– Review Control Sheet – CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07
27
10
SIZING EQUIPMENT (UPDATE) – PAC F2
Processo de Revisoes Document Revision Record Rev. Rev.
Data Date
Preparado á Prepared by
Revisto á Reviewed by: (Discipline)
Revisto á Reviewed by:
Aprovada á Approved by:
Aprovada á Approved by SNLPP
A
07/27/2010
FRANCELI NIEVES
PEDRO MARQUEZ
ANDRES FIGUEREDO
EULISES RIVAS
CARLOS JIMENEZ
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 2 of 52
Rev.: A
INDEX 1
OBJETIVE 5
2
SCOPE
3
REFERENCE
5 5
3.1 Documents 5 3.2 Diagrams
5
3.3 Abbreviations
6
4
GENERAL PROCESS DESCRIPTION 6
5
SIZING DESIGN CRITERIA AND METHODOLOGY 7 5.1 Gas/Liquid Cylindrical Cyclone – GLCC (DS 205) 7 5.1.1
Design Criteria............................................................................................8
5.1.1.1 GLCC Diameter.....................................................................................8 5.1.1.2 Inlet Nozzle Area...................................................................................9 5.1.1.3 GLCC Length (Upper and Lower Parts)...............................................9 5.1.2
Methodology...............................................................................................9
5.2 Liquid/Liquid Pipe Separator – LLPS (DS 204) 5.2.1
9
Methodology..............................................................................................11
5.3 Liquid/Liquid Cylindrical Cyclone – LLCC (DS 206A/B) 5.3.1
11
Design Criteria..........................................................................................12
5.3.1.1 LLCC Inlet...........................................................................................12 5.3.1.2 LLCC Diameter...................................................................................12 5.3.1.3 LLCC Length.......................................................................................13
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301
PROJECT Nº: 015/BLK3/05
5.3.2
Page 3 of 52
Rev.: A
Methodology.............................................................................................13
5.4 Liquid/Liquid Hydrocyclone Package – LLHC (DS 207A/B) 5.4.1
DATE: 07/27/10
13
Design Criteria..........................................................................................14
5.4.1.1 Available Pressure/Pressure Drop......................................................15 5.4.1.2 Oil Droplet Size/Distribution................................................................15 5.4.1.3 Liquid Viscosity/Temperature..............................................................15 5.4.1.4 Hydrocyclone diameter/Performance..................................................15 5.4.2
Methodology.............................................................................................16
5.5 Induced Gas Flotation Unit – IGF (DS 208) 16 5.5.1
Methodology.............................................................................................16
5.6 Vessels
16
5.6.1
Design Criteria..........................................................................................16
5.6.2
Methodology.............................................................................................17
5.7 Pumps System
6
17
5.7.1
Design Criteria..........................................................................................17
5.7.2
Methodology.............................................................................................18
PROCESS DATA 6.1.1
18
Process conditions....................................................................................18
6.2 Forecast and Most Likelihood Estimation (MLE) 7
RESULTS
22
7.1 GLCC DS 205 Sizing
22
7.2 LLPS DS 204 Sizing
23
20
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 4 of 52
Rev.: A
7.3 LLCC DS 206A/B Sizing 24 7.4 LLHC DS 207A/B Sizing 25 7.5 IGF DS 208A/B Sizing 7.6 Sizing Summary 8
ATTACHMENTS
26
27 30
ATTACHMENT A: Process Flow Diagram 31 ATTACHMENT B: Process Equipment Sizing Results: LLHC and IGF 33 ATTACHMENT C: Induced Gas Flotation Unit Selection ATTACHMENT D: Vessels Calculation Notes
38
ATTACHMENT E: Pumps Calculation Notes
42
GLCC, LLPS, LLCC, 36
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
1
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 5 of 52
Rev.: A
OBJETIVE
To show calculation notes of major equipments to be installed on PACASSA F2 Platform (PAC F2), as part of the project: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)”. 2
SCOPE
This document provides calculations and sizing of the equipments: Gas/Liquid Cylindrical Cyclone, Liquid/Liquid Pipe Separators (LLPS), Water Treatment Packages (Liquid/Liquid Cylindrical Cyclone (LLCC), Liquid/Liquid Hydrocyclone (LLHC) and Induced Gas Flotation (IGF) Unit), pumps and vessels to be installed in the PAC F2 Platform as part of the project: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)”. 3
REFERENCE
3.1
Documents
1 2
Description Basis and Design Criteria Preliminary Heat &Mass Balance – PAC F2
3.2
Diagrams
1
Description Process Flow Diagram – PAC F2
Document N° 015/BLK3/05 0 PFEED001301 015/BLK3/05 2 PFEED111201
Document N° 015/BLK3/05 2 PFEED11501
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
3.3
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 6 of 52
Rev.: A
Abbreviations
BUF:
Bufalo
PAC:
Pacassa
GLCC:
LLHC:
IGF:
LLPS:
Liquid/Liquid Pipe Separator
LLCC:
Liquid/Liquid Cylindrical Cyclone
Gas/Liquid Cylindrical Cyclone Liquid/Liquid Hydrocyclone Package Induced Gas Flotation
APPLICABLE STANDARS AND CODES API (American Petroleum Institute) API RP 14E: Recommended Practice for Design and Installation of Offshore Production Platform Piping Systems, Fifth Edition, October 1, 1991. AP Spec 12J: 1, 1989.
