vent on 44-E-318.

3.2

HP Recycle Gas Circuit The new bypass lines in the HP Recycle Gas circuit are purged with the section including the 44-E-303 and 44-E-315. Refer Chapter 3, Section 3.5 of the existing manual for a description of the procedure and isolation points.

3,3

Cold Demethanizer 44-V-308 is purged with the Demethanizer section. Refer Chapter 3, Section 3.7 ofthe existing manual for a description of the procedure and isolation points. 44.V-308 is isolated by 44-XV-9081,44-FV-1070, 44-LV-2126, M-4402 and the valve in the 44-P-302A/B vent line. 44-V-308 can be pressurized using the 2" utility connection and depressurized using the 3" vent valve and the 1" drain valves located downstream of 44-FV-1070 and downstream of 44LV-2126.

3.4

Debutanizer Trim Condenser and NGL Subcooler The tube sides of 44-E-406 and 44-E-407 are purged with the Debutanizer section. Refer Chapter 3, Section 3.8 of the existing manual for a description of the procedure and isolation points. The shell sides of 44-E-406 and 44-E-407 are pressurized using the 2" utility connection on the exchangers. Depressurization is performed using the 2" vents on 44-E-406 and 44-E-407.

CHAPTER 3



4.0


PHASE 1 COMMISSIONING OF UTILITY SYSTEMS There are several utility systems that were extended to serve the new equipment. The following utilities will be started up prior to the restart of the existing plant. •

Instrument air

•

Plant air

•

Nitrogen

•

Saturated Low Pressure Steam

•

Utility Water

o

Fire Deluge

•

Cold Flare and Acid Flare

•

Cold Drain Cryogenic

The open drain system is connected to the existing open drain system. This is underground piping and will be completed in an early stage. The open drain system needs to be available at the restart of the existing unit, it may be necessary to cover the open funnels to avoid hydrocarbons in areas still under construction or pre-commissioning. Below is a description of the different utilities that need to be live at the restart of the existing unit

4.1

Instrument Air Instrument air is required early to facilitate the instrumentation loop checking and stroking of the new or modified control valves. It is important to notify GASCO Operations about the intended commissioning of the instrument air system. The instrument air system is cleaned using instrument air as per the procedure in the PreCommissioning Manual. After the shutdown, the existing instrument air system will be commissioned according to the procedure given in Chapter 3 of the existing Operating, Maintenance and Safety Manual. Once the existing network has been pressurized, the following steps are required to commission the E R M extension: •

At tie-in point T44-125, remove the blind (if installed).

•

Ensure all users of instrument air in the new section are closed off.

•

Notify GASCO Operations that the new systems are ready to be commissioned.

•

Slowly open the valve at the tie-in point.

•

Pressurize the new instrument air header.

CHAPTER 3




Slowly open the users one by one and check with Operations to ensure the pressure in the main header does not drop. If the instrument air header remains at its original pressure, then the instrument air system is in service.

4.2

Plant Air Plant air is used at the new utility stations. The plant air system is normally pressurized so it can be used when required. The plant air system is blown clean with plant air. After the shutdown, the new plant air system will be commissioned along with the existing system. The following steps are required:

4.3

•

Check that the B L valve is closed and associated blind swung closed.

•

Ensure that all drains, vents, and connections to atmosphere are closed.

•

Ensure that the block valves at the new utility stations are closed.

•

At tie-in points T44-126 and T44-148, remove the blinds (if installed).

•

Notify GASCO Operations that the new system is ready to be commissioned.

•

Slowly open the B L valve until the pressure comes up to header pressure, then fully open the B L valve.

•

The new plant air system is in service.

Nitrogen The nitrogen system is required for the new utility stations and the nitrogen supply to the dry gas seal system of the new Propane Compressor, 44-C-202. The nitrogen for the utility stations will be in service at the restart of the existing plant. The part that feeds the Propane Compressor seal system will be blinded off and when the compressor is ready for start up this blind will be removed. NOTE: The nitrogen buffer system for the compressor must be put into operation before the lube oil pumps can be started. After the shutdown, the existing nitrogen system will be commissioned according to the procedure given in Chapter 3 of the existing Operating, Maintenance and Safety Manual. Once the existing network has been pressurized, the following steps are required to commission the E R M extension: •

CHAPTER 3

Remove the blind at tie-in point T44-124.

11




Ensure that the valves at the four new utility stations are closed (US-201, 202, 203 and 204) Notify GASCO Operations that the new system is ready to be commissioned. Pressurize the new nitrogen extension by slowly opening the valve in line 44-2051-N22"-13091. Close the main valve and depressurize the new system to approximately 0.1 barg using the utility stations. Repressurize the system following the above instructions. Repeat these steps until the header contains less than 0.1 vol% oxygen. The new nitrogen system is now in service.

4.4

Saturated Low Pressure Steam Saturated low pressure steam is used at the new utility stations and as heat tracing for the seal gas lines to the new Propane Compressor. The tracing steam for the seal gas piping of the Propane Compressor is required at the start up of that compressor. After the shutdown, the low pressure steam system will be commissioned along with the existing system according to the procedure provide in the existing Operating, Maintenance and Safety Manual. The following additional steps are required:

4.5

•

Ensure that the block valves at the new utility stations are closed.

•

Ensure that all steam trap block valves are open and bypasses closed.

•

At tie-in points T44-137 and T44-138, remove the blinds (if installed).

•

Notify GASCO Operations that the new system is ready to be commissioned.

•

The steam lines to the utility stations will be heated up and blown them clean.

•

Close the valves at the utility stations and keep the system pressurized.

•

The new saturated low pressure steam line is then considered in service.

Utility Water There is one service station in the extension of the compressor building that has a utility water connection. The connection will be made during the shutdown. When the connection is completed the new line will be flushed and put into service.

4.6

Fire Deluge The existing fire deluge system is extended to include new spray systems for the Cold Demethanizer Bottoms Pumps (44-P-302A/B), the Propane Compressor (44-C-202), the Cold Demethanizer Column (44-V-308) and the Propane Receiver (44-V-205).

CHAPTER 3

12



GASCO ProjectNo.: 13522102 Doc. No.: PP-AOWT-44-00-00!

The fire deluge system will be flushed before it is put into service. The existing system is live at the time the new connections are made. A spray test is conducted to demonstrate that the system is ready for operation. Each new spray system activated by manually opening the following valves: Equipment Protected 44-C-202 44-V-205 44-P-302A/B & 44-V-308

Deluge Valve DV-7401 DV-7402 DV-7403

Before opening DV-7401, ensure that the new orifice 44-FO-1411ERM has been properly installed in line 34-8002-FD-6". After the line cleaning and the demonstration spray test, the new system is considered in service.

4.7

Cold Flare and Acid Gas Flare The new flare lines must be in service after the planned shutdown. The tie-ins must be completed and blinds installed as per the marked up P&ID's included in the PreCommissioning and Commissioning Manual. The new lines in both flare systems will be nitrogen purged together with the existing flare headers according to the procedure provided in Section 3.10.3 of Chapter 3 in the existing Operating, Maintenance and Safety Manual. The new piping shall be purged to an oxygen concentration of less than 1 vol%. After the nitrogen purge, the flare lines are commissioned according to the procedure provided in the existing manual (Section 4.1.1 of Chapter 3).

4.8

Closed Drain Cryogenic The new CDC lines must be in service after the planned shutdown. The tie-ins must be completed and blinds installed as per the marked up P&ID's included in the PreCommissioning and Commissioning Manual. The new CDC lines will be purged together with the existing CDC headers according to the procedure provided in Section 3.10.3 of the existing Operating, Maintenance and Safety Manual. The new piping shall be purged to an oxygen concentration of less than 1 vol%. After the nitrogen purge, the flare lines are commissioned according to the procedure provided in the existing manual (Section 4.1.2 of Chapter 3).

CHAPTER 3

13



5.0


FINAL PREPARATION IN PHASE 1 PRIOR TO FEED-IN Once the E R M tie-ins are complete, Unit 44 will be re-started. The majority ofthe start-up procedure outlined in Chapter 3 of the existing Operating, Maintenance and Safety Manual is valid for the Phase 1 start-up. The minor changes are described in this section.

5.1

Dehydration Section Pressurization of Gas Dehydration Section No changes. Refer to Chapter 3, Section 5.2.1 ofthe existing manual. Pressurization of Gas Cooling and Filtration Section No changes. Refer to Chapter 3, Section 5.2.2 of the existing manual. Feed Gas Dehydrators Initial Regeneration No changes. Refer to Chapter 3, Section 5.2.3 ofthe existing manual.

5.2

NGL Recovery Section The new E R M equipment will be dried out and pressurized with the existing unit as described below. nd

2 Feed Chiller (44-E-318): The tube side ofthe exchanger is dried and pressurized with 44E-306 in Step b ofthe procedure provided in Chapter 3, Section 5.2.5.2 of the existing manual. Cold Demethanizer (44-V-308): The column is dried and pressurized with 44-V-306 in Step d ofthe procedure provided in Chapter 3, Section 5.2.5.2 of the existing manual. Debutanizer Trim Condenser (44-E-406) and NGL Subcooler (44-E-407): The tube side of the exchanger is dried and pressurized with Debutanizer system in Step i of the procedure provided in Chapter 3, Section 5.2.5.2 of the existing manual.

5.3

Refrigeration Section There are no changes to the start-up procedure for the existing refrigeration system. The E R M Refrigeration is not started-up in Phase 1.

CHAPTER 3

14


6.0



PHASE 1 START-UP The modifications implemented in Phase 1 do not change the start-up sequence defined in the existing manual in Section 6.0 of Chapter 3. Unit 44 will start-up in C3 mode operation. Once the unit is stabilized, the operating parameters are adjusted to increase ethane recovery using the procedures provided in Chapter 11 of the existing manual. The new E R M equipment commissioned in Phase 1 will operate as follows: nd

2 Feed Chiller (44-E-318): Feed gas flows through the tube side ofthe exchanger. No cooling is achieved because the ERM refrigeration system is not in service. Cold Demethanizer (44-V-308): The overhead vapor from V-306 passes through V-308. No mass transfer occurs because there is no flow of liquid to the top of the column. No liquid is sent to the tower in Phase 1. A small amount of liquid entrainment from V-306 to V-308 is expected. However, the vapor velocity at the top of V-306 is significantly below the allowable velocity required for good vapor/liquid separation. V-306 also has a demister pad. The demister will coalesce any liquid entrained with the vapor and prevent it from being carried over to the new column. The new Cold Demethanizer has also been designed with a large liquid holdup volume in the bottom of the tower. Based on the large available volume and the very small expected liquid particle size, it would take many, many months before the liquid would build up to the level of the vapor inlet nozzle. Since the new Cold Demethanizer will only operate in Phase 1 without the bottoms pumps for approximately 2 months, this is not a valid concern. Even in the very unlikely event that liquid does accumulate in 44-V-308, the column could be intermittently drained to the CDC system during the Phase 1 operating mode. The CDC is open to the Cold Flare System. There are two locked open valves in the main CDC header to the flare. As long as these valves are not closed when the column is drained, there is no way the CDC system can be over pressurized. If the new column had to be drained, procedures would be in place to ensure that the CDC header valves were open and that the 3" V-308 drain valve was only slowly cracked open. The 3" valve is a globe valve, so it is possible to throttle and control the flow. Because the column can be drained very slowly, the built-up back pressure in the CDC system will not come near to the 7.0 barg design pressure. The drain valve would be closed during normal operation and only used if the liquid level built up to the high level. The liquid level in V-308 can be monitored in Phase 1 using L G 2125 and LI-2126. Debutanizer Trim Condenser (44-E-406): Liquid from 44-E-402 flows through the tube side ofthe exchanger. No cooling is achieved because the E R M refrigeration system is not in service. N G L Subcooler (44-E-407): Liquid from 44-P-401A/B flows through the tube side ofthe exchanger. No cooling is achieved because the E R M refrigeration system is not in service. The new controls and instruments will operate as follows:

CHAPTER 3

15




44-LV-2035: The disk stack of the existing valve is modified to increase the capacity of the valve (larger Cv). The valve will operate at a lower percentage open. 44-PV-3058: The valve trim is modified to increase the capacity ofthe valve (larger Cv). The valve will operate at a lower percentage open. 44-XV-9080: The new ESD valve will be forced open. The new Triconex system is not activated in Phase 1. Low temperatures are not a concern during the Phase 1 operation because the new refrigeration system is not started up. 44-PIC-3064: The new Debutanizer pressure control scheme works as follows: •

If the tower pressure falls, PV-3064 will open. The hot vapor will warm-up the surface of the liquid in 44-V-402, increasing the vapor pressure in the drum. This will cause liquid to accumulate in 44-E-402. Once enough surface area has been flooded with liquid, the system will reach a new equilibrium and the bypass will close.

•

If the tower pressure is too high, the bypass will close. The pressure in 44-V-402 will fall and liquid will move out of 44-E-402 into the drum. This will expose more surface area and the tower pressure will reduce.

At low ambient temperatures, the pressure in the Debutanizer will tend to decrease as the condensation temperature decreases. NOTE: Ifthe hot vapor bypass valve goes fully open and the pressure continues to fall, the louvers on 44-E-402 should be partially closed. 44HIC-9092 can be used for this purpose. The louvers should be closed slowly until the Debutanizer pressure stabilizes. 44-HS-5056: The new refrigeration system will not be commissioned in Phase 1. Therefore, the new hand switch will pass the signal from TIC-5056 through to PIC-3630 so that the temperature of 44-V-301 can be controlled. 44-TIC-5068/44-LY-2044A: The existing DCS temperature indicator (TI-5068) is being converted to a controller. A new minimum select is also being added to the V-304 level control loop. If the shell side outlet temperature of E-314 begins to fall and approach the system limits, the temperature controller will begin to throttle back the flow of cold liquid from V-304. This new functionality will be active during Phase 1. 44-LY-2044C: The new vent solenoid added in the LIC-2044 control loop cannot be used because the Triconex is not activated in Phase 1. There will be no impact on the operation of LV-2044. 44-FIC-1048: A new temperature correction will be used by the existing flow controller. TI5121 will be used instead of TI-5105. In the Phase 1 operation, the process temperature at TI5121 will be identical to TI-5105 so there is no impact on control.

CHAPTER 3

16


7.0



PREPARATION PRIOR TO INITIAL PHASE 2 OPERATION The following procedures outline a suggested method for air purging the new sections prior to the Phase 2 start-up. There are other suitable options. The procedures given here should be used only as a guide and subject to further development at site.

7.1

Preparation of the ERM Refrigeration System This section includes 44-V-205, 44-V-206, 44-V-207, 44-E-203,44-E-204, 44-E-205, 44-E318, 44-E-406, 44-E-407 and 44-C-202. Check and ensure that the following essential equipment is in the correct position/status: •


•


•

The relevant valves have been locked open or. closed according to their normal positions shown on the P&ID's

•


«


•

A l l control valves are in manual mode. See Table 7.1.2 for the correct position of the valves

o

The ESD systems are functional. A l l on-off shutdown valves are closed.

Table 7.1.1 A l l manual valves are in their normal operating positions except for the following: VALVE NO.

FUNCTION C3 make-up

P&ID NUMBER 22717-104

POSITION Closed

LINE NUMBER 10"-P-44C202-2

P&ID NUMBER 22717-103

POSITION Open

8"-P-44C202-2

22717-102

Open

v

44-00-30-041

Closed

;

44-00-30-019-2

Closed

v

44-00-30-028-1

Closed

44-00-30-028-3

Closed

LINE NUMBER 2"-P-FILL

Table 7.1.2 The positions ofthe control valves are as follows:

44-HV-9092

FUNCTION 2 Stage Anti-surge I Stage Anti-surge E-203 Vent

44-LV-2111

44-E-318 Level

44-LV-2116

44-E-406 Level

44-LV-2121

44-E-407 Level

VALVE NO. 44-FV-1402 44-FV-1403

CHAPTER 3

nd

st

44-2037-RF-2 31170 44-2007-RF-4' 31170 44-2024-RF-6 31170 44-2034-RF-3"-

17


V A L V E NO.

FUNCTION

44-LV-2404


P&ID N U M B E R

POSITION

44-E-204 Level

LINE N U M B E R 31170 6"-P-44V205-l

22717-103

Closed

44-LV-2405

44-E-205 Level

3"-P-44E204-l

22717-102

Closed

44-PV-3402A

44-V-206

18"-P-44V206-1

22717-103

Open

44-PV-3402B

44-V-207

18"-P-44V207-1

22717-102

Open

44-PV-3410A

4"_P-44C202-3

22717-104

Closed

44-2065-RF-2"31170 3"-P-44E205-2

22717-104

Closed

44-TV-5404

44-E-203 Hot Vapor Bypass 44-V-205 vent to flare 2 ^ Stage Quench

22717-103

Closed

44-TV-5405

1 Stage Quench

3".p-44205-3

22717-102

Closed

44-PV-3410B

7.2


51

Preparation of the Cold Demethanizer Bottoms Pumps This section includes 44-P-302A/B. Check and ensure that the following essential equipment is in the correct position/status: •


•

A l l instruments are open

•


•

A l l bypasses of control valves are closed.

•

A l l control valves are in manual mode. See Table 7.2.2 for the correct position ofthe valves

•

The ESD systems are functional. A l l on-off shutdown valves are closed.

Table 7.2.1 A l l manual valves are in their normal operating positions except for the following: V A L V E NO.

FUNCTION 44-P-302A suction 44-P-302B suction 44-P-302A/B vent 44-LV-2126 downstream 44-FV-1070 upstream

CHAPTER 3

LINE N U M B E R 44-2014-HC-12" 33450-C 44-2014-HC-3" 33450-C 44-2015-HC-2' 33450-C 44-2015-HC-8' 33450-C 44-2016-HC-4 33450-C

P&ID N U M B E R 44-00-30023-4

POSITION Closed

44-00-30023-4

Closed

44-00-30023-4

Closed

:

44-00-30023-4

Closed

V

44-00-30023-4

Closed




Table 7.2.2 The positions of the control valves are as follows: VALVE NO. 44-LV-2126

FUNCTION 44.v-3 08 Level

44-FV-1070

P-302A/B Min Flow Bypass

CHAPTER 3

LINE NUMBER 44-2015-HC-8 31170-C 44-2016-HC-4" 33450-C v

19

P&ID NUMBER 44-00-30023-4

POSITION Closed

44-00-30023-4

Open



8.0


PHASE 2 PURGING The procedure defined in.Chapter 3, Section 3.0 ofthe existing Operating, Maintenance and Safety Manual should be followed for purging the new E R M equipment. The existing procedures should be augmented the procedures by contained in the E R M PreCommissioning and Commissioning Manual.

8.1

ERM Refrigeration System Subsystem 1: Purging of propane make-up line 44-2001-RF-3"-31170 Subsystem 2: Purging of 44-V-205, 44-E-203, 44-E-204 (tube side), 44-E-205 (tube side), and associated piping. Subsystem 3: Purging of 44-V-203, 44-V-204,44-E-204 (shell side), 44-E-205 (shell side), 44-C-202 and associated piping. Note: To increase the nitrogen circulation in each subsystem, it is possible to purge through additional dedicated vent valves other than those identified in the procedures below. In such a case, the oxygen content should be monitored at every vent point in the system.

8.1.1

Subsystem 1 Equipment Status: Refer to Section 7.1 of this Chapter. The subsystem is isolated by 44-033 (BL isolation valve), M-070 in line 44-0513-RF-3"-ClR, and the propane fill valve in line 2"-P-FILL-L31. The subsystem is pressurized by using the %" utility connection in line 44-0513-RF-3"-ClR. Depressurization is performed by opening the new fill valve and venting through the 3" vent on 44-V-205.

8.1.2

Subsystem 2 Equipment Status: Refer to Section 7.1 of this Chapter. The subsystem is isolated by the propane fill valve in line 2"-P-FILL-L31, 44-LV-2111, 44LV-2116, 44-LV-2121,44-LV-2404, 44-LV-2405, 44-TV-5404, 44-TV-5405,44-PV-3410B and 44-XV-7400. The subsystem is pressurized by using the 2" utility connection on 44-V-205. Depressurization is performed using the 3" vent on 44-V-205 and the 2" vent connections on 44-E-203.