Specification for Oil and Gas Separators, Seventh Edition, October
Total General Specification GS ECP 103: 4
Process Sizing Criteria
GENERAL PROCESS DESCRIPTION
Current production for PAC F2 platform is about 3,900 SCMD of liquid and 140,000 SCMD of gas. New environmental regulation will be complied and current production losses must be minimized. Therefore, new top facilities are required. Design of the new facilities is based on MSI IWS Technology (Patent Pending). New Gas/Liquid Cylindrical Cyclone (GLCC DS 205) receives multiphase flow from wells to separate gas and liquid phase. The gas from top is sent to COBO P1 via
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 7 of 52
Rev.: A
subsea pipeline, while the liquid from bottom is transferred to Liquid/Liquid Pipe Separator (LLPS DS 204) for a primary separation, which will reduce the water cut for crude oil to about 6%.Then crude oil goes to PAC F1 platform via Export Pumps GX 201A/B/C and existing oil pipeline. The water stream from LLPS is rich in oil (6%) and flows to the Water Treatment Package, which consist of a Liquid/Liquid Cylindrical Cyclone (LLCC DS 206 A/B) to reduce the oil content at about 2,000 ppm, a Liquid/Liquid Hydrocyclone Package (LLHC DS 207A/B) which outlet water stream has a 100 ppm of oil content and an Induced Gas Flotation Unit (IGF DS 208A/B) to obtain water overboard (with 25 ppm of oil as maximum) to be disposed to the sea or injected into wells. Process Flow Diagrams for both options are shown in the Attachment A. 5 5.1
SIZING DESIGN CRITERIA AND METHODOLOGY Gas/Liquid Cylindrical Cyclone – GLCC (DS 205)
A schematic representation of the GLCC DS 205 is shown in Figure 1. The separator is basically a vertical piece of pipe with a downward inclined inlet and two outlets, one at the bottom and the other at the top. The gas and liquid mixture flows tangentially from the inlet into the cylindrical cyclone forming a vortex. Due to the centrifugal, gravitational and buoyancy forces, the liquid moves to the wall, descends and exits from the lower part, while the gas moves to the centre, ascends and exits from the top.
Figure 1. Gas/Liquid Cylindrical Cyclone (GLCC)
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 8 of 52
Rev.: A
The liquid level control and/or pressure control ensure proper operation for different flow conditions, eliminating or reducing liquid carry over into the gas stream and/or gas carry under into the liquid stream. Determination of liquid level is important for the prediction of both liquid carry over and gas carry under. For proper operation of the GLCC, the liquid level must be maintained below the inlet to avoid gas flowing through the liquid stream and carrying liquid into the gas. Also, the liquid level should be sufficiently high above the exit at the bottom to avoid gas carry under into the liquid stream and prevent gas liberation in the liquid meter. 5.1.1 Design Criteria For GLCC design criteria following document was taken as reference: Gomez, L. E., R. Mohan, O. Shoham, J. Marreli, and G. Kouba. “Aspect Ratio Modeling and Design Procedure for GLCC Separators.” Journal of Energy Resources Technology (ASME Transactions) 121, no. 1 (March 1999): 15 23. GLCC Diameter The diameter should be such that superficial gas velocity is less than the critical velocity in order to allow liquids to drop out. In contrast, the diameter should be small enough to maintain the efficiency of the centrifugal separation and prevent gas carry under into the liquid stream. Inlet Nozzle Area
The inlet nozzle area should be small enough to ensure the entrance liquid tangential velocities in the recommended range of 3 to 6 m/s.