8.1.3

Subsystems Equipment Status: Referto Section 7.1 ofthis Chapter. The subsystem is isolated by 44-LV-2404, 44-LV-2405, 44-TV-5404, 44-TV-5405, 44-XV7400, 44-XV-7401, 44-XV-7402 and 44-XV-7405.

CHAPTER 3

20




The subsystem is pressurized by using the 2" utility connections on 44-E-204 and 44-E-205. Depressurization is performed using the 3" vents on 44-V-206 and 44-V-207 and opening 44XV-7405.

8.2

Cold Demethanizer Bottoms Pumps The procedure below applies to the Phase 2 start-up only. For subsequent start-ups, 44-P302A/B will be purged with the Demethanizer system. Equipment Status: Refer to Section 7.2 of this Chapter. The system is isolated by the 44-P-302 A/B suction isolation valves, 44-FV-1070, 44-LV2126 and the valve in line 44-2015-HC-3/4"-33450. The system is pressurized by using the V " utility connection in line 44-2015-HC-3/4"-33450. The system is depressurized using the 1" vent valves upstream of 44-LV-2126 and 44-FV1070.

CHAPTER 3

21


Ethane Recovery Maximization (ERM) Project Operation of V-308 Bottoms Pumps, P-302A/B Rev. 0 - May 20, 2005

GASCO Project No.: 13522102

OPERATION OF V-308 BOTTOMS PUMPS P-302 A/B Rev. 0 - May 20, 2005 The loss of one V-308 Bottoms Pump, P-302, when in ERM mode, will force the Unit 44 operations to return to the 50% C2 Recovery Mode as a precaution against the potential loss of the spare operating pump. The liquid holding time in V-308 is only about 7 to 8 minutes. This means that the failure of the second pump would require the quick removal ofthe liquid feed streams from V-308. Rerouting the E-314 liquid feed stream to V-306 from V-308 can be done while operating in any mode. Removing V-307 bottoms from V-308 and routing it to E-305 cannot be done immediately in the ERM mode because the temperature of V-307 bottoms is too cold. In other lower recovery modes, the liquid from V-307 can be diverted the instant all pumping capacity is lost. The following procedure covers the potential scenarios for P-302 A/B operations. ERM MODE OF OPERATION I. Loss of One P-302 Pump while in ERM Mode 1. Place the spare P-302 pump in service. 2. Transition from the ERM Mode to the 50% C2 recovery mode. 3. V-307 bottoms will continue to be sent to the Cold Demethanizer, V-308. 4. Reroute E-314 outlet stream from V-308 to V-306 by opening valve M-4401 and closing valve M-4402.

II. Loss ofthe Second P-302 Pump (with the first one still unavailable) If the spare Cold Demethanizer Bottoms Pump fails to start on demand, it will no longer be possible to move liquid out of the Cold Demethanizer, V-308. Since the liquid in V-307 is cold, it cannot be immediately diverted to V-306. In order to the warm-up the system and allow continued operation the following actions are required:


Ethane Recovery Maximization (ERM) Project Operation of V-308 Bottoms Pumps, P-302A/B


Rev. 0 - May 20, 2005

1.

Unit Operator:

Reroute E-314 outlet stream from V-308 to V-306 by opening

valve M-4401 and closing valve M-4402. 2.

Unit Operator: Open valve to E-315 and close E-315 bypass valve.

3.

D C S Operator: Reduce flow from V-307 to a minimum to build level in V-307 and V-308.

4.

5

D C S Operator: Offload C-2o2 compressor I ' stage by closing 44-LV-2111 to E318.

5.

D C S Operator: Open EC-301 JT valves to warm-up the Recovery Tower.

6.

D C S Operator: Open FV-1203 to 100% to warm-up V-307.

7.

D C S Operator: When the level in V-308 reaches 100% close FV-1204.

8.

D C S Operator:

When the level in V-307 reaches the High High alarm point,

close FV-1041. 9.

DCS Operator:

Closely monitor the Demethanizer pressure

and

Recycle

Compressor load to ensure that they do not increase out of design limits. Adjust the flow of steam to E-308 to maintain the stability of the system. o

10. By this time, the temperature in V-307 should be above - 5 0 C crack open M4403 and close M-4404 to divert the stream to E-305. Open FV-1204. C l o s e l y m o n i t o r the overhead temperature of the Demethanizer (TIC-5081) a n d (TIo

5086) to e n s u r e that they do not fall below - 4 0 C .

If the temperatures are

within limits, slowly open M-4403 to increase the flow to V-306. 11. W h e n all of the excess liquid in V-307 and V-305 has been processed and the liquid levels are normal, close the EC-301 JT valves and transition the unit to C 2 Enhancement mode. 12. Drain V-308 level to C D C , if necessary.

OTHER MODES OF OPERATION: In other operating modes, the outlet stream from E-314 is sent to V-306, not V-308.

I. Loss of One P-302 Pump 1.

Place the spare P-302 pump in service.

2.

V-307 bottoms will continue to be sent to the Cold Demethanizer, V-308.


Ethane Recovery Maximization (ERM) Project Operation of V-308 Bottoms Pumps, P-302A/B Rev. 0 - May 20, 2005


II. Loss of the Second P-302 Pump (with the first one still unavailable) If the spare Cold Demethanizer Bottoms Pump fails to start on demand or is otherwise unavailable, it will no longer be possible to move liquid out of the Cold Demethanizer, V-308. The liquid from V-307 should be diverted to E-305. Diverting the flow of liquid from V-308 to E-305 will cause the Demethanizer (44-V-306) overhead temperature to fall. However, since the unit will be operating at a lower C2 recovery level, there is no risk of the temperature approaching the normal minimum 0

recommended value of -35 C and the switch over can be performed immediately.

1. Open M-4403.

This action will re-direct the liquid from V-307 to the existing

Demethanizer Reflux Condenser (44-E-305). 2.

Close M-4404. This action will stop the flow of liquid to the Cold Demethanizer.

RETURNING PUMPS TO SERVICE 1. When both pumps are available to be placed in service, start one pump on minimum flow recycle and place the second pump in standby mode. 2. Divert V-307 bottoms from V-306 (E-305) to V-308 (refer to the Switching procedure). 3. Return the unit to the ERM mode of operation. PUMPS P-302A/B Seal Pressure Settings •

The seal chamber pressure is estimated to be at 25.5 barg (Flowserve estimate).

•

Recommended seal system pressurization is 29.5 barg (with nitrogen to 26.5 barg and with methanol to 29.5 barg).

•

Seal Low Pressure Alarm set at 27.5 barg

•

Seal low Low Pressure Pump Shutdown at 26.5 barg.



9.0

FINAL PREPARATION IN PHASE 2 PRIOR TO START-UP

9.1

Pressurization of the ERM Refrigeration Section


The E R M Refrigeration system is pressurized using propane from Unit 45. The propane is used to displace the nitrogen in the system prior to filling 44-V-205 and starting 44-C-202. The refrigeration system is divided into two sections: Section 1:

44-V-205, 44-E-203, 44-E-204 (tube side), 44-E-205 (tube side), E-318, 44E-406, and 44-E-407

Section 2:

44-V-206, 44-V-207, 44-E-204 (shell side), 44-E-205 (shell side), 44-C-202

The sections are separated by 44-XV-7400, 44-XV-7401, 44-XV-7402, 44-LV-2404, 44-LV2405, 44-TV-5404 and 44-TV-5405. 9.1.1

Pressurization of Section 1 Line up section 1 as follows: «

Open all inlet and outlet valves on 44-E-203

•

Open bypass of 44-LV-2111 so that 44-E-318 can be pressurized

•


•


»

Open upstream/downstream valves of 44-PV-3410B and close bypass

•

Open upstream/downstream valves of 44-HV-9092 and close bypass

•

Check that the nitrogen pressure is not greater than 0.1 barg in the system

•

Check that the propane fill globe valve in line 2"-P-FILL is closed

The material of construction for the refrigeration system lines and equipment is Low Temperature Carbon Steel. The system has a cold design temperature of-45 C. During the pressurization/filling operation, flashing liquid propane could lead to a temperature very close to the design temperature. Therefore, the propane loading steps should be performed in such a way as to minimize the liquid propane flashing. Care should also be taken to avoid placing any undue stress on the equipment and piping while at the cold temperatures. 0

Open blind B-033 and slowly open manual battery limit valve 44-033. Crack open the 2" globe valve and pressurize the system to 3 barg. The pressure can be monitored using 44PIC-3410, 44-PI-3411 and 44-PI-3412. The propane transfer pumps (45-P-503A/B) do not need to be started for this initial pressurization. Monitor the level in 44-V-205 using 44-LG2413 and 44-LI-2403 to ensure that the vessel is not overfilled. When 3 barg is reached, close the 2" fill valve and allow the system to warm-up to ambient temperature. Vent the system the following all high points to purge the nitrogen:

CHAPTER 3

22



• • • •


44-HV-9092 bypass valve of 44-PS V-8403 A/B on 44-V-205 bypass valve of 44-PS V-8410 A/B on 44-E-318 bypass valve of 44-PS V-8412 A/B on 44-E-406/7

Depressurize the section down to 0.1 barg. Repeat the pressurization/depressurization steps 4 times. Once the section has been completely purged of nitrogen, pressurize again and allow the section to maximum pressure. The maximum pressure will depend on the ambient temperature. Monitor the pressure using 44-PIC-3410. Once the pressure is stable, close the bypass valve around 44-LV-2111, 44-LV-2116 and 44LV-2121. Transfer liquid propane from Unit 45 by starting pump 45-P-503 A or B. Open the 2" globe valve and fill 44-V-205 to 30% level on 44-LI-2403. The level can monitored locally using 44-LG-2413. 9.1.2

Pressurization of Section 2 Before pressurizing the compressor section, first check that the buffer and seal gas systems are commissioned. «

Ensure that seal gas flows (nitrogen) to the compressor is established with the following readings: 44-FIC-1431 = 1.7 m3/h 44-FG-1436= 1.7 m3/h

•

Ensure that the buffer gas flow (nitrogen) to the compressor is established with the following reading: 44-PI-3433 = 1.4 barg 44-FI-1437 = 3.4 m3/h 44-FI-143 8= 1.7 m3/h 44-FI-1439= 1.7m3/h

Ensure that 44-XV-7405 is closed. Crack open the bypass valve around 44-LV-2405 to pressurize the section to 3.0 barg. The pressure can be monitored using 44-PG-4402, 44-PG-4405 and 44-PG-4406. When 3 barg is reached, close the bypass valve and allow the system to warm-up to ambient temperature. Vent the system the following all high points to purge the nitrogen: • •

CHAPTER 3

bypass valve of 44-PS V-8400 A/B on 44-C-202 discharge bypass valve of 44-PSV-8401 A/B on 44-V-206

23



•


bypass valve of 44-PS V-8402 A/B on 44-V-207

Depressurize the section down to 0.1 barg. Repeat the pressurization/depressurization steps 4 times. Once the section has been completely purged of nitrogen, pressurize again to about 5.0 barg.

9.2

Filling 44-V-205 •

Open the 2" globe valve in the propane filling line.

•

Start the transfer pump 45-P-503 A or B and fill 44-V-205 to 90% level on 44-LI-2403.

•

Stop the pump and close the fill valve

At this stage, the refrigerant loop is ready for start-up.

9.3

Pressurization of Cold Demethanizer Bottoms Pumps The new flammable gas detectors at the pumps should now be checked and working properly. With the Cold Demethanizer (44-V-308) pressurized and in operation, the blinds that were installed for the Phase 1 separation must be removed. Be aware valves do leak and extreme care must be taken when removing these blinds. •

Check ifthe purging and tightness testing of the pump circuits was completed and the fine mesh suction strainers are installed.

•

A l l drain and vent valves are closed, the seal system is charged.

•

A tightness test shall be done after the removal of the spades to ensure that the flanges that are opened are tight. This tightness test will be done using nitrogen to save time. The oxygen content in the newly commissioned part shall be checked, since there will be ingress of oxygen during the removal ofthe blinds.

•

If the oxygen content in the whole system is less then 0.5% oxygen the circuits are safe to receive hydrocarbons.

•

NOTE: The pumps will be started up at low temperatures so the system must also be very dry to avoid hydrate formation during start-up.

To pressurize the pumps, slowly open the 2" ball valve in the pump vent line (44-2015-HC2"-33450). Check the pressure using 44-PG-4111 A/B and 44-PG-4112A/B and check for leaks using a soap solution or portable gas detector. If no leaks are found, open the suction valves ofthe pumps. 44-XV-9081 and 44-LV-2126 should still be closed at this time.

9.4

Liquid Fill the Cold Demethanizer and the Bottoms Pumps 44-P-302A/B In order to establish a liquid level in the Cold Demethanizer 44-V-308, the feed line to the column will be commissioned.

CHAPTER 3

24




Redirect slowly a portion ofthe feed flow 44-V-307fromthe Demethanizer Column 44V-306 to the Cold Demethanizer Column 44-V-308 by slowly opening manual valve M 4404 (See P&ID 44 00 30023/1). The operation of the Demethanizer Column shall not be disturbed. Level controller 44-LIC-1204 will maintain the level in 44-V-307. Slowly fill up the Cold Demethanizer. Open 44-XV-9081. Leave the suction valves to the two Cold Demethanizer pumps open in order to fill them at the same time the column is filled. Also ensure that the W equalizing lines from the pump discharge lines to the column are open. Monitor the level in the Cold Demethanizer using 44-LG-2125 and in the control room by 44-LT-2126. Check the local level reading with the DCS reading and adjust the DCS reading if required. When the level in 44-V-308 reaches 50%, close manual valve M-4404. The pumps are filled and gas free. The discharge valves are still closed.

CHAPTER 3

25



10.0


P H A S E 2 START-UP Once the above Phase 2 pre-startup steps have been completed, the E R M systems are ready to be commissioned.

10.1

Cold Demethanizer Bottoms Pumps Start-up The first activity will be the test running of the Cold Demethanizer Bottom Pumps 44 P302A/B by circulating bottom product back to the Cold Demethanizer. Each pump will be run for two hours and the temperatures, pressures, flows and integrity of the seals will be checked. T

The procedure outlined below should be followed in conjunction with recommendations contained the pump vendor's Installation, Operation and Maintenance Manual (document no OHH OPN 0402). •

Check the level in the Cold Demethanizer. The level should be at least 50%.

•

Open the minimum flow control valve 44-FV-1070, set the flow controller at 260 m3/hr.

•

Get the electrical department to energize the pump. Refer also the rotating equipment testing procedure in the Pre-commissioning and Commissioning manuals.

•

Start the pump and check the rotation direction, check the discharge pressure with the discharge valve still almost closed. When the discharge pressure is established, slowly open the discharge valve. The pump's amp meter must be monitored. As soon as the amp meter drops below the red indication, the discharge valve can be fully opened.

•

Run the pump with the-flow-controller-44-Fie-1070-at-260-m3/hr-for-two-hours-and-take— readings every 30 minutes as per the agreed log sheet.

•

In case of any abnormal noise or out of the ordinary readings, stop the pump immediately and inform Fluor's mechanical engineer for further action.

•

Perform this test run for both pumps and leave one pump in operation.

Once the pump is operating normally, the following steps are required to integrate the new pump into the Unit 44 operation: •

Reduce the set point of 44-FIC-1070 to 80 m3/hr.

•

Open manual valve M-4404 and close manual valve M-4403.

•

Place the Cold Demethanizer level controller (44-LIC-2126) in auto.

The integration of the pump will not have a significant impact on operating conditions of the rest of Unit 44. The main change will be the increased overhead temperature of the Demethanizer (44-V-306). Product recoveries in Unit 44 will not be affected.

CHAPTER 3

26



10.2


Propane Compressor Start-up

10.2.1 General Infonnation The procedures presented in this section are intended to be a guideline for the start-up of 44C-202. For more detailed information about the compressor and its auxiliary systems, refer to the vendor installation, operation and maintenance manuals. Overall Refrigeration System: Compressor: Electric Motor: Anti-surge & Performance Controls:

Toromont Process Systems GE Oil and Gas (AC Compressor) GE CCC

The functional test of the overall control and protection instrumentation must be successfully completed before the start up of the compressor can be initiated. The vendor representatives of all these suppliers will be present during the functional test as well as for the initial start up. The following vendor representatives will be on site: a) General Electric b) Toromont c) C C C d) A B B Automation The start-up sequence will be performed in the following sequence: •

Buffer and Seal Gas System Commissioning

•

Lube Oil System Commissioning

•

Motor Purging and Cooling

•

Compressor Start-up

10.2.2 Buffer and Seal Gas Systems •

Ensure that seal gas flows (nitrogen) to the compressor is established with the following readings: 44-FIC-1431 = 1.7 m3/h 44-FG-1436= 1.7m3/h

•

Ensure that the buffer gas flow (nitrogen) to the compressor is established with the following reading: 44-PI-3433 = 1.4 barg 44-FI-1437 = 3.4 m3/h 44-FI-1438 = 1.7m3/h 44-FI-1439 = 1.7m3/h

CHAPTER 3

27





10.2.3 Lube Oil System Once the seal gas systems have been properly commissioned and the lube oil system has been properly flushed, the lube oil systems can be commissioned. Refer to the lube oil flushing procedure for details. •

Place the local selectors in the following positions: 44-C-202 PIMA: 44-C-202 P1MB:

HAND OFF

•

Check the lube oil tank level (44-LG-2430), oil temperature (44-TG-6432) and setting for the lube oil tank nitrogen blanketing.

•

Check that the lube oil system's valves are in their correct open or closed positions.

•

Check the line up to 44-C-202 E l and start the aircooler fans.

•

Start 44-C-202-P1A locally.

•

Check the pressure profde in the system.

•

Fill the overhead rundown tank (44-C-202-TK2) using the check valve bypass valve. Verify TK2 is overflowing using the local sight glass (44-FG-1425).

•

Verify annunciator 44-XL-9478A is lit.

•

Switch 44-C-202 P1 MB to AUTO.

10.2.4 Motor Purging and Cooling The main compressor drive motor includes a purge system to enable the motor to operate in the classified area. Prior to energizing the main motor start relay, the motor must go through a purge cycle to evacuate any explosive gas from the intemals of the motor. Instrument air is used as the purge medium. The local "Main Purge Switch" is manually closed to start the purge cycle. The purge controller automatically runs through the purge cycle, which lasts about 25 minutes. After completion ofthe start-up purge, the controller keeps the motor pressurized. The "Motor Ready to Start" contact XS-9560 is used in the compressor start-up permissive logic. The status ofthe purge can be monitored using the following: •

XL-9460A: Purge Complete

•

XL-9460B: Purge in Progress

•

XL-9460:

Motor Ready to Start

The motor is cooled using an Air to Air cooling arrangement. Three 50% blowers are provided.

CHAPTER 3

28



•


Place the local selectors in the following positions:

44-C-202 BL1MA: HAND 44-C-202 BL1MB: HAND 44-C-202 BL1MC: OFF •

Start 44-C-202-BL1A and B locally.

•

Check that air pressure has been established using 44-PDI-3425.

•

Switch 44-C-202 BL1MC into AUTO.

2 out of 3 blowers must be operating in order for the main motor to start.

10.2.5 Compressor Start-up The following permissives must be satisfied before the compressor can be started: •

Air motor purge complete (XS-9460)

•

Lube oil pressure not low (PAL-3421 not active)

•

Lube oil rundown tank level high (LAH-2420 active)

•

Lube oil supply temperature not low (TAL-5416 not active)

•

Lube oil fans running (XS-9476A/B/C, 2 out of 3)

•

Motor blowers running (XS-9477A/B/C, 2 out of 3)

•

Compressor discharge ESD valve open (XZSO-7400)

•

Compressor side load ESD valve open (XZSO-7401)

•

Compressor suction ESD valve open (XZSO-7402)

•

1 section anti-surge valve open (FZSO-1403)

•

2 section anti-surge valve open (FZSO-1402)

•

Depressuring valve closed (XZSC-7405)

•

Reset HSR-9455 in DCS

•

Activate HS-9452 in DCS. This will authorize the start of the compressor motor locally.

a.

Prior to starting the compressor, ensure that the compressor casing and suction lines have been drained to the CDC to ensure that any liquid condensed is removed.

b.

When XV-7400, XV-7402 and XV-7403 are opened, the compressor section will be fully pressurized. Low-low shutdowns PALL-3404 and PALL-3405 should not be active.

c.

Check that the anti-surge and performance controllers are in AUTO.

d.

Check that the Propane Condenser (44-E-203) fans have been started.

CHAPTER 3

st

nd

29



10.3


e.

Give notice to the proper GASCO department(s) and start the motor using the local push button. Check the rotation.

f.

The compressor will operate in full recycle (no process load). The level controllers at the new process exchangers (44-E-318, 44-E-406 and 44-E-407) will remain closed.

g.

Take readings of all the flows, pressures, temperatures as recommended by the vendor. Check the circuit for leaks; check the seal flows and the correct functioning of the lube oil system.

h.

After the flows, pressures and temperatures have stabilized, run at least for another two hours to ensure that the circuit is stable and sufficient data is collected to evaluate the compressor's performance.

Transition to ERM Mode This procedure assumes that Unit 44 is miming in C2 Enhancement Mode (20% C2 recovery) at steady state conditions. It also assumes that the new refrigeration package (44ME-201) is started-up and running in recycle at no process load. General Overview The operating conditions of the Debutanizer will be changed first to ensure that the overhead product is totally condensed and to avoid venting of light ends from the accumulator. The operating conditions of the Demethanizer will be adjusted before changing the temperature profile around the cold boxes to avoid overloading the recycle compressor loop. Stepwise Instmctions • Ensure that the Debutanizer is fed above tray 23. Gradually increase the column pressure to 18.5 barg (PIC-3068), simultaneously increase the set point of TIC-5099 to 156 C, and start to reduce the reflux flow rate. The target is around 10 m3/h. Do not proceed further until the column is stabilized. Closely monitor the C5+ content ofthe NGL to ensure it stays on specification. The C5+ constraint may limit the reduction of the reflux flow rate. 0

•

Start to reduce the heat input to the Demethanizer by throttling TV-5088B at 44E-307 outlet. Decrease slowly the set point of TIC-5082. The temperature should be lowered from about 55 C to 28 C. Closely monitor the level on the steam condensate side ofthe Demethanizer Reboiler (44E-308). If the level rises too high, decrease the set point on TIC-5088 (side reboiler retum) and/or reduce the steam pressure with PIC-3076. 0

0

•

The C2 content of the NGL should begin to increase. Monitor flow from the Demethanizer via FIC-1042 and NGL composition using AI-7094A. Begin raising the level of propane refrigerant in the Debutanizer Trim Condenser (44E-406). 44-LIC-2116 should be in manual. Monitor the position of PV-3068 (vent to flare) to ensure the level is high enough to totally condense the overhead product.

•

Begin introducing propane refrigerant into the NGL Subcooler. Place 44-LIC-2121 in manual and slowly open 44-LV-2121. Once the level reaches normal, place the controller in auto.

CHAPTER 3

30




Open the new recycle gas bypass around 44-E-315 (manual valve M-4405) and close the inlet isolation valve M-4406. Open the new recycle gas bypass around 44E-303. Once the temperature/pressure profiles in the Demethanizer system has stabilized, gradually reduce the temperature in 44V-301 from - 9 C to -22 C. This is achieved by increasing the level in E-318 using LIC-2 111. Keep the existing refrigeration package in a base loaded condition (speed is fixed using HIC-7201/HS-5056). The temperature of the 44-V-303 should be monitored closely in conjunction with the temperature of 44-V301. 44-V-303 is constructed of LTCS and has a cold design temperature of -45 C. The expected temperature in C2 recovery mode is -31 C. NOTE: This temperature should be maintained above -35°C to ensure that the temperature at the outlet of the 44-V-303 level control valve (44-L V-2040) does not f a l l below -45°C. A new temperature indicator (44-TI-5131) with a low temperature alarm has been provided at the outlet of 44-LV-2040 to alert the Operators of low temperatures. 0

0

0

0

0

0

Reduce the operating temperature in 44-V-302 from -31 C to -42 C. This is achieved by adjusting the set point of TIC-5058. 0

0

Reduce the set point of TIC-5207 (44-V-307 overhead) from -51 C to -58 C. 0

o

Reduce the set point of TIC-5080 (44-V-305 bottoms) from -58 C to -60 C. Keep the isolation valve on the liquid line to 44-E-303 closed. 0

Reduce the set point of TIC-5054 (residue gas from 44-E-301) to 22 C. When the ethane recovery level increases to about 30%, re-route the stream from 44E-314 to the new Cold Demethanizer (44-V-308) by opening manual valve M-4402. Close manual valve M-4401 in the line to 44-V-306. Change the set point of TIC-5212 to 53 C. This will begin steam flow to the Debutanizer Feed Preheater (44-E-405). 0

Once all the controllers have reached the set points listed above, the unit should stabilize at the following conditions: _> 44-V-301 at -22°C 0

44-V-302 at -42 C o

44-V-305 bottom temperature at -60 C 0

o

-» 44-V-306 top / bottom temperatures are -18 C and 50 C 0

0

44.V-401 top / bottom temperatures are 72 C and 177 C 0

_> 44-V-402 at 29 C Once the system has stabilized, HS-5056 should be positioned such that temperature of 44-V-301 is maintained by adjusting the load of existing refrigeration system via TIC5056. The new refrigeration package should be based loaded (fixed level set point for 44LIC-2111).

CHAPTER 3




Once the system has stabilized, the anti-surge valves for the new Propane Compressor should be closed (44-FV-1402 and 44-FV-1403 at 44-C-202). If not, the following steps are recommended: a. ) Increase the load on 44-E-406 by decreasing the duty of the upstream aircooler (44-E402). b. ) Increase the load on 44-E-318 by decreasing the duty ofthe upstream exchanger (44E-306) or by slightly opening the warm feed gas bypass valve M-052.

CHAPTER 3

32




CHAPTER 4

N O R M A L START-UP

CONTENTS

SECTION 1.0

2.0

PAGE

GENERAL

2

1.1 1.2 1.3

2 3 3

Stepl Step 2 Step 3

CONTROLLER SETPOINT, A L A R M AND TRIP SETTINGS

4

2.1 2.2

4 2

CHAPTER 4

Existing Controls Modified for E R M Operation New Controls Added for ERM Operation


1.0



GENERAL The unit will be started up using the normal start up procedures described in the following: •

Chapter 4 of the existing Operating, Maintenance and Safety Manual

•

Section 6 of Chapter 11 of the existing Operating, Maintenance and Safety Manual (C2 Enhancement Addendum)

•

Chapter 3 of the E R M Operating, Maintenance and Safety Manual

Using the above referenced procedures, Unit 44 will normally be started up in the following sequence:

1.1

•

Step 1: C3 mode + E R M Phase 1

•

Step 2: Transition to C2 Enhancement mode

•

Step 3: Transition to ERM mode (ERM Phase 2)

Step 1 In a normal start-up (i.e. all start-ups after the initial start-up), the E R M Phase 1 equipment will be prepared, purged, dried, pressurized and started up along with the existing systems. nd

2 Feed Chiller (44-E-318): The tube side ofthe exchanger is dried and pressurized with 44E-306 in Step b ofthe procedure provided in Chapter 3, Section 5.2.5.2 ofthe existing manual. Cold Demethanizer (44-V-308): The column is dried and pressurized with 44-V-306 in Step d of the procedure provided in Chapter 3, Section 5.2.5.2 of the existing manual. Debutanizer Trim Condenser (44-E-406) and NGL Subcooler (44-E-407): The tube side of the exchanger is dried and pressurized with Debutanizer system in Step i of the procedure provided in Chapter 3, Section 5.2.5.2 ofthe existing manual. The Cold Demethanizer Bottoms Pumps should also be prepared, purged, pressurized and dried along with the Cold Demethanizer as a part of Step 1. The pumps will not be started until Step 3. Refer to Chapter 3 of this manual for more information. For a normal start-up, separation blinds will not be required to isolate the Phase 2 systems from the rest of the plant.

CHAPTER 4


A

1.2



Step 2 Using the procedure contained in the C2 Enhancement Addendum, the unit is transitioned to C2 Enhancement mode.

A

1.3

Step 3 Once the unit is operating stably in C2 Enhancement mode, the Cold Demethanizer Bottoms Pumps can be started. Refer to the procedure in Section 10.1 of Chapter 3 for more information. The E R M refngeration system is prepared, purged, pressurized and start-up according to the procedures contained in Chapter 4 of this manual. This procedure can also be selective applied for re-starts of the E R M refrigeration system after trips. Once the E R M refrigeration system is operating smoothly in recycle, the unit can be transitioned to the E R M operating mode using the procedure in Section 10.3 of Chapter 3.

CHAPTER 4



2.0

CONTROLLER SETPOINT, ALARM AND TRIP SETTINGS

2.1

Existing Controls Modified for ERM Operation

2.1.1

Setpoints and Alarms


The E R M Project does not impact the existing Dehydration System or the existing Refrigeration System. Therefore, there are no changes to the controller set points or alarms shown in the following P&ID's: 44-00-30001 44-00-30002 44-00-30003 44-00-30004 44-00-30005 44-00-30007

44-00-30008 44-00-30009 44-00-30014 44-00-30015 44-00-30016 44-00-30017

The changes to the existing controller set points and alarms for the P&ID's listed below are summarized in Table 2.1. 44-00-30018 44-00-30019- 1 of 2 44-00-30019-2 of 2 44-00-30020 44-00-30021 44-00-30022 44-00-30023 - 1 of4 44-00-30023-2 of 4 44-00-30023-3 of 4 44-00-30023-4 of 4 44-00-30024 44-00-30025 44-00-30026 44-00-30027 44-00-30028- 1 of 3 44-00-30028- I of 3 44-00-30028- 1 of 3

2.1.2

Trips No changes to existing trip settings are required.

CHAPTER4

FLUOR Conlract AOWT Rev. 0. 23-Sept-04

GASCO Ethane Recovery Maximization Project 5221

TABLE 2.1 - UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)

Alarms

Operating Mode Description

Tag Number

P&ID

TIC-5054

018

ERM Case

30% C2 20% C2 10% C2 C2 Recovery Recovery Recovery Rejection

High

Comments

Low

TEMPERATURE Residue Gas to E-309 LP Recycle Gas from E-301 V-301 Temperalure Feed Gas from E-301

018

22

23

18

22

22

30

New conlrol selpoinl. New TAL selpoinl. Currenl TAL = -19.

TIC-5056 TI-5057

018

-23

-20

V-302 Temperature Feed Gas from E-302

TI-5059

HP Recycle Gas from E-302

TI-5060


TI-5075


TI-5118

Feed Gas from E-313

018

-38

-60

-58

-55

-56

018

-42

-38

-32

-31

019

-35

-28

019

Feed Gas from E-306

TI-5063

019

V-304 Temperature

TI-5065

020

2nd Stage Liquid lo E-314

TI-5066

020

TIC-5067

020

2nd Stage Liquid from E-314

TI-5068

020

-28

-24

EC-301(Expander) Outlei

TI-5070

021

-60

-56

021

-40

New control setpoint. New TAL setpoint. Current TAL = -30.

-55 -62

-57

-53

-54

63

-50

-51

52 64

-35

New TAL setpoint.

-36

-65

New TAL selpoinl. Currenl TAL = -58.

62

42

-18 -53

64

New conlrol setpoint.

-15

-34

53 TI-5113

New control setpoint. New TAL setpoint. Current TAL = -37.

-36

018

EC-301 (Compressor) Inlet

-17

-32

TI-5062

EC-301 (Compressor) Outlet

-35

-42

1st Stage Liquid from E-313

Feed Gas from E-314

New control setpoint.

64

64

FLUOR Contract AOWT Rev. 0, 23-Sept-O'f




Tag Number

P&ID

Units

ERM Case

Residue Gas from E-311

TI-5073

021

•C

54

V-30S Overhead

TI-5076

022

•C

022

•C

-60

022

•c

-42

Reboiler Retum HP Recycle Gas fram E-303

TI-5078

V-305 Tray 11

TI-5079

V-305 Bottoms

TIC-5080

022

V-306 Overhead

TIC-5081

023 1/3

V-306 Tray 2

TIC-5082

023 1/3

V-306 Reboiler Draw

TI-5083

023 1/3

V-306 Reboiler Return

TI-5084

023 1/3

V-306 Overhead lo E-305

TI-5085

023 1/3

Alarms

30% C2 20% C2 10% C2 C2 Recovery Recovery Recovery Rejection 54

54

-61

60

-38

54

54

55

-53

-12

•35

-32

-31

High

Comments

65

60

42

•C

V-305 Bottoms from E-317

TI-5205

023 3/3

Feed Gas from E-317

TI-5206

023 3/3

V-307 Ovhd Temperature

TIC-5207

023 3/3

V-306 Side Reboiler Outlet

TIC-5088

024

Recycle Gas from E-307

TI-5089

024

Recycle Gas to E-315

TI-5090

024

Recycle Gas from E-315

TI-5092

024

C-301 Suction

TI-5740

48

35

69 70

-19

V-306 Top Feed from E-305

New conlrol selpoinl. New TAL setpoinL Current TAL = -56 New conlrol setpoint. New TAH setpoinL Curren TAH = 1. New control setpoint. New TAL setpoint. Current TAL = 67.

•c

-12

-38

-43

-53 32

New TAL setpoint. Current TAL = -37

-30 -45

15

22

33

38

40

38

37

40

37

22

27

22

22

22

22

22

64

65

New control setpoint. New TAL setpoint. Current TAL = -53. New conlrol setpoint. New TAL setpoinL Currenl TAL = 24.


FLUOR Contract AOWT Rev. 0, 23-Sept-04

TABLE 2.1 • UNIT 44 CONTROLLER AND ALARM SET POINTS (EXISTING)


Tag Number

PSID

C-301 Discharge V-401 Feed Temperature

TIC-5212

026

Units

ERM Case

•C

89

•C

53

V-306 Bolloms from E-101 C5+ form E-401

87 63

71

TI-5096

50

026

V-306 Bottoms to E-401

TI-5107

V-401 Overhead

TI-5098

TI-5102

V-401 Tray 26

TI-5294

V-401 Reflux/NGL Product

TI-5105

177

177

73

80

°C

29

40

barg

59.3

59.3

027

028

New control setpoint. New TAH setpoint. Curren TAH = 73

82

62

74

New TAL setpoint. Current TAL = 84

120

75

77

55

55

73

75

156

•C

TIC-5099

V-401 Reboiler Retum

72

027

Comments

High

76

58

C5+ to Storage

V-401 Tray 7

Alarms

10% C2 C2 30% C2 20% C2 Recovery Recovery Recovery Rejection

145 165

161

48

59

65

160

110

PRESSURE EC-301 (Expander) Inlet

PIC-3501

59.3

59.3

59.3

39.1

38.6

EC-301 (Expander) Outlet

PI-3044

021

barg

39.6

39.6


PIC-3046

021

barg

41.8

42.1

42.0

42.2


PI-3047

021

barg

42.1

42.0

42.2

EC-301 (Compressor) Outlet

PI-3515

021

barg

42.7

42.6

42.4

44.2

39.2

46.2

40.4

41.8 42.4

37.1

37.1

37.0

EC-301 (Compressor) Inlet

PI-3516

021

barg

38.0

V-305 Overhead

PI-3049

022

barg

39.5

39.5

39.0

39.0

38.5

PDI-3050

022

bar

0.2

0.2

0.2

0.2

0.2

V-305 Pressure Drop

68.0

0.5


FLUOR Contract AOWT Rev. 0,23-Sept^4


Operating Mode Description HP Recycle from E-315 V-306 Overhead V-306 Overhead to E-305 V-306 Pressure Drop V-306 Tray 17

Tag Number

P&ID

PIC-3058

Units

ERM Case

barg

50.5

023 1/3

barg

23.0

23.0

PI-3052

023 1/3

barg

23.0

23.0

023 1/3

PI-3055

023 1/3

V-306 Tray 10

barg

23.0

23.0

23.6

23.6

barg

PIC-3060

025

barg

21.7

PIC-3201

025

barg

51.5

C-301 Suction

PI-3730

025

barg

C-301 Discharge

PI-3731

V-401 Pressure Drop

23.0

0.2

023 3/3

C-301 Discharge

50.5

23.0

High

50.5

New control setpoint.

22.7

New control setpoint. New PAH setpoint. Cunen PAH = 23.3

23.0

22.7

0.2

0.2

23.0

22.7

barg PIC-3202

C-301 Suction

50.5

PIC-3051

PDI-3054

Alarms

30% C2 20% C2 10% C2 C2 Recovery Recovery Recovery Rejection

PIC-3064

027

PDI-3065

027

PIC-3068

028

23.6

23.6

23.6

21.7

21.7

21.4

51.5

51.5

21.7

21.4

51.5

51.5

15.0

15.0

51.5 21.7

barg

51.5

barg

18.5 0.2

barg

17.5

Nm3/h

283000

51.5 18.5 0.2

0.2

0.2

20.0

New PAH setpoint. Currenl PAH = 24.5

19.6

New PAH selpoinl. Current PAH = 22.6

59.5 17.9 59.0

50.5

New PAL setpoint. Currenl PAL = 51.6 New PAH setpoint. Current PAH = 18.5

0.5

17.5

14.5

14.5

13.9

283000

283000

283000

283000

240000

89400

89400

581500

586300

257

253

336

323'

New PAH selpoinl. Current PAH = 18.0

FLOW Feed Gas to E-301 Feed Gas to E-313 EC-301 (Compressor) Inlet

FIC-1034 FIC-1035

019

FI-1501

021

Liquid from V-305

FIC-1041

Liquid from V-306

FIC-1042

023 1/3

89400

89400

89400

561000

568420

574800

m3/h

195

213

m3/h

378

365

Nm3/h

351

Cascade from TIC-5054 Cascade from TIC-5061

642000

270400 Cascade from LIC-2046

420

275

New control setpoint. Current FAH = 380. Cascade from LIC-2047

FLUOR Contract AOWT Rev. 0, 23-Sept-M



Alarms


Tag Number

ERM Case

Feed Gas to E-317

FIC-1203

023 3/3

Liquid from V-307

FIC-1204

023 3/3

Flow from E-316

FIC-1201

024

C-301 Suclion

FI-1730 FIC-1046

C2 10% C2 20% C2 30% C2 Recovery Recovery Recovery Rejection 92200

92200

92200

153

m3/h 55000

52400

50700

111600

113600

117100

58

91

NGL to Storage

High

92200

110000

183

200

121800

87000

60000

13000

120000

61700

60 350

200

Cascade from TIC-5207 New FAH setpoint. Current FAH = 136. Cascade from LIC-2204 New controi setpoint. New FAH setpoint. Curren FAH = 39000 New FAH selpoinl. Current FAH = 109500 New control setpoint. Current FAL = 60. Cascade from FIC-1048 New FAL and FAH setpoints. Currenl FAH = 280 Cunent FAL = 250. Cascade from LIC-2059

LEVEL V-301 Level

795

1190

400

No impact.

V-302 Level

LIC-2038

550

740

350

No impact.

V-303 Level

LIC-2040

1675

2900

450

No impact.

250

No impact.

018

LIC-2042

019

680

V-304 Level

LIC-2044

020

1400

2480

320

No impact.

V-305 Level

LIC-2046

1050

250

No impact.

LIC-2047

023 1/3

70%

3000

300

No impact.

E-308 Level

LIC-2050

023 1/3

250

No impact.

E-403 Level

LIC-2052

026

80%

1020

500

No impact.

LIC-2204

023 3/3

20%

5250

300

No impact.




2.2

New Controls Added for ERM Operation

2.2.1

Setpoints and Alarms


The setpoints for the new controllers and alarms added for the E R M Project are described in Table 2.2a. 2.2.2

Trips The new trip functions and the associated trip settings that have been added for the E R M Project are described in Table 2.2b. The following Cause and Effect Diagrams are also provided:

2.2.3

Drawing Number

Description

CEC 44-00-25-001

Unit 44 Process Cause and Effect Chart

04305 CET

E R M Refrigeration Package Cause and Effect

Manual Valves Table 2.2c provides a summary of the position (open or closed) for the manual valves added for the E R M Project based on the target ethane recovery level. N O T E : When changing the positions of a set of valves, it is critical that the closed valve be opened before the open valve is closed. This will prevent the system from being blocked-in. For example, when transitioning from C2 Enhancement mode to E R M mode, manual valve M-4402 is opened before M-4401 is closed.