Velocity should be less than the fluid erosional velocity according to API RP 14E.
GLCC Length (Upper and Lower Parts) The length of the upper part (above the GLCC inlet) should be large enough to prevent liquid carry over in the form of swirling upward liquid film or as droplets. Also, The length of the lower part (below the GLCC inlet) should be large enough to maintain a
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 9 of 52
Rev.: A
finite liquid column below the vortex (for different flow conditions) in order to allow sufficient time for the separation of bubbles from the liquid phase and prevent the entrapment of bubbles in the existing liquid stream. Recommended minimum value of both lengths (upper and lower part) is 1.2 to 1.5 m as minimum. 5.1.2 Methodology
Calculations were developed using calc sheet property of MSI and final results are presented in the Attachment B.
5.2
Liquid/Liquid Pipe Separator – LLPS (DS 204)
Working principles and modeling of this type of separator was presented in: Gassies, Mathieu, L. Gomez, R. Mohan, and O. Shoham. “A Simplified Model for the Design of the Liquid Liquid Horizontal Pipe Separator.” TUSTP Manual, 2008. Design for LLPS requires determining two key parameters: diameter and length. A flow condition analysis allows determine the suitable diameter which stratified flow is promoted using Oil/Water Flow Pattern Maps due to each flow pattern has an unique hydrodynamic flow characteristics. Then, an appropriate length can be determined to enable oil water separation considering two different approaches. The first method considers the trajectories in a stratified two phase flow for an oil droplet in water and for a water droplet in oil, and selects the longest one as a design criterion for the length (see Figure 2). The second method uses the batch separation model describing the evolution of an oil water mixture in a classic gravity settler in order to determine the length required for full separation (see Figure 3).
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 10 of 52
Rev.: A
Figure 2. Particle Trajectory in Stratified Two Phase Flow.
Figure 3. Classic Gravity Settler Schematic.
5.2.1 Methodology
Calculations were developed using calculation spreadsheet property of MSI and final results are presented in the Attachment B.
5.3
Liquid/Liquid Cylindrical Cyclone – LLCC (DS 206A/B)
Design criteria and physical working principles for this type of equipment were presented in: Oropeza Vazquez, C., et al. "Oil Water Separation in a Novel Liquid
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 11 of 52
Rev.: A
Liquid Cylindrical Cyclone (LLCC) Compact Separator – Experiments and Modeling." Journal of Fluids Engineering (ASME Transactions) 126, no. 4 (July 2004): 553 564. A schematic of the LLCC DS 206A/B is shown in Figure 4. The LLCC has a configuration similar to GLCC, i.e. a vertical pipe section, but with a horizontal tangential inlet. The horizontal inlet promotes oil water segregation and both liquids phases enter the vertical section through a reducing area nozzle, increasing their velocities. The swirling motion and the gravity force in LLCC produces a centrifugal separation, where the oil phase moves to the centre and an oil rich stream exits at top. While the clear water moves to the pipe wall, flows downward and exits through the bottom. LLCC has neither moving parts nor internal devices. The LLCC design criteria are developed based on physical flow mechanisms occurring in the LLCC and limitations of the application in the field. These design criteria should be considered as the limiting design parameters appropriate for each element of the LLCC in order to ensure proper LLCC performance.
Figure 4. Liquid/Liquid Cylindrical Cyclone (LLCC) Compact Separator.
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 12 of 52
Rev.: A
5.3.1 Design Criteria LLCC Inlet Inlet diameter should be sufficiently large to permit stratification. Also, the inlet length should be sufficiently long to avoid dispersion of the two layers. The inlet nozzle should be able to generate an area reduction, providing a water superficial velocity approximately 2 m/s, in order to keep the slot area reduction between 20 to 30% of the inlet pipe area. LLCC Diameter
Water cut should be less than 65%.
Optimal split ratio is 46%.
The diameter should be such that the superficial liquid velocity in the LLCC permits a tangential velocity /axial velocity ratio (Vt/Vz) of 9, for a tangential velocity of 1.8 m/s.