CHAPTER4


FLUOR Conlract AOWT Rev. 0, 23-Sept-04

TABLE 2.2a - UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW)

Alarms


Tag Number

P&ID

Units

30% C2 ERM Case Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

-36

-32

-27

51

55

40

40

20

58

High

Low

Comments

TEMPERATURE E-313 Shell Side Inlet

TI-5131

019-1

-39

-37

V-401 Overtiead from E-402

TI-5124

028-1

51

51

E-406 Tube Side Outlet

TI-5127

028-1

20

30

35

35


TI-5121

028-3

20

35

35

35

59 35 35

-41

E-203 Outlet

TI-5410

22717-104

55

55

55

55

55

C-202 Low Stage Inlet

TIC-5405

22717-102

-24

-24

-24

-24

-24

C-202 Side Load Inlet

TIC-5404

22717-103

16

16

16

16

16

25

C-202 Discharge

TI-5401

22717-101

75

75

75

75

75

85

Lube Oil Supply

TI-5416

10512S

60

71

Lube Oil Reservoir

TI-5417

10512S

75

50

C-202 Motor Bearing

TI-5420AB

GE 127

70

80

High-high alarm at 90°C

C-202 Motor Bearing

TI-5421AB

GE 127

70

80

High-high alarm at 90°C

40 o

15

Set TAL at 0.1 C above the vapor dew point at suction pressure read by PT-3405. Set TAH at I O X above the vapor dew point at suclion pressure read by PT-3405. Set TAL al 0.1 "C above the vapor dew point at suction pressure read by PT-3404. Set TAH al 10°C above the vapor dew point al suction pressure read by PT-3404.

C-202 Motor Stator

TI-5422AB

G E 127

120

130

High-high alarm a l l 40°C

C-202 Molor Slator

TI-5423AB

G E 127

120

130

High-high alarm at M O ' C

C-202 Motor Stator

TI-5424AB

GE 127

120

130

High-high alarm at M O ' C

C-202 Gear High Speed Bearings

TI-5430AB

GE127

97

107


TI-5431AB

G E 127

TI-5432AB

GE 127

C-202 Gear Low Speed Bearings

TI-5433AB

GE 127

C-202 Gear Inboard Thrust Bearings

TI-5434A-C

G E 127

C-202 Gear Outboard Thrust Bearings

TI-5435A-C

G E 127

C-202 Bearings

TI-5440AB

GE 127

97 97 97 97 97 89

107


C-202 Bearings

TI-5441AB

GE127

89

99

C-202 Bearings

TI-5442AB

G E 127

89

C-202 Bearings

TI-5443A8

G E 127

89

99 99

107 107 107

107 99


FLUOR Contract AOWT Rev. 0, 23-Sep(-04

TABLE 2.2a • UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW

Alarms

Operating Mode Tag Number

P&ID

C-202 Bearings

TI-5444AB

GE 127

89

C-202 Bearings

TI-5445AB

GE 127

89

Description

Units


20% C2 Recovery

10% C2 Recovery

C2 Rejeclion

High

C-202 Bearings

TI-5446AB

GE 127

89

99

C-202 Bearings

TI-5447AB

G E 127

89

99

CM-202 Inlet Air

TI-5425A

GE411

CM-202 Inlet Air

TI-5425B

GE411

^

f-r-

Low

99 99

80

„ ^ .

PRESSURE PI-3081

023-4

barg

23.3

23.3

23.3

23.3

22.3

PDI-3082

023-4

bar

0.2

0.2

0.2

0.2

0.2

P-302 Discharge

PI-3083

023^

barg

26.0

23.0

P-302A Seal Pot

PI-3084A

023^1

barg

28.0

27.0

P-302B Seal Pot

PI-3084B

023-4

V-308 Tray 8 V-308 AP

V-205

PIC-3410A 22717-104

0.5

27.0

28.0 barg

18.8

18.8

18.8

18.8

19.7

17.0


PI-3403

22717-102

barg

1.0

1.0

1.0

1.0


PI-3402

22717-103

barg

6.4

6.4

6.4

C-202 Discharge

PI-3401

22717-103

barg

19.3

19.3

V-206

PI-3413

22717-103

barg

6.4

V-207

PI-3414

22717-102

barg

1.0

PDI-3430

GE561

mmH20

1000

2540

Seal Gas Filler AP (N2)

PDI-3431

G E 561

mmH20

1000

2540

Balance Chamber AP

PDI-3432

GE 561

mmH20

1000

1270

Buffer Gas

PI-3433

GE561

barg

1.4

C-202 Lube Oil

PI-3421

G E 529

barg

1.4

Lube Oil Pump A Discharge

PI-3415A

10512S

barg

5.2

4.5

Lube Oil Pump A Discharge

PI-3415B

10512S

barg

5.2

4.5

Lube Oil Filter AP

PDI-3416

10512S

_bar _

0.3

PI-3417

10512S

PDI-3425

GE411

Seal Gas Filler A P (Process Gas)

Lube Oil Supply CM-202 Air Intake

g

b a r

9-

mmH20

0.2

6.4

1.0 6.4

7.3

5.3

19.3

19.3

19.3

20.2

17.5

6.4

6.4

6.4

6.4

8.6

1.0

1.0

1.0

1.0

1.4

2.8

0.7

1.0 1.0 20.0

Comments

GASCO Ethane Recovery Maxtmization Project 5221


TABLE 2.2a • UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW)

Alarms


Tag Number

P&ID

Units


20% C2 Recovery

10% C2 Recovery

C2 Rejection

201

241

239

High

Low

Comments

FLOW P-302 Discharge

FIC-1070

023^1

m3/h

265

60

22717-102

Nm3/h

22500

26000

18000

Alarm settings to be confirmed by vendor.

FI-1402

22717-103

Nm3/h

78400

90000

63000

Alarm sellings lo be conlirmed by vendor. Alarm sellings to be confirmed by vendor.

C-202 Low Stage Inlet C-202 Side Load Inlei C-202 Discharge

202

236

FI-1400

22717-103

Nm3/h

100900

116000

81000

C-202 Discharge to Seal System

FIC-1430

G E 561

Nm3/h

1.7

2.9

1.2

^ 2 to C-202 Seal System

FIC-1431

GE 561

Nm3/h

1.7

Primary Vent Gas to Flare (Suction)

FI-1432D

GE 561

3.4

Primary Vent Gas to Flare (Discharge)

FI-1433D

G E 561

Nm3/h NmS/h

Cascade from LIC-2126

1.2

3.4

6.8

2.4

LEVEL E-318 Level

LIC-2111

019-2

1390

1590

500

V-308 Level

LIC-2126

023^1

4100

5000

2000

E-406 Level

LIC-2116

028-1

1240

1440

E-407 Level

LIC-2121

028-3

810

960

500 500

V-205 Level

LI-2403

22717-104

888

-1194

V-206 Level

LIC-2404

22717-103

-381

Measured from centerline of E-204

V-207 Level

LIC-2405

22717-102

-229

Measured from centerline of E-205

C-202 Lube Oil Rundown Tank

LI-2420

GE529

533 305 92%

C-202 Lube Oil Reservoir

LI-2431

10512S

100%

830

MISCELLANEOUS E-203 Vibration Bay 1

VAH-9050

041

E-203 Vibration Bay 2

VAH-9051

041


VAH-9052

041

E-203 Vibralion Bay 4

VAH-9060

041


VAH-9061

041


VAH-9062

041


VAH-9070

041


VAH-9071

041


VAH-9072

041

77%

^*

f-'V

^

mm

ass

d''J.-1~--- .... *

Measured from centerline of V-205


GASCO Elhane Recovery Maximization Project 5221

TABLE 2.2a - UNIT 44 CONTROLLER AND ALARM SET POINTS (NEW)

Alarms

Operating Mode 30% C2 ERM Case Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

Tag Number

P&ID

C-202 Motor - Vibration X

VXI-9410

G E 127

72

VYI-9410

GE 127

72

85 85

High-high Alarm at 99 um

C-202 Motor - Vibration Y C-202 Motor - Vibration X

VXI-9411

G E 127

72

85


C-202 Motor - Vibration Y

VYI-9411

GE 127

72

85


C-202-E1A Vibration

VAH-9415A

10512S

C-202-E1B Vibration

VAH-9415B

10512S

C-202-E1C Vibralion

VAH-9415C

10512S

VXI-9420

G E 127 32

45

Description

C-202 Gear High Speed - Vibration X

Units

High

iC-202 Gear High Speed - Vibration Y

VYI-9420

GE 127

C-202 Gear Low Speed - Vibralion X

VXI-9421

G E 127

C-202 Gear Low Speed - Vibration Y

VYI-9421

GE 127

51

64

C-202 Gear Low Speed - Vibration X

VXI-9422

G E 127

51

64

C-202 Gear Low Speed - Vibration '

VYI-9422

GE 127

51

C-202 Gear High Speed - Vibralion X

VXI-9423

G E 127

32

64 45

C-202 Gear High Speed - Vibration Y

VYI-9423

G E 127

32

45

C-202 Compressor - Vibration X

VXI-9430

G E 127

32

C-202 Compressor - Vibralion Y

VYI-9430

G E 127

32

45 45 45 45

Low

Comments

High-high Alarm al 99 um

64


VXI-9431

G E 127

32

C-202 Compressor - Vibration Y

VYI-9431

G E 127

32

C-202 Gear Low Speed - Axial Posilion

VZI-9424AB

GE 127

0.13

C-202 Compressor - Axial Position

VZ1-9432AB

G E 127

0.13

C-202 Gear High Speed - Acceleration

VI-9441

GE 127

m/s2

C-202 Gear Low Speed - Acceleration

VI-9440

G E 127

m/s2

C-202 Compressor - Acceleration

VI-9450

G E 127

m/s2

C-202 Compressor - Acceleration

VI-9451

GE 127

m/s2

39 39 39 39

High-High Alarm at 50 m/s2 High-High Alarm at 50 m/s2



TABLE 2.2b - UNIT 44 SETTINGS FOR NEW TRIPS

Description

Tag Number

P&ID

Units

Trip

Action

TEMPERATURE E-314 Shell Side Outlet

TALL-5126

020

-43

Closes LV-2044

E-313 Shell Side Inlet

TALL-5130

019-1

-43

Closes XV-9080 and LV-2111

C-202 Discharge

TAHH-5400

22717-101

90

C-202 shutdown

TI-5417 TI-5417

10512S

32

Heater on

10512S

50

Heater off

C-202-E2A

TI-5418A

10512S

75

Heater off

C-202-E2B

TI-5418B

10512S

75

Heater off


TAHH-5430

G E 127

C-202 shutdown


TAHH-5431

G E 127


TAHH-5432

G E 127


TAHH-5433

G E 127

C-202 Gear Inboard Thrust Bearings

TI-5434A-C

G E 127

115 115 115 115 115 115 115 115 115 115 115 115 115 115

Lube Oil Reservoir Lube Oil Reservoir

C-202 Gear Outboard Thrust Bearings

TI-5435A-C

GE127

C-202 Suction End Bearings

TAHH-5440

G E 127

C-202 Suction End Bearings

TAHH-5441

G E 127

C-202 Discharge End Bearings

TAHH-5442

G E 127

C-202 Discharge End Bearings

TAHH-5443

GE127

C-202 Active Thrust Bearings

TAHH-5444

G E 127

C-202 Active Thrust Bearings

TAHH-5445

G E 127

C-202 Inactive Thrust Bearings

TAHH-5446

G E 127

C-202 Inactive Thrust Bearings

TAHH-5447

G E 127

P-302A Seal Pressure

PALL-3084A

P-302B Seal Pressure

PALL-3084B

023-1 023-1

C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown

PRESSURE barg

26.5

P-302A Trip

barg

26.5

P-302B Trip

Comments




Tag Number

P&ID

Units

Trip

Action

C-202 Discharge

PAHH-3400

barg

C-202 Side Load

PALL-3404

barg

21.0 3.6

C-202 shutdown

Description

Comments

C-202 Suction

PALL-3405

22717-101 22717-103 22717-102

barg

0.0

C-202 shutdown

C-202-P1A Discharge

PAL-3415A

10512S

barg

4.5

Start B pump

C-202-P1B Discharge

PAL-3415B

10512S

barg

4.5

Start A pump

C-202 Lube Oil

PALL-3420

G E 529

barg

0.35

C-202 shutdown

2 out of 3 voting

Primary Vent Gas to Flare (Suction)

FAHH-1432

GE561

Nm3/h

9.5

C-202 shutdown

2 out of 3 voting

Primary Vent Gas to Flare (Discharge)

FAHH-1433

GE 561

Nm3/h

9.5

C-202 shutdown

2 out of 3 voting

V-308 Level

LALL-2127

023-4

300

P-302 A/B shutdown

V-206 Level

LAHH-2401

22717-103

-991

C-202 shutdown

Trip setting is measured from V-206 centerline.

V-207 Level

LAHH-2402

22717-102

-686

C-202 shutdown

Trip setting is measured from V-207 centerline.


VSH-9050AB


VSH-9051AB


VSH-9052AB


VSH-9060AB


VSH-9061AB


VSH-9062AB


VSH-9070AB


VSH-9071AB

041 041 041 041 041 041 041 041

C-202 shutdown

FLOW

LEVEL

MISCELLANEOUS Fan motor shutdown

Activated from D C S

Fan motor shutdown


Fan motor shutdown


Fan motor shutdown


Fan motor shutdown


Fan motor shutdown


Fan motor shutdown


Fan motor shutdown





Description

Tag Number

P&ID

Units

Trip

Action

Comments

Fan motor shutdown



VSH-9072AB

041


VXAHH-9420

G E 127

64

C-202 shutdown


VYAHH-9420

G E 127

VXAHH-9421

GE 127


VYAHH-9421

GE 127


VXAHH-9422

G E 127

64 102 102 102

C-202 shutdown



VYAHH-9422

G E 127

C-202 shutdown


VXAHH-9423

GE 127


VYAHH-9423

G E 127

102 64 64


VXAHH-9430

G E 127

57

C-202 shutdown


VYAHH-9430

G E 127

57

C-202 shutdown


VXAHH-9431

G E 127

57

C-202 shutdown


VYAHH-9431

G E 127

57

C-202 shutdown

2 out of 2 voting

C-202 Gear Low Speed - Axial Position

VZAHH-9424AB

GE 127

0.25

C-202 shutdown

2 out of 2 voting

C-202 Compressor - Axial Position

VZAHH-9432AB

G E 127

mm

0.25

C-202 shutdown

C-202 Gear High Speed - Acceleration

VAHH-9440

G E 127

m/s2

50

C-202 shutdown

C-202 Gear Low Speed - Acceleration

VAHH-9441

GE 127

m/s2

50

C-202 shutdown

->4

C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown C-202 shutdown



TABLE 2.2c - UNIT 44 MANUAL VALVES

Operating Mode Valve Tag

M-4401 M-4402

M-4404

20% C2 Recovery

10% C 2 Recovery

C2 Rejection

Comments

Open

Open

Closed

New valve

P&ID

ERM Phase 1

E-303 Bypass (HP Recycle)

018

Closed

Open

Open

E-314 Outlet to V-306

020

Open

Closed

Closed

Open

Open

Open

New valve. Works together with M-4402.

023-1

Closed

Open

Open

Closed

Closed

Closed


022

Closed

Closed

Closed

Closed

Closed

Open

Existing valve

023-1

Open

Closed

Closed

Closed

Closed

Closed


Description

E-314 Outlet to V-308 E-303 Isolation (V-305 Bottoms)

M-4403

30% C 2 Recovery

ERM Mode

V - S O / Liquid to V-306 V-307 Liquid to V-308

023-1

Closed

Open

Open

Open

Open

Open


Open

Closed

Closed


Closed

Open

Open


M-4405

E-315 Bypass (HP Recycle)

024

Closed

Open

Open

M-4406

E-315 Isolation (HP Recycle)

024

Open

Closed

Closed

Page ONSHORE GAS DEVELOPMENT PROJECT N" 545

TITLE

ADNOC - HABSHAN PROCESS CAUSE AND EFFECT CHART

UNIT 44 4 i 5

RevPage

Rev.

| 6 | 7

Page

! r

8 i 9

x ': x I x 1 X X I X

: X i

! X j X ' X j X

1 Bis

X I X | X

X

2 Bis . X

2 Ter

. -5

X X

X

X

FLUOR

Project 5221 Agreement 13522102 Fluor Contract AOWT

Unit

CEC

44

3/3/95

A. PIHOUEE

R. AGAZZI

8.1

19/9/94

Y. SIMON

J. CASTEL

7\ai/5/c*\

2 I'

2/8/94

Y. SIMON

R.AGAZZI

7Ai

1

25/1/94

i

H. MAHE

J. CASTEL

0

5/10/93

i

A LEGALL

R. AGAZZI

Rev.

JJ/MUfAA

Written by

Checked by

6/5/97 19/4/97

Document revisions 76001. CECO! - SPPW - R x . 1 - AKO-W1J0M.0 .

Serial No

Rev

25-001

CERTIFIED

1 W o4

Rev

Symbol

Dm

;

f >NiH A

;E

Y. SIMON

A. RABINIAUX

Y. SIMON

R. AGAZZI

Written by

Checked by

PROCESS SPECIFICATION OrjuctiC

TECHNIP CEC CLIENT

Rev. ADNOC

LOCATION HABSHAN

NOTES

UNIT 44

5

|

7 6 ^ J L C=C

Date 5/10/93 25/1/94 2/8/94

Made by ALG HM

3/3/95 19/4/96

PHA

GENERAL A/OTES-

Le«f«< 1 conBtponctstoa loea! sftm down ( t o pump E * M t»o*r) Level 2 corresponcft to • systam shut down (a.g. group of items) or zone anm oown Zona stu* down corresponds to Units 34 - *A shut down tor xor* 20

17 IE

WOTES 1 S I G N A l WITH START UP OVERRIDE •W-HS-SOIS FOR 44J'ALI -3029 t * - H S - X \ B FOH 4*4>ALL-3032

25 26

2 SIGNAL G E N E R A T E D BY COMPRESSOR VENDOR PLC

4DEIETCO 5 SIGNAL WITH START-UP OVERRIDE 4 4 + i & 9 0 M FOR 44-PALL-3069

8 SIGNAL W T H START UP O V E R R D E 44+IS-9021 FOR 44-FAU.-3071 9 XV-9006 PERMISSIVE TO O P E N : 44-PclSt-3Q73 10 CONTROL TRANSFERRED TO 44-LV-20S2B 11 ESO S E Q U E N C E O F MACHINES AND PACKAGES A R E BY VEWJORS 12 INWatTION O F 44-XHSC-9077 F THE HEATER W g - I O I U l IS RUNNING (STATUS OF HEATCR B Y 44-XL-7817) 13 44-XZSO-90O3 P E R M B S V E TO START 44-C-201 14 44-XZSC7501 PERMISSIVE TO OPEN 44.XV-S0OS B PERMISSIVE TO START 44-EC-301 (XS-9022) 15 CLOSING T H E V A L V E 44-XV-9006 WHL STOP THE TURBO EXPANDER AND WIU. GENERATE A N A L A R M IN D C S 16 44-XZSO9010 INHIBIT TO START THE TURBO-EXPANDER 44-)tZSO-9010 AUTHORISATION TO START THE TURBOEXPANDER 17 INHIBITION OF H - X H S O - M X H WHEN THE 44-C-201 IS RUNNING (44-XS-7620) 18 WITH THE TIME DELAY •= 1 MN. 19 R E S E T FACILITIES T O B E PROVIDED AFTER ACTIVATION OF HAND SWITCHES 20 SHUT OOWN OF EXPANDER WHEN M-XV-9007 IS CLOSED (INTERNAL SIGNAL)

7600L-CEC01 - S P P 1 - R*v.2- A N G - W l 2 3 * 4 0

C. •

Checked by RA JC RA RA RA

Page

PROCESS SPECIFICATION M-yuerK. '

j CEC ADNOC LOCATION HABSHAN

NOTES

UNIT

imm

Made by YS YS

Checked by RA JC

YS

RA

44

siSENERAL NOTES' L e v * 1 coTBsporKts t o * local shut down (•.& punp tnut oown) Level 2 ayrMpontlJ to a systam mul down (e.g. o™4> o* " m i ) or zone s h u (Sown Zone s i u down correspanOs to Units 34 • 44 shul down for zone 20

titOTES21 SIGNAl. WITH START U P OVERRIDE •M-HS-BOBS FOR 44-XZSC-9077 22 SIGNAL WITH START U P OVERRIDE -M-HSÔBT FOR M-XSC-gOCD 23 23 W Z S C - i 5 a \ AND 4+-XZSC-7S01 PERMISSIVE T O O P E N WOCVÔIO 24 444tS-711B AND 4 4 . X Z S O « 1 1 D A N D 4 4 j a S a « X » PERMISSIVE TO START 4 4 E C J 0 1 25 THE ACTION IS POSSIBLE ONLY IF OIL PUMPS HAVE BEEH SHUT DOWN FOR MORE THAN 5 MINUTES ( 4 4 - X M 1 0 5 )

37 ~ 38 39

r

42 43 45 46 ~ 47 48

-

49 50 51 52 S3 54 55 58 57 58 59 60 61 62 63 64 65 66 67 66 76OOL-CEC01 - S P P 1 - R*»-2- ANG - WI23M.0

Page:

1 Bis 19/4«6

'36 •'

-.Rti' . (

76CG_ Z=.Z Date. 2/8/84

CUENT

Sona'N:

FUNCTION PETtfORMED . 4<-ME-lBl H I S H U T D O W S I G N A L

I

R E G E N , C A S T O H X A T E R 44-MZ-I01 H i

MOTOR BAY U . «*-g-301 MOTOR BAY IB MOTOR BAY 2A 44-t-m MOTOR BAY IB 44-Z-2H MOTOR BAY JA 4*-g-3M MOTOR BAY 3B 44-R-m ;*4.XS-90S6A MOTOR BAY 4A 4*-Z-3»l | U-XS-K16 B MOTOR BAY 4B MOTOR BAY 5A **-t^2*l jl 44-X3-9W7B MOTOR BAY 5B 44-g-Hl MOTOR BAY SA 44-E-3H MOTOR BAY A 44-E-i« t BAY BB 44.E-2IJ j44.X5-90rt B MOTOR BAY 9A 44.E.2H MOTOR BAY gB 44-g-itl MOTOR BAY IOA 44-RÎI MOTOR BAY HB 44-Z-Ut MOTOR BAY IIA44-g-2» MOTOR BAY 1 IA U - t A i 1 MOTOR BAY IIA 44-E-2U MOTOR BAY IIB 44-g-3»l

-

paw

RIV I

DATI

rag TRIP TRIP TRIP TRIP

ISSUED FOR CONSTRUCTION tSSUED TOR PIS1GW

FnoiT

BY

CtDPD t F J a

DRAWIWC TITLE

ABU DHABl NATIONAL OIL COMPANY BECHTIXTrCHNIP

'*—v***'

JiJV

JOINT VEISTURK ONSHOM GAS DEVEU)Pfgwr FROJECT

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44-P.W1 HC SUMP DRUM PUMP

ISSUED FOR DESIGN DRAWING NO-

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ABU DHABl NATIONAL OIL COMPANY

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CONDENSATE TO STORAGE CONDENSATE TO STORAGE CONDENSATE TD FLARE DRUM STEAM CONDENSATE FROM 44-E-403 NGL TO STORAGE 44-FV-l04t U-ME-IH-H1 SHUTDOWN SIGNAL 44-XS-9M9 44-XS-9051A/B *i-i>-4H Am DEBUTANP J R REFLUX PUMP W-LV-30S2A

3 FOR CONSTRUCTION DESCRgTlON REV DATE ABU DHABI NATIONAL OIL COMPANY

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DATE

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BECHTEL TECHNIP

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1 CLIENT PAGE

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ABU DHABI NATIOMAL OIL COMPANY

REISSUED FOR CONSTRUCTION ISSUED FOR DESIGN DESCRIPTION. DRAWING NO.

DRAWING TITLE

BECHTEL TECHNIP CAUSE d EFFECT CHART JOTNT VENTURE ONSHOM CAS DEVELOPMENT PROJeCT

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ABU DHABI NATIONAL OIL COMPANY

ISSUED FOR DESIGN DESCRIPTION DRAWING NO,

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U-E-203 PROPANE OOWOENSgR F W S

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_ W - 3 0 B COLD OEUETHANIZER B O n O M S O U U E T

4*£>31B 2ND FEED CHILLER

4AE-tO& DEBUTANIZER TRIM CONDENSER

44E-407 NGL SUBCOOLER

ISSUED FOR CONSTRUCTION NOTES:

FOR

REVISED PER GASCO COMMENTS

LOGIC R E F E R TO TOROMONT C&E.

ISSUED FOR APPROVAL

C O N D E N S E R W . E . 2 0 3 F A N S TRIP F R O M O C S .

DESCRIPTION

SflKO

FIUOR. G A S C O E T H A N E R E C O V E R Y MAXIMIZATION P R O J E C T

C A U S E AND E F F E C T CHART

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FUNCTION P E R F O R M E D *j-C-202 C O M P R E S S O R

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U-E-203 P R O P A N E C O N D E N S E R FANS

DEMETHAHLZER BUTTOMS PUMP A4-P-302A DEMETHANIZER BUTTOMS PUMP 44-P-303B

44V-30B COLD DEMETHANIZER BOTTOMS OUTLET

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F O R 44-C-202 L O G I C R E F E R T O T O R O M O N T C A E .

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13522102 CONTRACT AOWT

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CUEm

TOROMONT PROCESS SYSTEMS, INC

GASCO ERM PROJECT #5221 SHUTDOWN/INTERLOCK SYSTEMS CAUSE AND EFFECT DIAGRAM PROPANE REFRIGERATION SYSTEM STATUS

OUTPUT OR EFFECT DESCRIPTION

DATE

CHK

APP'D

APPROVED P3R CONSIUlXmON ISSUED POR DESIGN GWO

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PROJECT NUMBER: 22717 INPUT OR CAUSE DESCRIPTION jjoxmKJuxnn*

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BOB GEAStL&ILHD END RADIAL BBARWO TBUP. EIOH GEAR H. J. COITLWO END X.

Document No. 0430S C E T

A. lEARDOTEMP.

P a g e 1 of 3

Rev. 4 By: GWO Data: 06/29/2004

TOROMONT PROCESS SYSTEMS, INC

GASCO ERM PROJECT #5221 SHUTDOWN/INTERLOCK SYSTEMS CAUSE AND EFFECT DIAGRAM PROPANE REFRIGERATION SYSTEM

OUTPUT OR EFFECT DESCRIPTION

DATE

CHK

APP'D

MWW

OWO

APPROVED POR CONSTRUCTION ISSUED RJR DESIGN

GWO

PROJECT NUMBER: 22717 INPUT OR CAUSE DESCRIPTION

LL»EAJUNOTEMP-

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lOOTOF J l W N t J O

LUl HO ILHJU? A DUOtAROE PBEOTBF. LOW

Document rto. 0 4 3 0 5 C E T

P a g e 2 of 3

Rev. 4

By: G W O

Date: 06/29/2004

TOROMONT PROCESS SYSTEMS, INC.

GASCO ERM PROJECT #5221 SHUTDOWN/INTERLOCK SYSTEMS CAUSE AND EFFECT DIAGRAM PROPANE REFRIGERATION SYSTEM STATUS

DATE

OUTPUT OH EFFECT DESCRIPTION

T

APPROVED TOR CONSTTtUCnON ISSUH) Hm DF.SIGN

PROJECT NUMBER: 22717 PHO HO.

INPUT OR CAUSE DESCMPTION

onEOLmuriDUawtoEraEASutELDw * muum} A B m&uutE LOW !SFAXA-no« IIXTO OAJ TWMUU HOT LOW JJlEOl-lMXYOttTEMmATWlUm ujiKon.iRwavoa-rtMPEfcA-miEK LUIEOB.IS3avoaU\tLU)W

LUIE OIL i £ a a \ o a KEAm ovatmip LUIE OIL ttsavoB HEATBI ovsnsip UJIE OL fuwps W T mjwwnw

2 OUT OP 1 KOT IUN

NOTES: 0 = HOI PRESENT, P = PERMISSIVE, R = RESET 1. AFTER "NORMAL STOP". ESD VALVES XV7400, 7401, 7402 WILL REMAIN OPEN. FLARE VENT VALVE XV7405 REMAINS CLOSED. 2. SEPARATION GAS PERMISSIVE ONLY ACTIVE ON INITIAL PUMP STARTUP, I.E. BOTH PUMPS NOT RUNNING AND MAIN MOTOR NOT RUNNING. 3. ESD VALVES MUST BE OPENED BEFORE START-UP BY FIELD OPERATOR AFTER LOGIC IS RESET. FLARE VENT VALVE XV-7405 REMAINS CLOSED EXCEPT UPON ESD WITH DEPRESSURIZATION. 4. OUTPUT IS ENERGIZED WHEN ALL TRIP CONDITIONS ARE NORMAL AND RESET FROM HS-9455 IS RECEIVED. 5. START OUTPUT IS ENERGIZED FOR S SECONDS WHEN DCS START PULSE IS RECEIVED IF ALL TRIPS ARE CLEARED AND RESET, AND ALL PERMISSIVES SATISFIED. 6. LOCAL START PERMISSIVE IS ENERGIZED WHEN DCS AUTH FOR LOCAL START IS RECEIVED IF ALL TRIPS ARE CLEARED AND RESET AND ALL PERMISSIVES SATISFIED. 7. ONLY ONE RELAY CONTACT FOR HEATER CONTROL, OPEN = HEATER OFF, CLOSED = HEATER ON. CONTACT CLOSES WHEN TEMPERATURE FALLS TO SOFTWARE SETTING FOR TSL5417 AND REMAINS CLOSED UNTIL TEMP. REACHES TSH5417 OR OTHER TRIP CONDITION IS PRESENT. 8. AUTO START ANYTIME LESS THAN 2 FAN MOTORS ARE RUNNING OR LOW MOTOR AIR PRESSURE OCCURS. 9. DEPRESSURIZING VALVE OPEN PB IS DISABLED WHILE COMPRESSOR IS RUNNING 10. XZSC7400 IS A ONE-SHOT TRIP ACTION WHEN VALVE CLOSED POSITION FIRST OCCURS. TRIP LOGIC MAY BE RESET BY HSR945S WHILE VALVE IS CLOSED. 11. SURGE CONTROLLER IS SIGNALED FOR NORMAL UNLOAD AND 10 SECONDS LATER COMPRESSOR IS STOPPED AND NON ESD VALVES ARE DE-ENERGIZED. 12. SURGE CONTROLLER IS SIGNALED FOR RAPID UNLOAD AS LOCAL STOP IS CONNECTED DIRECTLY TO THE MOTOR STARTER. TRIP LOGIC MAY BE RESET BY HSR9455 WHILE MOTOR IS NOT RUNNING (XS7414 OPEN CONTACT IS A ONE-SHOT TRIP ACTION) 13. HSR9455 IS ENABLED ONLY AFTER ALL TRIP CONDITIONS ARE NORMAL. 14. REFERENCE APPENDIX "A" ATTACHED FOR START-UP FLOW CHART

Document No. 04305 CET

Page 3 of 3

Rev. 4 By: GWO

Dato: 06/29/2004




CHAPTER 5

N O R M A L OPERATION

CONTENTS

SECTION 1.0

2.0

PAGE

OPERATING VARIABLES AND CONTROL PHILOSOPHY

2

1.1 1.2 1.3 1.4 1.5

2 4 4 6 6

Gas Chilling and Expansion Recovery Tower Demethanizer System Recycle Compressor Debutanizer

TROUBLESHOOTING. 2.1 2.2 2.3 2.4

CHAPTER 5

E R M Refrigeration System Shutdown Trip of the Existing Refrigeration System Other Trips Understanding Alarms

8 8 9 9



1.0


OPERATING VARIABLES AND CONTROL PHILOSOPHY The ethane recovery performance of Unit 44 is dependent on the following three main variables: s

»

Temperature ofthe I ' Stage Feed KO Drum (44-V-301). Ethane recovery increases as the temperature of 44-V-301 is lowered.

•

Temperature at the bottom of the Demethanizer (44-V-306). In order to hold the recovered ethane in the liquid stream, the temperature at the bottom of the column is reduced.

•

Temperature ofthe Debutanizer Overhead Accumulator (44-V-402). As ethane recovery increases, the temperature of 44-V-402 must be lowered to ensure that the C2+ N G L is totally condensed.

These variables are discussed in detail in this section.

1.1

Gas Chilling and Expansion

1.1.1

First Stage Chilldown The E R M modifications do not impact the flow control philosophy used in the first stage gas chilldown section of the unit. The dried feed gas is distributed and controlled as follows: 44-FIC-1034 controls the gas flow to 44-E-301. 44-FIC-1034 is reset by 44-TIC-5054 (residue gas from E-301). This arrangement ensures that the residue gas leaves 44-E-301 at a fairly constant temperature and optimizes the recovery of refrigeration from the residue gas. 44-FIC-1035 controls the gas flow to 44-E-313. 44-FIC-1035 is reset by 44-TIC-5061 (feed gas from E-313). This arrangement allows the temperature approach of 44-E-313 to be optimized. 44-HIC-7210 controls the gas flow to 44-E-306 and 44-E-318. The three feed paths operate in parallel. Therefore, the pressure drop across each path (including the control valve) must be the same. Since the pressure drop through the 44-E306/44-E-318 flow path is the highest, 44-HV-7210 will normally be operated full open. 44FV-1034 and 44-FV-1035 will close as required to maintain the required flow rate at the available AP. NOTE: Operating with 44-HV-7210 full open will minimize pressure drop through the system and will maximize C2/C3 recovery. The key temperature control point for the first stage chilldown section is at 44-V-301. The temperature of V44-V-301 is controlled by adjusting the load ofthe two propane chillers (44E-306 and 44-E-318). 44-E-306 provides the majority ofthe required cooling duty. 44-E318 provides less duty, but its refrigeration is at colder level. Two control schemes are provided: 1.

CHAPTER 5

Set the duty of 44-E-318 and control the temperature of 44-V-301 by adjusting the duty of 44-E-306. In this option, the set point for the 44-E-318 level controller would remain




fixed, and the 44-E-318 tube bundle would remain completely submerged. The temperature of 44-V-301 would be controlled by adjusting the speed of the 44-C-201. The compressor speed impacts the operating pressure and evaporation temperature on the propane side of 44-E-306. This option is similar to the current control approach. 2.

Set the duty of 44-E-306 and control the temperature of 44-V-301 by adjusting the duty of 44-E-318. In this option, the set point for the 44-C-201 speed controller would remain fixed. The temperature of 44-V-301 would be controlled by adjusting the propane level in44-E-318 (44-TIC-5056 to LIC-2111 cascade control).

Option 1 is recommended due to the flexibility of the steam turbine driver and the larger design duty of 44-E-306. A new Hand Switch (44-HS-5056) is provided to allow the operators to select the preferred control mode. The pressure drop on the feed gas side of 44-E-306 is much higher than the design valve. It is believed that this is due to plugging from molecular sieve dust. The high pressure drop currently limits the flow through 44-E-306. To solve this problem, the existing feed gas bypass line around the First Stage Chilldown section is re-routed to between 44-E-306 and 44-E-318. The relocated bypass ensures that the new feed chiller can always be fully loaded by mixing warm feed gas from dehydration section with the outlet from 44-E-306. Manual valve 44-M-052 can be used to adjust the flow if required. The manual valve should be adjusted to maintain the temperature of 44-V-301 as low as possible. As shown in the table below, the temperature of 44-V-301 is reduced as ethane recovery increases.

44-V-301 Temperature

1.1.2

ERM Mode

30% C2 Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

-22

-21

-19

-17

-12

Second Stage Chilldown The flow and temperature control strategies for the second stage chilldown section are not changed as a result ofthe E R M Project. As the ethane recovery level increases, the temperature of 44-V-302 will decrease. The temperature of 44-V-302 can be controlled to a limited extent with TIC-5058 which bypasses a portion of the gas from 44-V-301 around 44-E-302. The temperature of 44-V-302 is mainly dependent on the temperature of 44-V-301.

44-V-302 Temperature

CHAPTER 5

ERM Mode

30% C2 Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

-42

-39

-35

-32

-32





1.1.3


Expander The control scheme for the expander (44-EC-301) is not modified. The E R M operating conditions will have the following effects: Inlet Temperature:

As shown in Section 1.1.2 of this Chapter, the temperature of 44-V302 will decrease.

Inlet Volumetric Flow: The inlet flow to the expander will decrease due to the lower inlet temperature and the higher percentage of feed gas condensed in 44V-301 and 44-V-302. Power:

1.2

The power generated by the expander will decrease due to the lower inlet flow.

Recovery Tower The control scheme for the Recoveiy Tower (44-V-305) is not modified. As shown in the table below, the temperature of 44-V-305 is reduced as ethane recovery increases. ERM Mode

30% C2 Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

44-V-305 Top

-64

-61

-60

-58

-57

44-V-305 Bottom

-60

-57

-56

-53

-54

The Recovery Tower Reboiler (44-E-303) is not used in any ofthe C2 recovery modes.

1.3

Demethanizer System The purpose of the Demethanizer system is to fractionate light components from the NGL. The overhead vapor from the demethanizer system is recycled back to the Recovery Tower and used as reflux to improve product recovery. The new Cold Demethanizer (44-V-308) acts as extension of the existing Demethanizer. Since 44-V-308 is made of stainless steel and has a minimum design temperature of -100 C, lower operating temperatures are possible. The cold stream from 44-V-307 is sent to the new tower instead of 44-E-305. This moves the coldest streams into the new column and protects the carbon steel Demethanizer from exposure to low temperatures. In the E R M operation, the overhead temperature of 44-V-306 will actually increase. o

The operating pressure of the Demethanizer (44-V-306) remains unchanged the E R M operation. As in the current design, the Demethanizer pressure is controlled by adjusting speed of the Recycle Gas Compressor turbine with performance controller PIC-3740.

CHAPTER 5




As explained above, the overall temperature profile in the Demethanizer is reduced in E R M mode to maximize the C2 content in the bottom stream to the Debutanizer. The temperature profile is lowered by adjusting the overall reboiling duty (bottom reboiler + side reboiler). The following table summarizes the expected temperatures at the Demethanizer control point.

44-V-306 Tray 2 Temperature

ERM Mode

30% C2 Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

28

42

48

61

75

In the E R M mode of operation, most of the heat input to the column will be generated by the Bottom Reboiler (44-E-308). The duty ofthe Side Reboiler (44-E-307) is minimized with TV-5088 B such that the thermosiphon reboiler is continuously primed. The amount of feed preheating is also reduced by bypassing 44-E-315 in E R M mode. As the ethane recovery level is decreased, it will be necessary to increase the amount of feed preheating in order to unload the Demethanizer Bottom Reboiler. This will require the new bypass around 44-E-315 to be closed. The table below provides the recommended valve positions for the various operating modes. ERM Mode

30% C2 Recovery

20% C2 Recovery

10% C2 Recovery

M-4405

Open

Open

Open

Closed

C2 Rejection Closed

M-4406

Closed

Closed

Closed

Open

Open

NOTE: When performing this operation is necessary, M-4406 should be opened before M4405 is closed.

The new Cold Demethanizer and Cold Demethanizer Bottoms Pumps are fully integrated with the existing Demethanizer. The overhead vapor from V-306 is sent to V-308. Liquid from V308 is sent to V-306 (via P-302A/B). In E R M mode, the liquid from V-304 is sent to V-308 after being heated in E-314. The heavy components in this stream act as a sponge for light components and improve ethane recovery. As the ethane recovery level is decreased, this stream is not required and should be redirected to 44-V-306 using manual valve M-4401 and M-4402.

CHAPTER 5

ERM Mode

30% C2 Recovery

20% C2 Recovery

10% C2 Recovery

C2 Rejection

M-4401

Closed

Closed

Open

Open

Open

M-4402

Open

Open

Closed

Closed

Closed




In case of a high flow alarm (FAH-1070) on the discharge ofthe new Cold Demethanizer Bottoms Pumps, the stream from 44-E-314 should be re-directed to V-306 using manual valves M-4401 and M-4402. If this operation is necessary, M-4401 should be opened before M-4402 is closed.

1.4

Recycle Compressor

'

The controls for the Recycle Gas Compressor are not modified for the E R M Project. As ethane recovery increases, the molecular weight of the recycle gas will decrease. This will impact the amount of discharge pressure generated by the Recycle Gas Compressor. The discharge pressure of the compressor should be maximized. This will help ensure that the recycle gas is condensed in 44-E-304 and will increase the amount of JT cooling across PV3058. Both of these effects will improve ethane recovery. A new bypass is added around 44-E-303. This bypass is located near E-301/2/4 and reduces the pressure drop in the recycle loop. This helps compensate for the lower discharge pressure of the compressor. The new bypass should be used for all modes of operation except for C2 rejection mode. When transitioning to higher ethane recovery modes, it is important to adjust the Demethanizer operating temperatures before adjusting the temperature of 44-V-301. This will prevent the recycle compressor from being overloaded. In case of gas build up in the recycle loop, the existing pressure control valve PV-3201 located at compressor discharge will prevent a trip the compressor by releasing the excess gas to residue gas grid. The set point of PIC-3201 shall be adjusted slightly above the normal compressor discharge pressure (which depends on the operating conditions).

1.5

Debutanizer In E R M mode, the operating conditions of the Debutanizer have to be adjusted to account for the increased ethane content of the overhead stream. The raw N G L from the Demethanizer is heated in the Debutanizer Feed Preheater (44-E-405) before being fed to tray 23 of the Debutanizer. The temperature profile of the tower will not change significantly as the ethane content ofthe N G L increases. The main effects on the system will be: 1. A lower temperature will be required to condense the overhead stream. 2. The reflux rate can be reduced. The new Debutanizer Trim Condenser (44-E-406) provides the cooling necessary to condense the overhead stream. High level refrigerant from the new refrigeration system is used on the shell side of the new exchanger. Since 44-E-406 is located at grade below the Debutanizer Overhead Accumulator (44-V-402), the pressure at the exchanger will be higher than the pressure in 44-V-402 due to the static head of the liquid. Therefore, the NGL leaving 44-E406 must be subcooled to prevent vaporization in the drum. 44-E-406 has been designed to provide the necessary subcooling.

CHAPTER 5




As discussed in Section 3.1 of Chapter 2 the Debutanizer pressure control scheme is modified for the E R M Project. Tower pressure will be controlled using the hot vapor bypass. The accumulator pressure will be an outfall from the Debutanizer pressure (44-V-402 Pressure = V-401 overhead pressure - 44-E-402 DP - 44-E-406 DP - static head). The temperature ofthe NGL leaving 44-E-406 can be controlled by adjusting the level of propane on the shell side ofthe exchanger (TIC-5127 to LIC-2116 cascade). In normal operation, it is recommended to use straight level control (no temperature cascade). In the event that pressure in the system continues to fall even with the hot vapor bypass is fully open, the temperature controller can be used to reduce the amount of subcooling achieved in 44-E-406 and the pressure will stabilize.

CHAPTER 5


Ethane Recovery Maximization (ERM) Project Switching V-307 Bottoms Stream from E-305 to V-308 Rev. 0


Switching V-307 Bottoms Stream From E-305 to V-308 Rev.O May 19, 2005 The following procedure covers the diversion of V-307 bottoms stream from E-305 to V-308 and the concurrent alignment of V-308 bottoms stream to E-305 (Opening of valve M-4404 and closing of valve M-4403). The temperature in the top section of the Demethanizer, V-306, will increase as soon as cold liquid from V-307 is replaced with warmer liquid from V-308. V-306 top temperature is expected to increase by approximately 15 C in the new steady state. 0

The key to a successful switch is to minimize the time that flow to E-305 is lost or reduced during the switch to minimize the potential for upsets due to the loss of cooling at the top of V-306. When valves M-4403, M-4404, and LV-2126 are open, the flow from LV-2126 will preferentially return to V-308 instead of flowing to E-305. The period of time when all three valves are open should be as short as possible to minimize the loss of flow to E-305. In this procedure, we want to control the flow rate to E-305 by minimizing the loss of flow to E305 and avoiding a subsequent high rate of flow from V-308. The flow rate can be best controlled by minimizing the time it takes to make the switch, minimizing the recycle back to V 308. This can be done by opening valve M-4404 and closing valve M-4403 quickly as soon as LV-2126 opens up. The target flow rate through 44LV-2126 is approximately 140 - 160 m /hr. Try to maintain a steady flow rate from LV-2126 and let the level in V-308 fluctuate during the switch. The target flow rate is 150-160 m /hr. 3

3

Preparation prior to the switch 1. LC-2126 at the discharge of P-302 should be on manual and should be closed. 2. Start P-302 on full recycle. 3. Reduce the level in V-307 from the normal 30% to 25% to have some room available for a possible level increase during the switch. 4. Increase the level in V-303 and V-304 to be able to increase flow to V-306 if additional flow is required to maintain V-306 level. 5. Steam flow to E-308 (Demethanizer reboiler) should be put on manual. (Note: There is a possibility that some off-spec product may be produced during transition. We believe this is unlikely because the reflux will be warmer than normal during transition). The Reboiler retum temperature and the Reboiler duty should remain constant during the transition. 6. The temperature controller, TIC-5088, for side reboiler, E-307, should be kept in manual during the switch. The Reboiler retum temperature should remain constant. 7. The recycle gas compressor should be on speed control with no reset from PIC-3051 A. During the switchover, the board operator must monitor the Demethanizer pressure. If the pressure rises as indicated by PIC-3015A above 22 barg, the operator must increase the compressor speed to bring the pressure back down to normal.


Ethane Recovery Maximization (ERM) Project Switching V-307 Bottoms Stream from E-305 to V-308 Rev. 0


8. Due to the transitive nature of the switchover some alarms may occur. Therefore, the alarm set points associated with this system may need to be reviewed by the Operators to avoid unnecessary nuisance alarms during the transition. When making the switch, it is critical to establish a steady flow from the V-308 to E-305 as quickly as possible to maintain a steady flow to E-305. After the system is stable, the levels in V-307 and/or V-308 can be slowly corrected to the normal values after the switch is completed. Performing the Switch 1. Open the block valve between V-307 and V-308 (M-4404) approximately 15-20% to raise the level in V-308 to 35%. 2. When the level in V-308 reaches 35%, DCS operator will open LV-2126 to achieve a minimum flow rate of 100 m /hr. 3. As LV-2126 opens, the Field operator will quickly open the block valve between V-307 and V-308 (M-4404). 4. While one field operator opens M-4404 valve, another field operator shall immediately close the block valve between V-307 and V-306 (M-4403). 5. The DCS operator manually ramps up LV-2126 to a flow rate of 150-160 m /hr. his flow rate should keep the level in V-308 under control by establishing a steady flow of liquid to E-305. 6. Level controller LC-2126 must be put on automatic once levels are stabilized. 7. Monitor V-306 reboiler E-307 and E-308 retum temperatures and V-306 tower pressure. Adjust as necessary, but avoid sudden large changes in the controllers. 8. Slowly re-establish normal levels in V-303, V-304, V-307, and V-308. 3

3


Ethane Recovery Maximization (ERM) Project Performance Test Procedure Rev. 0



STARTUP of ERM Refrigeration System and Integration In The C2 Rejection Mode of Operation Rev. 0-May 19, 2005 ERM Refrigeration Compressor Startup and Switch to C2 Rejection Mode Refer to Compressor Startup Procedures, Section 10.2, Chapter 3, Operating, Maintenance and Safety Manual - Unit 44. Once the compressor is stable on recycle, a portion ofthe refrigeration load will be switched over from C-201 to C-202 by placing chiller 44-E-318 in service. The load to C-202 second stage will come from chillers 44-E-407 and 44-E-406. 1. Introduce propane refrigerant into 44-E-407, raising the level using LIC-2121. Set the level in 44-E-407 to target for a 44-E-407 tubeside outlet temperature of 0

20 to 25 C. 2. Ensure that the Debutanizer is operating at 15 barg. The temperature of 44-Vo

402, should be about 60 C. Begin raising the level of propane refrigerant in the Debutanizer Trim Condenser (44-E-406). 44-UC-2116 should be in MANUAL. As the level of propane is increased, the temperature of 44-V-402 will fall. The pressure of the Debutanizer will also begin to fall. Close the louvers of the Debutanizer Condenser (44-E-402) in order to maintain the temperature of o

44-V-402 at 60 C. Once the level of propane in 44-E-406 reaches normal, place 0

the controller in AUTO. The target outlet temperature for 44-E-402 is 66 C. C-202 compressor second stage should be close to being loaded at the completion of these two steps. 3. Introduce propane refrigerant into 44-E-318 to reduce the temperature in V-301 0

to -12 C. Increase the level in 44-E-318 using LIC-2111 to shift the refrigeration load from C-201 to C-202, keeping LV-2111 in manual. Once the level in E-318 reaches normal, place the controller in Auto. Position HS-5056 such that the temperature of V-301 is maintained by adjusting the load ofthe existing 0

refrigeration system via TIC-5056 and select a set point of -12 C. 4. The anti-surge valves for the new Propane Compressor, C-202, should be closed (44-FV-1402 and 44-FV-1403). If not, the load to the second stage can be increased by increasing the duty on 44-E-406 and decreasing the duty of the upstream air cooler, 44-E-402. The load to the first stage can be increased by


Ethane Recovery Maximization (ERM) Project Performance Test Procedure Rev. 0


increasing the load on 44-E-318 while decreasing the duty of the upstream exchanger (44-E-306) or by slightly opening the warm feed gas bypass valve M052. 5. The following controllers should be adjusted to new set points: 0

TIC-5056 (44-V-301) at -12 C 0

TIC-5061 (outlet of 44-E-313) at -21 C 0

TIC-5058 (bypass around 44-E-302) at -32 C 0

TIC-5067 (tube side outlet of 44-E-314) at -32 C 0

TIC-5080 (Recovery Tower bottoms) at -42 C 0

TIC-5207 (V-307 flash Vapor to E-302) at -43 C 0

TIC-5088 (V-306 Side Reboiler) at 45 C 0

TIC-5082 (V-306 Steam Reboiler) at 75 C 0

TIC-5081 (V-306 Overhead) at 3 C 0

TIC-5054 (Residue Gas from 44-E-301) at 22 C 0

TIC-5212 (Feed to V-401 Debutanizer) at 74 C 0

TIC-5127 (44-E-406 outlet) at 59 C PIC-3064 (V-401 Debutanizer Pressure) at 15.0 barg

6. Monitor the load on the Recycle G a s Compressor (44-C-301) and Demethanizer Reboiler (44-E-308). If either equipment item approaches its design duty, increase the set point of TIC-5080 (44-V-305 bottoms). Ensure that the isolation valve on the liquid line to 44-E-303 is open. These actions wili put Recovery Tower Reboiler into service and will reduce the amount of light ends sent to the Demethanizer system.

Fluor Mideast, L t d . Contract No. AOWT

Ethane Recovery Maximization (ERM) Project


STARTUP of ERM Refrigeration System and Integration Into Ca Enhancement Mode of Operation Rev. 0-May 18, 2005 ERM C-202 Refrigeration Compressor Startup While on pre-ERM C2 Enhancement Mode.

This procedure covers the startup of the new ERM refrigeration system and its integration into the existing (or pre-ERM) C2 Enhancement mode of operation. Unit 44 will remain in the pre-ERM C2 Enhancement mode of operation, but the refrigeration load will now be divided between C-201 and C-202 compressors. To transfer some of the refrigeration duty from C-201 to C-202, it will be necessary to adjust the duty on 44-E-402 and 44-E-306. These adjustments will result in new targets for the Debutanizer overhead air cooler, E-402, outlet temperature (TI-5124), the NGL product rundown temperature (TI-5121), and the E-306 outlet temperature (TI-5063). All other temperatures and pressures should remain the same.

I. Startup and Integration of ERM Refrigeration System Into Unit 44 Operations Refer to Compressor Startup Procedures, Section 10.2, Chapter 3, Operating, Maintenance and Safety Manual - Unit 44. Once the compressor is stable on recycle, a portion of the refrigeration load will be switched over from C-201 to C-202 by placing a cooling load on 44-E-318, 44-E-407 and 44-E-406. 1. Introduce propane refrigerant into 44-E-407, raising the level using LIC-2121. Set the level in 44-E-407 to target for a 44-E-407 tubeside outlet temperature of SOX. 2. Maintain Debutanizer pressure at 18 barg (PIC-3064). The temperature of 44-Vo

402 should be about 50 C. Slowly begin raising the level of propane refrigerant in the Debutanizer Trim Condenser (44-E-406). 44-LIC-2116 should be in MANUAL. As the level of propane is increased, the temperature of 44-V-402 will fall. The pressure of the Debutanizer will also begin to fall. Close the louvers of the Debutanizer Condenser (44-E-402) in order to maintain the


Ethane Recovery Maximization (ERM) Project


o

temperature of 44-V-402 at 50 C (TIC-5127). Once the level of propane in 44E-406 reaches normal, place 44-LC-2116 controller in AUTO. The target outlet o

temperature for 44-E-402 is 60 C. 3. Introduce propane refrigerant into 44-E-318 while maintaining the temperature in 0

0

V-301 at -14 C (TIC-5056 set at -14 C). HS-5056 should be positioned such that the temperature of V-301 is maintained by adjusting the load of the existing refrigeration system (C-201) via TIC-5056. Slowly increase the level in 44-E-318 using LIC-2111 to shift the refrigeration load from C-201 to C-202. 4. The anti-surge valves for the new Propane Compressor, C-202, should be closed (44-FV-1402 and 44-FV-1403). If not, the load to the second stage can be increased by increasing the duty on 44-E-406 and decreasing the duty of the upstream air cooler, 44-E-402. The load to the first stage can be increased by increasing the load on 44-E-318 while decreasing the duty of the upstream exchanger (44-E-306) or by slightly opening the warm feed gas bypass valve M052. 5. The actual set points in effect at the time of the start of C-202 compressor should be retained. The set points in effect on April 8, 2005, in C2 Enhancement mode are listed here for reference only. 0

TIC-5056 (44-V-301) at -14 C o

TIC-5061 (outlet of 44-E-313) at -20 C 0

TIC-5058 (44-V-302) at -34 C 0

TIC-5067 (tube side outlet of 44-E-314) at -36 C o

TIC-5080 (Recovery Tower bottoms) at -50 C 0

TIC-5207 (V-307 flash Vapor to E-302) at -49 C 0

TIC-5088 (V-306 Side Reboiler) at 33 C 0

TIC-5082 (V-306 Steam Reboiler) at 53 C o

TIC-5081 (V-306 Overhead) at -30 C 0

TIC-5054 (Residue Gas from 44-E-301) at 18 C 0

TIC-5212 (Feed to V-401 Debutanizer) at 63 C o

TIC-5127 (44-E-406 outlet) at 50 C PIC-3064 (V-401 Debutanizer Pressure) at 18.0 barg





A

2.0

TROUBLESHOOTING

2.1

ERM Refrigeration System Shutdown In the event of a shutdown of the new refrigeration package for any of the causes described in Section 2.2.2 of Chapter 4, the chilling of the feed gas in 44-E-318 will stop. Due to this, the temperatures of 44-V-301 and 44-V-302 will begin to warm-up. As the temperatures increase, ethane recovery decreases. After the trip of the new refrigeration system, the set points for TIC-5056 and TIC-5058 should be increased to their current settings (approximately - 9 C and -31 C respectively). Once the front-end of the unit has warmed-up, the set points of TIC-5082 and TIC-5088 should also be increased to their current settings in order to adjust the Demethanizer temperature profile (about 50 C and 70 C respectively). 0

0

o

o

After these changes, the unit will transition to its new steady state operating point. The unit can continue to be operated at these new conditions at the full feed gas rate. When the ethane recovery level falls below 30%, it may be necessary to re-route the stream from 44-E-314 to the existing Demethanizer (44-V-306) by opening the manual valve. The valve in the line to the new Cold Demethanizer (44-V-308) should then be closed. Monitor the flow from 44-P302A/B to determine when to divert the flow. The trip of the new refrigeration package will also impact the Debutanizer. Cooling to the Debutanizer Trim Condenser (44-E-406) and NGL Subcooler (44-E-407) will stop. Since the vessels in the unit (44-V-301, 44-V-302, 44-V-305, 44-V-306, 44-V-307, and 44-V-308) will contain an inventory of light components, the ethane content of the NGL to the Debutanizer will not immediately decrease. Therefore, there may be momentary venting of light components from the Debutanizer Overhead Accumulator (44-V-402) via PV-3068 while the unit transitions to the new operating point. Ventingfrom44-V-402 is a better option than attempting to change the temperature profile ofthe Demethanizer too quickly. Doing this may overload the recycle gas compressor and result in a larger unit upset. As the Unit transitions to the new steady state condition, it may be necessary to divert the E314 shell side outlet stream from V-308 to V-306. The flow from P-302 and the level in V308 should be monitored. Ifthe high flow alarm or high level alarm in V-308 is reached, manual valve M-4401 should be opened and M-4402 should be closed.

2.2

Trip of the Existing Refrigeration System In the event of a shutdown ofthe existing refrigeration package, the chilling of the feed gas in 44-E-306 will stop. Due to this, the inlet temperature to 44-E-318 will begin to warm-up. As the temperature increases, load on the E R M refrigeration package will increase. If the load approaches the limits of the compressor's electric driver, the C-202 performance controller will start to close the suction valves (PV-3402A/B). This will increase the pressure in E-318 which will increase the propane evaporation temperature and reduce heat transfer. This will prevent the new compressor from tripping. After the trip of the existing refrigeration system, the set points for TIC-5056 and TIC-5058 should be slowly increased to a value that results in the suction valves (PIC-3402A/B) completely open.

CHAPTER 5




The trip of the existing refrigeration system also results in the loss of cooling in 44-E-310. This will impact the performance ofthe mole sieve dehydrators. Refer to the existing Operating, Maintenance and Safety Manual for a description of this issue. 2.3

Other Trips Tag Number TALL-5126

Description E-314 Tube Side Outlet

Actions ESD logic can be reset and LV-2044 can be opened after: Feed gas flow to E-314 is firmly established or V-303 temperature is above -30 C. TIC-5058 is used to accomplish this. o

TALL-5131

E-313 Shell Side Inlet

ESD logic can be reset and XV-9080 can be opened after: 0

V-301 temperature increases to-15 C. TIC-5056 is used to accomplish this.

2.4

PALL-3084

P-302 Seal Pot

Check integrity of B Pump seal Start B Pump • If the level in V-308 rises to the High Alarm setpoint before the standby pump can be started, the liquid flow to V-308 should be diverted to V-306 by changing the positions of manual valves M-4401, M-4402, M-4403, and M-4404.

LALL-2127

V-308 Level

Check line-up of manual valves M-4401/2/3/4 Check position of LV-2126 Check position of LV-2044 Check position of FV-1204

Understanding Alarms Tag Number

Description

TAL-5068


TAH-5121


TAH-5124

V-401 Overhead from E402

CHAPTER 5

Actions Check position of TV-5067 Check position of LV-2044 Check propane level in E-407 via LI-2121 Check position of LV-2121 Check inlet temperature to E-407 via TI-5127 Check pressure of E-407 shell side via PI-3413 Check status of E-402 motors Check position of E-402 louvers



Tag Number


TAL-5131 TAH-5401

E-313 Shell Side Inlet C-202 Discharge

TAH-5404


TAH-5405


TAH-5410

E-203 Outlet

TAH-5416

Lube Oil Supply

TAH-5417 TAH-54XX

Lube Oil Reservoir C-202 Bearings

TAH-5423

C-202 Motor Stator

PAH-3081

V-308 Top

PAL-3081

V-308 Top

PDAH-3082

V-308 DP

PAL-3083

CHAPTER 5


Actions

Description

TAH-5127


Check propane level in E-406 via LI-2116 Check position of LV-2116 Check inlet temperature to E-406 via TI-5124 Check pressure of E-406 shell side via PI-3413 Increase setpoint of TIC-5056 (V-301) Check discharge pressure of C-202 via PI-3401 Check pressure of V-205 via PI-3410 Check status of E-203 motors Check position of E-203 louvers Check C-202 suction temperatures via TI-5404/5 Check position of anti-surge valves (FV-1402/3) Check position of quench valves (TV-5404/5) Check side load pressure via PI-3402 Check position of anti-surge valves (FV-1402/3) Check position of quench valve TV-5404 Check suction pressure via PI-3403 Check position of anti-surge valves (FV-1402/3) Check position of quench valve TV-5405 Check pressure of V-205 via PI-3410 Check status of E-203 motors Check position of E-203 louvers Check status of E1 motors Check position of TV-5415 Check temperature of TKI via TI-5417 Check status of E l motors Check LO temperature via local gauge Check supply temperature of LO via TI-5416 Check LO flow via local sight glasses Check LO pressure via PI-3417 and PI-3421 Check position of PC V-3418/3419 Check status of CM-202 blowers Check C-202 current Check C-202 performance controller PIC-3402 Confirm high pressure via PI-3051 Check flow via FI-1730 Check position of PV-8031 Confirm low pressure via PI-3051 Check flow via FI-1730 Check position of PV-8031 Confirm DP using PI-3081 and PI-3051 Check for signs of tower flooding Confirm low pressure using local gauge PG4111A/B Check pump running status Check suction pressure via PI-3081 Check position of FV-1070 Check position of LV-2126

P-302 Discharge

10



Tag Number PAL3084A/B

PAL-3401

C-202 Discharge

PAH-3402


PAL-3402


PAH-3403


PAL-3403


CHAPTER 5

Confirm low pressure with local gauge PG4117AJB Check integrity of seal Add barrier fluid to seal pot Confirm high pressure using local gauge PG-4402 Check pressure of V-205 via PI-3410 Check status of E-203 motors Check position of E-203 louvers Check position of hot vapor bypass PV-341 OA Check C-202 suction pressures via PI-3402/3 Consider venting non-consensables using HIC9092 • If pressure is high and all else is normal, reduce the load on the system. Confirm high pressure using local gauge PG-4402 Check pressure of V-205 via PI-3410 Check status of E-203 motors Check position of E-203 louvers Check position of hot vapor bypass PV-341 OA Check position of vent to flare PV-341 OB & HIC9092 Check C-202 suction pressures via PI-3402/3 • If pressure is low and all else is normal, slowly close E-203 louvers to increase the propane condensing temperature/pressure. Confirm high pressure using local gauge PG-4406 Check flow via FI-1402 Check position of anti-surge valve FV-1402 Check discharge pressure PI-3401. Confirm low pressure using local gauge PG-4406 Check flow via FI-1402 Check position of PV-3402A Check position of anti-surge valve FV-1402 Check discharge pressure PI-3401. Confinn high pressure using local gauge PG-4405 Check flow via FI-1403 Check position of anti-surge valve FV-1403 Check side load pressure via PI-3402 Check discharge pressure PI-3401. Confirm low pressure using local gauge PG-4405 Check flow via FI-1403 Check position of PV-3402B Check position of anti-surge valve FV-1403 Check side load pressure via PI-3402 Check discharge pressure PI-3401

P-302 Seal Pot

C-202 Discharge


Actions

Description

PAH-3401


11



Description

Tag Number PAH-3410

V-205

PAL-3410

V-205

PAH-3413

V-206

PAH-3414

V-207

PAL-3415

LO Pump Discharge

PDAH-3416 PAL-3417

LO Supply at LO Skid

PAL-3421

LO Supply at Compressor

Seal Gas Filter DP

PDAH-3431

Seal Gas Filter DP

PDAH-3432

Balance Chamber DP

CHAPTER 5


Actions

LO Filter DP

PDAH-3430


12

Confirm high pressure using local gauge PG-4403 Check discharge pressure of C-202 via PI-3400 Check status of E-203 motors Check position of E-203 louvers Check position of hot vapor bypass PV-341 OA Consider venting non-consensables using HIC9092 Confirm high pressure using local gauge PG-4403 Check discharge pressure of C-202 via PI-3400 Check status of E-203 motors Check position of E-203 louvers Check position of hot vapor bypass PV-3410A Check position of vent to flare PV-341 OB & HIC9092 • If pressure is low and all else is normal, slowly close E-203 louvers to increase the propane condensing temperature/pressure. Confirm high pressure using local gauge PG-4416 Check flow via FI-1402 Check position of PV-3402A Check position of anti-surge valve FV-1402 Check discharge pressure via PI-3401 Confirm high pressure using local gauge PG-4410 Check flow via FI-1403 Check position of PV-3402B Check position of anti-surge valve FV-1403 Check side load pressure via PI-3402 Confirm low pressure using local gauge PG4115A/B Check pump running status Check position of PCV-3419 Check position of PCV-3418 Confirm high DP with local gauge PDG-4417 Change to spare filter Confirm low pressure using local gauge PG-41 U Check LO pump running status Check position of PCV-3419 Check position of PCV-3418 Confirm low pressure using local gauge PG-41 IS Check LO pump running status Check position of PCV-3419 Check position of PCV-3418 Confirm high DP with local gauge PDIT-3430 Change to spare filter Confirm high DP with local gauge PDIT-3431 Change spare filter îiau&c to iu spaic unci Confirm high DP using local gauge PDIT-3432 Check integrity of balance piston


Tag Number


Description

PAL-3433

Buffer Gas

FAH-1070

P-302 flow

FAL-1070

P-302 flow

FAH-1400

C-202 Discharge

FAL-1400

C-202 Discharge

FAH-1402

C-202 Side Load

FAL-1402

C-202 Side Load

FAH-1403

C-202 Low Stage

FAL-1403

C-202 Low Stage

FAH-1430

Primary Seal Gas

FAL-1430

Primary Seal Gas

CHAPTER 5


Actions Check nitrogen header pressure Check position of valve PCV-3437 Check local gauges (FI-1438/9) for flow Confirm high flow using local indicator FI-1070 Check level in V-308 via LI-2126 Check position of valve FV-1070 Check position of valve LV-2126 • If flow is high and all else is normal, re-direct flow from E-314 to V-306 by opening M 4401 and closing M-4402. Confirm low flow using local indicator FI-1070 Check level in V-308 via LI-2126 Check position of valve FV-1070 Check position of valve LV-2126 Check position of FV-1402/3 Check flow of propane to E-318/406/407 Check position of PV-3402A/B Check performance of chillers Check position of FV-1402/3 Check flow of propane to E-318/406/407 Check position of PV-3402A/B Check performance of chillers Check position of FV-1402 Check position of PV-3402A Check propane flow to E-406/7 via FI-1411 Check position of LV-2116/2121 Check performance of E-406/7 Check position of FV-1402 Check propane flow to E-406/7 via FI-1411 Check position of LV-2116/2121 Check performance of E-406/7 Check position of FV-1403 Check position of PV-3402B Check propane flow to E-318 via FI-1412 Check position of LV-2111 Check perfonnance of E-318 Check position FV-1403 Check propane flow to E-318 via FI-1412 Check position of LV-2111 Check performance of E-318 Confirm high flow using local gauges Check position of FV-1430 Confirm low flow using local gauges Check position of FV-1430 Check DP across inlet filter

13


Tag Number FAL-1431


Description

Primary Seal Flow

FAL-1432D

Primary Seal Flow

LAH-2111

E-318 Level

LAL-2111

E-318 Level

LAH-2116

E-406 Level

LAL-2116

E-406 Level

LAH-2121

E-407 Level

LAL-2121

E-407 Level

LAH-2126

V-308 Level

LAL-2126

V-308 Level

LAH-2403

V-205 Level

LAL-2403

V-205 Level

CHAPTER 5


Actions Confirm low flow using local gauges Check position of FV-1431 Check DP across inlet filter Check nitrogen header pressure C.hpck f l o w of n f spfll eras mine* Check flow seal gas using FTFI-1430 Check integrity of primary seal. Check flow of seal gas using FI-1430 Check integrity of secondary seal (low primary seal flow may be a sign of degradation of the secondary seal) Confirm high level using local gauge LG-2110 Check position of LV-2111 Check position of XV-7401 Check position of HV-7210 Confirm low level using local gauge LG-2110 Check position of LV-2111 Confirm high level using local gauge LG-2115 Check position of LV-2116 Confirm low level using local gauge LG-2115 Check position of LV-2116 Confirm high level using local gauge LG-2120 Check position of LV-2121 Confirm low level using local gauge LG-2120 Check position of LV-2121 Confirm high level using local gauge LG-2125 Check position of LV-2126 Check running status of P-302 Check position of FV-1070 Check position of XV-9081 • If level is high and all else is normal, re-direct flow from E-314 to V-306 by opening M 4401 and closing M-4402. Confirm low level using local gauge LG-2125 Check position of LV-2126 Check positions of M-4401/2/3/4 Check running status of P-302 Confirm high level using local gauge LG-2413 Check position of propane supply valves (LV2111, 2116, 2121) Check level in chillers (LI-2111, 2116, 2121) Confirm low level using local gauge LG-2413 Check position of propane supply valves (LV2111, 2116, 2121) Check level in chillers (LI-2111,2116,2121) Check position of hot vapor bypass (PV-341 OA)

Secondary Seal Gas

FAH-1432D


14


Tag Number


Description

LAH-2404

V-206 Level

LAL-2404

V-206 Level

LAH-2405

V-207 Level

LAL-2405

V-207 Level

LAL-2420 LAL-2431

LO Rundown Tank LO Reservoir

CHAPTER 5


Actions Confirm high level using local gauge LG-2414 Check position of LV-2404 Check position of TV-5404 Check level in E-406/7 via LI-2116/2121 Confirm low level using local gauge LG-2414 Check position of LV-2404 Confirm high level using local gauge LG-2415 Check position of LV-2405 Check position of TV-5405 Check level in E-318 via LI-2111 Confirm low level using local gauge LG-2415 Check position of LV-2405 Check position of fill valve. Confirm low level using local gauge LG-2430 Check LO flow using local sight glasses Check the all drains are closed.

15


3.0


GASCO ProjectNo.': 13522102 Doc. No.: PP-AOWT-44-00-001

TRANSITION TO REDUCED C2 RECOVERY MODES This procedure assumes that Unit 44 is running in E R M C2 Recovery Mode (40% C2 recovery) at steady state conditions. General Overview When reducing the ethane recovery level, the temperature profde around the cold box (44-V301 and 44-V-302) should be adjusted using TIC-5056 and TIC-5058 prior to adjusting the temperature profile of the Demethanizer. This will prevent the recycle compressor loop from being overloaded. The Debutanizer operating conditions are changed last to avoid venting of light components from the accumulator. Controller set points for ethane recovery values of 30%, 20%, and 10% are provided in Table 2.1 and 2.2a in Chapter 4. Set points for ethane rejection are also provided in the tables. Changes to the ethane recovery level should be done gradually allowing for unit stabilization at intermediate points. Stepwise Instructions • Gradually increase the temperature in 44-V-301 via TIC-5056 to the value corresponding to the target ethane recovery level. •

The temperature of 44-V-302 will increase. Adjust the set point of TIC-5058 to the proper value.

•

Increase the set point of TIC-5207 to the proper value.

•

Adjust the Demethanizer temperature profile using TIC-5082 (bottom reboiler) and TIC5088 (side reboiler).

o

As ethane recovery decreases, the steps are required:

CHAPTER 5

•

The flow of reflux to the Debutanizer will need to be increased to maintain the C5+ specification.

•

The required duty of the Debutanizer Trim Condenser (44-E-406) will decrease. The duty can be adjusted by changing the set point of TIC-5121 or decreasing the propane level in the exchanger using LIC-2116.

•

At ethane recovery levels around 20%, the stream from 44-E-314 should be redirected to 44V-306 by opening the manual valve. The valve in the line from 44-E314 to 44-V-308 should be closed. The switch should occur when the flow from 44P-302 approaches 265 m3/h.

•

At ethane recovery levels around 10%, the isolation valve for the recycle gas to 44-E315 should be open. The recycle gas bypass around 44-E-315 should be closed. The switch should occur when the Demethanizer Reboiler approaches its design duty.

•

In ethane rejection mode, the Recovery Tower Reboiler is required (44-E-303). The block valve in the liquid line to the exchanger should be opened. The new recycle gas bypass for44-E-303 that is located near44-E-301 and 44-E-302 should be closed.

•

At low ethane recovery levels, the operating pressure of the Debutanizer can be reduced.

16




CHAPTER 6

NORMAL SHUTDOWN

CONTENTS

SECTION

PAGE

1.0

GENERAL

2

2.0

TRANSITION TO C3 MODE

2

3.0

STOP THE ERM REFRIGERATION SYSTEM

2

CHAPTER 6


1.0



GENERAL The majority of the nonnal shutdown procedure contained in Chapter 6 ofthe existing Operating, Maintenance and Safety Manual is applicable to the modified unit. Any differences are highlighted in this section. In all shutdowns, the new Cold Demethanizer would be shutdown with the existing Demethanizer. Prior to the shutdown, the liquid inventory in the Cold Demethanizer would be reduced the operational minimum (low level alarm).

2.0

TRANSITION TO C3 MODE Before shutdown, Unit 44 should be transitioned to C3 mode using the procedure defined in Section 2.2 of Chapter 5 in this manual. Once the unit has stabilized in C3 Mode, the new E R M exchangers should be taken out of service by switching the level controllers into manual and closing the level control valves. ERM Exchanger

Controller

44-E-318

44-LIC-2111

44-E-406

44-LIC-2116

44-E-407

44-LIC-2121

Once the level control valves are closed, all of the propane in the exchangers will vaporize and the will Propane Compressor (44-C-202) will be operating in full recycle.

3.0

STOP THE ERM REFRIGERATION SYSTEM Once the process exchangers have been decoupled from the refrigeration system, the inventory of liquid propane in exchangers 44-E-204 and 44-E-205 should be reduced to a minimum. The level controllers should be switched into manual and the level valves closed. A l l ofthe propane from the exchangers will end up in 44-V-205. Monitor the level in 44-V205 to ensure that the drum is not over filled. At this stage, the compressor is ready to be stopped. General procedures and actions associated with shutting down the compressor are shown below. Refer to the detailed instructions from the vendor for more information. •

Stop the compressor using 44-HS-9451

o

LV-2404, LV-2405, LV-2111, LV-2116, LV-2121 will move to their safe positions (closed)

•

The anti-surge valves (FV-1402 and FV-1403) will open fully

•

The quench valves close (TV-5404 and TV-5405)

CHAPTER 6




The normal stop button will not close the ESD valves which isolate the compressor. If isolation is required, the ESD valves can be closed with the local push buttons. The ESD valves are: 44-XV-7400: 44-C-202 discharge 44-XV-7401: Side load vapor 44-XV-7402: Suction vapor Depending on the nature and duration of the shutdown, it may be necessary to also shutdown the auxiliary systems. The refrigeration system can be depressurized to the Cold Flare system using the relief valve bypass lines and the depressurization valve in the compressor discharge (XV-7405). Purging the hydrocarbons out is done using the procedure described in the existing Operating, Maintenance and Safety Manual. Before any maintenance can be done on the compressor, it is critical that the compressor is properly isolated (valves and blinds), drained, depressurized and inerted.

CHAPTER 6




CHAPTER 7 EMERGENCY SHUTDOWN CONTENTS SECTION

PAGE

1.0

GENERAL

2

2.0

UTILITIES FAILURE

3

2.1 2.2 2.3 2.4 2.5 2.6

Loss of Electrical Power Loss of Steam Loss of Instrument Air Loss of Nitrogen Loss of Cooling Water Loss of Fuel Gas

3 3 3 3 3 3

UNIT SHUTDOWN INTERLOCKS

4

3.1 3.2

4 4

3.0

CHAPTER 7

ESD System - Level 1 ESD System - Level 2



1.0


GENERAL The emergency shutdown philosophy used in the design ofthe E R M system is consistent with the existing unit. The new ERM shutdowns are divided into two categories: Level 1: Local shutdown involving an individual item affected by an upset condition, but not affecting other items. Level 2: Provides protection against certain critical process upsets conditions. This is a system shutdown including a number of items or complete systems.

CHAPTER 7



2.0

UTILITIES FAILURE

2.1

Loss of Electrical Power


In the event of a total power failure, the Propane Compressor (44-C-202), Cold Demethanizer Bottoms Pump (44-P302A or B), Propane Condenser fans (44-E-203), lube oil pumps, and lube oil cooler fans will stop. The unit will have to be shutdown according to the procedure in the existing manual. 2.2

Loss of Steam The E R M Project does not add any new steam users. Refer to the existing manual for a description of this case.

2.3

Loss of Instrument Air In the unlikely event of a loss of instrument air, all new control valves will move to their fail safe positions. Depending on the duration of the instrument air failure, the unit will need to be shutdown following the procedures contained in the existing manual. The Propane Compressor (44-C-202) will be shutdown. The Propane Condenser fans and Cold Demethanizer Bottoms Pump can continue to operate.

2.4

Loss of Nitrogen Nitrogen is used in the new Propane Compressor seal system (secondary seal fluid and buffer gas). A loss of nitrogen will result in several alarms: FAL-1431: FAL-1432D: FAL-1433D: PAL-3433:

Low Low Low Low

flow of Secondary Seal Gas primary vent flow (suction side) primary vent flow (discharge side) buffer gas pressure

Operating the compressor without nitrogen is not recommended. If the outage lasts for more than two hours, the compressor should be stopped to avoid damage to the labyrinths. It will not be possible to re-start the lube oil pump of the compressor until buffer gas pressure is re-established. 2.5

Loss of Cooling Water The E R M Project does not add any new cooling water users. Refer to the existing manual for a description of this case.

2.6

Loss of Fuel Gas The E R M Project does not add any new fuel gas users. Refer to the existing manual for a description ofthis case.

CHAPTER 7



3.0


UNIT SHUTDOWN INTERLOCKS There are many emergency situations that may cause all or part ofthe unit to be shutdown by means of the automatic Emergency Shut Down (ESD) system. The major new shutdowns added as a part ofthe E R M Project are described below. Some ofthe ancillary shutdowns and local controls which are part ofthe equipment vendor's scope are not shown. Refer to the Process Cause and Effect charts in Section 2.2 of Chapter 4 for additional information on these shutdowns.

3.1

ESD System - Level 1 Low-Low Level Detection Cause: Low-low level in the Cold Demethanizer, 44-V-308 (LALL-2127) Effect: Cold Demethanizer Pumps (44-P-302A/B) tripped Low-Low Temperature Detection Cause: Low-low temperature at shell side inlet to 44-E-313 (TALL-5130) Effect: Close XV-9080 and LV-2111 Cause: Low-low temperature at shell side outlet of 44-E-314 (TALL-5126) Effect: LV-2044 moved to safe position (closed) Low-Low Pressure Detection Cause: Low-low seal pressure in P-302A/B seal system (PALL-3084A/B) Effect: 44-P-302A/B stopped High-High Vibration Detection Each fan of 44-E-203 is equipped with a high vibration switch which trips the motor when high vibration is detected.

3.2

ESD System - Level 2

3.2.1

E R M Refrigeration System The E R M refrigeration system is shutdown in the event of any of the following: • • • • • • • • • • •

High-high level in 44-V-206 (LAHH-2401) High-high level in 44-V-207 (LAHH-2402) High-high 44-C-202 discharge temperature (TAHH-5400) High-high 44-C-202 bearing temperature High-high 44-C-202 discharge pressure (PAHH-3400) Low-low 44-C-202 suction pressure (PALL-3405) Low-low 44-C-202 side load pressure (PALL-3404) Low-low lube oil pressure (PALL-3420) High-high C-202 vibration High-high C-202 axial displacement High-high C-202 gear acceleration

The Level 2 shutdown for the compressor system results in the following actions:

CHAPTER 7



•

CM-202 trip

•

ESD valves to safe position:


44-XV-7400 closed (C-202 discharge) 44-XV-7401 closed (C-202 suction) 44-XV-7402 closed (C-202 side load) •

Control valves to safe position: nd

44-FV-1402 open (2 stage anti-surge) 44-FV-1403 open (1 stage anti-surge) 44-LV-2111 closed (liquid to 44-E-318) 44-LV-2116 closed (liquid to 44-E-406) 44-LV-2121 closed (liquid to 44-E-407) 44-LV-2404 closed (liquid to 44-E-204) 44.LV-2405 closed (liquid to 44-E-205) 44-PV-3402A open (C-202 side load) 44-PV-3402B open (C-202 suction) 44-TV-5404 closed (quench to 2 stage) 44-TV-5405 closed (quench to l stage) st

nd

51

An ESD button in the main control room (44-XS-9467) has also been provided for the compressor system. This button results in all ofthe above action plus trips the lube oil pumps and lube oil cooler fans. The compressor system can also be automatically shutdown and depressured by activation of the following: • • • •

High-high primary seal vent flow, suction side (FAHH-1432) High-high primary seal vent flow, discharge side (FAHH-1433) 44-XHS-9466 (IES) 44-XHS-9469 (local)

These trips cause all of the effects described above plus open ESD valve 44-XV-7405 to depressurize the compressor. 3.2.2

Unit 44 and Zone 20 Shutdowns The existing Unit 44 and Zone 20 shutdowns include the following new actions: e • • .

CHAPTER 7

C-202 trip (including all actions listed in Section 3.2.1 except 44-XV-7405) 44-P-302AyB shutdown 44-E-203 shutdown 44-XV-9081 closed




CHAPTER 8

SAFETY

CONTENTS

SECTION 1.0

GENERAL.

CHAPTER 8

PAGE 2



1.0


GENERAL The fire, explosion, and toxic hazards present in Unit 44 after the implementation of the E R M Project are identical to those described in the existing Unit 44 Operating, Maintenance and Safety Manual. The updated safety drawings, including the drawing showing location of the new flammable gas detectors, are provided in Chapter 10 of this manual.

CHAPTER 8




CHAPTER 9

EQUIPMENT AND DATA SHEETS

CONTENTS

SECTION

PAGE

("AS-BUILT" DATASHEETS TO BE INSERTED WHEN AVAILABLE)

CHAPTER 9



Ethane Recovery Maximization (ERM) Project Equipment List Rev.2

Doc. No.: NM-A0W-M4-06-001

ETHANE RECOVERY MAXIMIZATION (ERM) PROJECT Equipment List Revision 2

Approved Rev.

Date

22-Mar-04 15-Sep-03

Description

Approved for Construction Approved for Design

By

Chk.

Disc.

Proj.

"^7 2>

DWM

GASCO

FLUOR Contract AOWT Date: 22-Mar-04, Rev. 2 By: DTS / OPM / PL CHK: ED

ETHANE RECOVERY MAXIMIZATION Rel: 13522102 OGD-I Train 3 - Unit 44 EQUIPMENT LIST - VESSELS

Rev

Item No.

Descripiion

Criticality

Inside

Rating

Diameter

Design T/T

44-

V-402

44-

V-205

Propane Receiver

2.7

44-

V-206

High Pressure Knockout Drum

2.3

44-

V-207

Low Pressure Knockout Drum

1.7

Equipment List - Unit 44 - Rev 2.xls

2.5

Operating

Temp

barg

m Debutanizer Overhead Accumulator

Press

Press

Materials of Construction

Orient.:

Requistion

Ih/lc

Hor./Vert.

Manulacturer

90/-29

18

29

CS

22/FV

90/-45

19

55

LTCS

6.1

22/FV

85 / -45

6.4

16

LTCS

6.1

22/FV

85 / -45

-24

LTCS

1 OF 8

Remarks

P&ID

barg

20

10.0

Insul.:

Ic 40 mm

Ic

50 mm

02 0810 06 Add insulation to existing vessel. JENKINS Remove inlet distributor. 44 00 30 028 2 4-0701-01 Part of Refrigeration Package Horizontal Toromont 44-ME-201. 22717-104 Horizontal

Horizontal

Ic Horizonta 100 mm

4-0701-01 Toromont 22717-103 4-0701-01 Toromont 22717-102

Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201.

FLUOR

WD'

Contract AOWT Date: 22-Mar-04, Rev. 2 By: DTS / OPM / PL CHK: ED

ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 • Unit 44 EQUIPMENT LIST - HEAT EXCHANGERS Criticality Rev

Item No.

Descripiion

Rating

Design

Shell Design

Duty

Press

Gcal/h

barg

Temp

Tube Design Press

Materials Of Constmction

Temp

barg

Shell

Tubes

Exch. Type

Requistion Total Suriace No. Series Manufacturer XNo. Area.m' P&ID Parallel

44- E-318

2ncl Feed Chiller

3.15x 1.1

22/FV

85 / -45

75

85 / -45

LTCS

LTCS

BKU

644

1x 1

44-

E-406

Debutanizer Trim Condenser

6.79 x 1.1

22/FV

85/-45

20

90/ -29

LTCS

LTCS

BKU

605

1x 1

44-

E-407

N G L Subcooler

0.92x1.1

22/FV

8 5 / -45

30

90/-29

LTCS

LTCS

BKU

206

1x 1

85/-45

LTCS

LTCS

BXU

456

1x 1

85 / -45

LTCS

LTCS

BXU

111

1x1

High Temperature Subcooler

44-

E-205

Low Temperature Subcooler

44-

C-202 E2A/B

Lube Oil Healer


0.78 x 1.1

22/FV

8 5 / -45

22

ELEC.

2 OF 8

Remarks

Kettle ID = 1.76 m, Tube Length = 6.1 m 4-0401-01 Energy Exch. Cold insulation: S S = 220 mm thk. T S = 44 00 30 019 2 160 mm thk. Kettle ID = 1.83 m, Tube Length = 6.1 m 4-0401-01 Energy Exch. Cold insulation: S S = 100 mm thk. T S = 44 00 30 028 1 40 mm thk. 4-0401-01 Energy Exch. 44 00 30 028 3 4-0701-01 Toromont 22717-103

Kettle ID = 1.17 m, Tube Length = 6.1 m Cold insulation: S S = 100 mm thk. TS = 40 mm thk. Part of Refrigeration Package 44-ME-201. Bundle ID = 1.07 m, Tube Length = 6.1 m Cold insulate both T S & S S , 50 mm thk.

4-0701-01 Toromont 22717-102

Part of Refrigeration Package 44-ME-201. Bundle ID = 0.61 m, Tube Length = 6.1 m Cold insulate both T S & S S , 100 mm thk.

4-0701-01 Toromont 10512S

Part of Refrigeration Package 44-ME-201 Electric heaters = 2 x 4.5 kW


ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 - Unit 44 EQUIPMENT LIST - AIR COOLERS

Item No.

Rev

44-

Description

E-203

Propane Condenser

C-202E1 A/B/C

Oil Cooler


Design Conditions

Criticality

Design

Process

Operating

Rating

Duty

Flow rate

Inlet Temp

Gcal/h

Kg/hr

ban

15.13x1.1

217600

22

0.082

9870

13.8

77

Press

Temp

Materials Of Construction

Bare Surface Area, rr?

Requistion Total Fan No. of Bays Power, / Bundles Manufacturer KW P&ID

Header

Tubes

91 (hot) -45 (cold)

LTCS

LTCS

5936

18x 30kW

121 (hot) 5 (cold)

SA-516 GR70

SA-214 WLD

53.5

3x 3.7kW

30F8

9/18

Remarks

Exisling supplus Item (45-E-701) used in new service. Tube Lengths 12.2 m 44 00 30 041 Total Width = 18 x 3.6 m GEA-BTT

4-0701-01 Toromont 10512S

Part of Refrigeration Package 44-ME-201


ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 - Unit 44 EQUIPMENT LIST - COLUMNS

llem No.

Rev

Description

Criticality

Inside

Rating

Diameter

Press Part

44-

V-308

Cold Demethanizer


2.4

Operating

Design T/T

12.8

28/FV

Temp

°C 85/-100

Temp

Press


barg

"C

Shell

Internals

23.3

-36 Top -19 Bot

304 L

304 L

4 OF 8

Insul.:

Ih/lc

Requistion

Tray Type

Manulacturer

Remarks

P&ID Ic 220 mm

8 Valve Trays

4-0201-01 Fireproof exterior of skirt. Trays supplied KNM by Sulzer. 44 00 30 023 4

FLUOR

Mi E T H A N E R E C O V E R Y MAXIMIZATION

Contract A O W T

Ref: 13522102

Date: 22-Mar-04, R e v . 2 By: D T S / O P M / P L

CHK: ED

OGD-I T r a i n 3 - U n i t 4 4 E Q U I P M E N T LIST - P U M P S

Rev

Item No.

44-

Description

P-302 A/B


C-202P1 A/B

Oil Pumps


Criticality

Rated

Pump

Rating

Capacity

Head

Temp

Press

m3/h

m

°C

bai ar^

202x 1.3

61

-100

35.5

23.6

5.2 barg

Design Conditions

piujp Density, kg/ma

850

Materials of Construction Casing

Impeller

316L

316L

Cast Steel

5 OF 8

PumpType

Driver: Motor or turbine

45

centrifugal

Screw

Esfd Driver kW

motor

15

Requistion Pump Eff. % Manufacturer P&ID 4-0801-01 Sulzer 44 00 30 023 4-0701-01 73.3 Toromont 10512S 70.7

Remarks

One operating and one spare. API A-8 Seal Plan 53B. C2 Rejection mode is controlling (240 m3/h). Part of Refrigeration Package 44-ME201. One operating and one spare.

FLUOR

(MM

Contract AOWT Date: 22-Mar-04, Rev. 2 By: DTS / OPM / PL CHK: EC

ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 - Unit 44 EQUIPMENT LIST - COMPRESSORS Criticality Description

Rating

Design Flowrate Actual mS/tir 11900

44- C-202

Propane Compressor


Molecular Weiaht

Suction Condiiions

barg 44.0

Temp

Discharge Pressure

'C

barg 6.3

14900

Design Conditions

22 barg Casing: LTCS 105*0 (hot) Internals: LTCS -45' C (cold) >

60F8


Compr. Type

centrifugal

Driver: Motor or turbine

Requistion Esfd Driver Manufacturer kW P&ID 5800

4-0701-01 Toromont 22717-101

Remarks Part of Refrigeration Package 44-ME-201. Spare rotor provided


ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 • Unit 44 EQUIPMENT LIST - TANKS Criticality Rev

Item No.

Description

Rating

Diameter

Operating

Design

Inside T/T

Press

Temp

C-202 TK-1

C-202 44- TK-2

Lube Oil Reservoir

Lube Oil Rundown Tank


Insul.: Ih/lc

Orient.:

Requistion

Hor./Vert.

Manufacturer

2.2 L 1.5 W

1.4 H

ATM.

0.5

1.8

ATM.

317LSS

316L

93

7 OF 8

Remarks

P&ID

barg

m 44-

Press

Materials of Constnjction

Vert.

4-0701-01 Toromont 10512S 4-0701-01 Toromont 16-440-901-526

Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201.

FLUOR Contract AOWT Date: 22-Mar-04, Rev. 2 By: DTS / OPM / PL CHK: E[

ETHANE RECOVERY MAXIMIZATION Ref: 13522102 OGD-I Train 3 - Unit 44 EQUIPMENT LIST - MISCELLANEOUS Requistion

Criticality Rev

Item No.

Description

Duty Specification

Rating

Manufacturer

Remarks

P&ID

44- C-202-X1

44-

C-202GB-202

44- Y-202

Lube Oil Console

C-202 Gearbox

Overhead Travelling Crane

44-

C-202F1 A/B

Lube Oil Filters

44-

C-202F2 A/B

Primary Seal Gas Filters

C-202F3 A/B

Secondary Seal Gas Filters

44-

44-

CM-202CM-202 Motor Air BL1 A/B/C Blowers


API-614 Lube Oil Console Containing: Lube Oil Reservoir (44-C-202-TK1) Lube Oil Filters (44-C-202-F1A/B) Lube Oil Pumps (44-C-202-P1A/B) Lube Oil Heater (44-C-202-E2A/B) Lube Oil Cooler (44C-202-E1A/B/C) API-613 Gearbox and API-671 Coupling Rated Capacity = 12,000 kg Span = 12 m Lift = 9 m Crane Travel = 44 m Cartridge Type, 10 micron, 316SS elements Design pressure = 16.2 barg Design temperature = 100°C 316 SS construction, 1 micron, glass fiber elements Design pressure = 24 barg Design temperature = -45°C 316 SS construction, 1 micron, glass fiber elements Design pressure = 24 barg Design temperature = -45 C 0

Cooling for CM-202 (TEAAC type). 3 x 10 kW motors.

8 OF 8

4-0701-01 Toromont

Part of Refrigeration Package 44-ME-201.

10512S 4-0701-01 Toromont 4-0801-02 J. Barnsely Cranes 4-0701-01 Toromont 10512S 4-0701-01 Toromont 16-440-938-561

4-0701-01 Toromont 16-440-938-561

Part of Refrigeration Package 44-ME-201. Spare gear set provided. Existing surplus crane (45-Y-101) modified for this new service. This service replaces existing 6T (Y001) crane. Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201. Part of Refrigeration Package 44-ME-201.

4-0701-01 Part of Refrigeration Package Toromont 44-ME-201. M68D100087




CHAPTER 10

DRAWINGS

CONTENTS

SECTION

("AS-BUILT" DRA WINGS TO BE INSERTED WHEN AVAILABLE)

CHAPTER 10

PAGE

^-393 1ST STAGE LIDUiD FLASH ORUH s.... mm . sua m IT Dtiip

f

x 'S BSW/ Full

FEED CHILLER

1ST STAGE LIOU1D/FEEO EXCHfiWDER

flEFR 1 LiRAliT FLASH DRUH £.» i IESS m m . 4e3a HH II P

1KM h n ^ r : » . [ ] ) O.n^

is

i ?3 B M C ' F J ] V e c w i

EJ«:

Tub. > 75 EWC I ! S M I t 1ST / ' ' S T Tvb* i 1ST / - ( S T ISl SIC.FLnSM

..•IW-^ll-H-£

" H i

VWW

^ I S l STC. FLOS" IIOUIB TO " E - J I S

FLUOR. 5. L l M * I E. l l

13 EE F E S i m E ••KK BT.PMS V«LVE,

r W I 13 PT I S « M i E F R >

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ETHANE RECOVERY MAXIMIZATION PROJECT PIPING AND INSTRUMENT DIAGRAM NGL RECOVERY - UNiT 44 THAMMAMA ' F ' OEBUTANIZER CONDENSERS TK]S Wfi*IMG TSSUED FOR T-Ê WlO/OR T I C CCD HEVISED FOR

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r» ANO M K N O ( H A U . COMPLY W I M IEC ANO B f L A i E l i D ACCORDtMM.*. C i f m n C A T E l M E Q U U D . 1. UENTLY AW4CREO CABLE SHALL OE S£CUR£DTO COMPfiESSOR H H E P E P R A C I K M . UWM) IrtUJN C O . T t D O S M R E H E I , H A N d T Ofl E O l i l * .

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TYPICAL. CONNECTION OF BENTLY NEVADA EOUIPMEMT

IT P O O r O W UONTIOR S E T P O K T t

MBRATWWTTRUaT PROOEB. K E Y m A W R S )

M BTtAOT-STATE C E A A T I O N

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MOTOR AA-CM-2Q2

•

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3

3 3

3 3 3

3 3

3 3

3 3

3 3

3 3 3

3

3 3

3 3 3 3 3 co«cncN-oi-

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3

6

i \ BEm'LY NEVADA SMO SYSTEM VIBRATION RACK

cowjEcnwor |

BENTLY NEVADA 3500 SYSTEM VIBRATION RACK

I

I

I

ALL INSTRUMENT TAGS TO BE PREFIXED WITH BILL OF MATERIAL

18-UW25-213

I.E.. «TE6«7A.

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K«8»«H*aOOMi R Wn O W A T K X • C M P R Z U O f l

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NOTES: 1. RELAYS ARE NORMALLY ENERGIZED AND WLL BECOME OE-ENERGIZED FOR AN ALERT OR DANGER COM51TION. JUNCTION flOX ON MOTOR J-BOX U4TM52

2. TEMPERATURE ELEMENTS FURNISHED IN THE COMPRESSOR, GEAR, ANO MOTOR ARE IOO OHM ft C C , 3 WIRE PLATINUM RESISTORS. TYPICAL COMPRESSOR RTD ELEMENT CONNECTIONS A R E

JUNCTION BOX ON UOTOR J-BOX M 4 T M M 3. COMPRESSOR BEARING RTD LEADS SHALL BE CONTINUOUS FROM ELEMENT TO COMPRESSOR MOUNTED JUNCTION BOX. RTD LEADS SHALL BE RUN IN COPPER FREE ALUMINUM CONDUfT. CONDUIT SHALL ENTER JUNCTION BOX FROM BOTTOM ONLY. JUNCTION BOX TO INCLUDE EXTERNAL AND INTERNAL GROUNDING LUG.

•'-•r.

TEMJ1A

[

TES421B

[

SPARE 4. RECOMMENDED COMPRESSOR BEARING TEMPERATURE MOWTOR SETPOIMTS: A.

SETPOINTS OF THE COMPRESSOR TEMPERATURE MONITOR TO BE I NITI ALLY SET AT BCC FOR ALARM 1 AND U V C FOR ALARM 2.

M

TYPICAL RTD CONNECTION BENTLY NEVADA TEMPERATURE MONITOR

SPARE

AFTER NORMAL OPERATION IS ESTABLISHED. SET THE ALARM SETPOINT 10*0 HIGHER THAN NORMAL FOR EACH INOIVIDUAL BEARING AND THE TRIP SETPOINT SHALL BE SET 23*C HIGHER THAN NORMAL FOR EACH BEARING.

7®=

7. ALL WIRE TERMINATIONS SHALL BE IDENTIFIED WITH A HEAT-SHRINK PRE-PRINTED SLEEVE AROUND THE W R E SHEATH AFTER THE WIRE ENTERS TO JUNCTION BOX.

g ALL W R E TERMINATIONS ON TERMINALS SHALL INCLUDE FERRELS.

. TEMPERATURE PRE-ALARMS ARE CONFIGURED ON TVC ANALOG MOOBUS POfWTS IN THE DCS

•

* i i »i i

Lj

i

•

t

i

i

1

BENTLY NEVADA 3n00 S Y S T E M TEMPERATURE RACK

. i

m ALL INSTRUMENT TAGS TO BE PREFIXED WITH "44", I.E., 44TE5447A.

F-SÔ* FLUOR No r ACWT «T91-tt/AWmCOHI-l M

01 04/09/04

JM GWO;

ftDBCD SIGNALS 10 MCC. DDED NOTES. ADDED I-5*?5B. /tl 10D0B?.

021 06/30/04 |GWQ|MWW

E—

PSET=20nnWC

XS-9477A (RUNNING)

\ /

XS-9480A (AUTQ START)

\

^ X S ^ S S A ^ (TRIP)

-D XS-9477B (RUNNING)

r

XS-94a3B

CTRIP)

START PERMISSIVE

/

XS-9477C (RUNNING)

PURGE COMPLETE

r • C-

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|

PURGE IN PROGRESS

/

X S ^ S S ^ (TRIF)_

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NOT PRESSURIZED

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XS^460

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MDTDR READY TD S T A R T

j

X S ^ M A PURGING ENDED XS-_9460D

XS-9499 (CCC FAULT TRIP)

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XS-946DC -

MOTOR NDT P R E S S U R I Z E D

7

XS-9472 (TRIP) _X^42D_(HULTIUN_TRIP)

A -

PURGING IN P R O G R E S S

\

[

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- I —

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A - PROCEED HotlflcMlor to procom do«a not constltuta Kcev M punc* , rait... Contmctof/Ssllor o) nny lliblllty. AcMpUnco l« nor Bccompllthod undar Uw wmt ot Hw Contr.ct/Purche»«

GASCO ERM Project 8-JUI-04 FLUOR No.: AOWT 4-0701-01/AOWT100011 -230-2

REFERENCE MOTOR DWG. H M88D1000B7 FOR COMPONENT DESCRIPTION.

UNlfSS OIHERWISE SPtOFTED

DO NOt SCALE Ofl RNtRAriO DRAWWC DO MOT UMUKll UPQMt.

cgtnDtKiw.-F«»om or:

|

1- PUCt OEC.1.060 2- PUCE OEC.t.OJO 3- PIACE OEC.t.010

BREAK ALL SHUtP COKNEIO AND fttWM BWtRS UNUSS OIWBWSI SPEC RED. STAi*> OP nc« pun iDonrKATioH IN ARIA HARKED [^>
MOTOR CONTROL DIAGRAM 04305

SIMILAR TO

MK.-

GEOil&Gas

'•LE NO.

NONE

TOROMONT FOR FLUOR/GASCO ABU DHABI

cx GWO

04/09/04

SCALE

^ MWW

04/09/04

1:1

PART WO

1/1

16-242-226-411

ISSUE

02

Vol 1 of 1 - Plant Operation Maintenance and Safety Manual

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