LLCC Length The length of the lower part (below the LLCC inlet) should be large enough to maintain a finite liquid column below the vortex (for different flow conditions) to allow sufficient time for the separation of droplets from the oil phase and prevent the entrapment of oil droplets in the existing water stream. 5.3.2 Methodology
Calculations were developed using calc sheet property of MSI and final results are presented in the Attachment B.
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
5.4
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 13 of 52
Rev.: A
Liquid/Liquid Hydrocyclone Package – LLHC (DS 207A/B)
Liquid/Liquid Hydrocyclones (LLHC), also called enhanced gravity separators, use centrifugal force to remove oil droplets from oily water. As is shown in Figure 5, static hydrocyclones consist of four sections: a cylindrical swirl chamber, a concentric reducing section, a fine tapered section, and a cylindrical tail section. The oily water enters the cylindrical swirl chamber through a tangential inlet, creating a high velocity vortex with a reverse flowing central core. The fluid accelerates as it flows through the concentric reducing section and the fine tapered section. The fluid then continues at a constant rate through the cylindrical tail section. Larger oil droplets are separated out from the fluid in the fine tapered section, while smaller droplets are removed in the tail section. Centripetal forces cause the lighter density droplets to move toward the low pressure central core, where axial reverse flow occurs. The oil is removed through a small diameter reject port located in the head of the hydrocyclone. Clean water is removed through the downstream outlet. They are driven by inlet water pressure and use a pressure drop across the cyclone to provide the energy to cause oil water separation. Normally, a system pressure is used to provide the driving pressure, but if too low (<4 bar), a pump can be used to boost the feed pressure. The oil stream flow is largely controlled by the orifice size, but can also be regulated by an outlet control valve and is typically set to allow at 2 to 4% of the inlet flow.
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PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 14 of 52
Rev.: A
Figure 5. Hydrocyclone.
5.4.1 Design Criteria A comprehensive explanation of operation and design criteria for LLHC is presented in: Gomez, C., J. Caldentey, S. Wang, L. Gomez, R. Mohan, and O. Shoham. "Oil Water Separation in Liquid Liquid Hydrocyclones (LLHC): Part 1 – Experimental Investigation." SPE Journal 7, no. 4 (December 2002): 353 361. Available Pressure/Pressure Drop It is always preferred to use the full system pressure to drive hydrocyclones. The preferred site to locate it in a process is on the water outlet line from the separator, upstream of the level control valves. This provides the highest capacity with minimal droplet shearing. The pressure differential ratio (PDR), defined as is shown below, should be maintained in the range of 1.7 to 2.0. PDR
Pinlet Preject Pinlet Poutlet
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PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 15 of 52
Rev.: A
Where, Pinlet is the pressure at unit inlet, Preject is the pressure of reject oil stream and Poutlet is the pressure of clean water stream. Oil Droplet Size/Distribution The oil droplet size range has a major impact on the hydrocyclone performance and it is important to maintain as little shearing of oil droplets as possible prior to the equipment, by installing it upstream of control valves. Liquid Viscosity/Temperature Temperature has a direct effect on the water viscosity which has a significant effect on its performance. At higher temperatures the water viscosity reduced, creating less resistance to the separation of oil droplets and resulting in higher levels of oil/water separation. Hydrocyclone diameter/Performance The effect of the diameter of the liner on oil & water separation is very important: smaller diameter hydrocyclone provides higher level of oil removal, but they have a lower capacity. Many liners are packaged inside each vessel to treat large flow, while still providing high oil removal levels. 5.4.2 Methodology
Calculations were developed using calc sheet property of MSI and final results are presented in the Attachment B.
5.5
Induced Gas Flotation Unit – IGF (DS 208)
Induced Gas Flotation (IGF) has been used to help oil separation from produced water using microbubbles of gas (approximately 10 to 50 microns) as an improved gas flotation technology. It is generally accepted that a bubble of gas of a given size will attach itself to a similar sized oil droplet and promote it to float to the surface where the oil coalesces, collects and is skimmed off. Using microbubbles, it is easier to get lower concentrations of oil in the treated water.
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 16 of 52
Rev.: A
The IGF is a patented gas/liquid contactor designed to supersaturate liquids with a gas and does not contain any moving parts. It can be used to entrain a variety of gases into liquids at or above the saturation point. The Gas Liquid Reactor (GLR TM) is a platform technology for the creation of microbubble in a moving liquid. The Attachment B shows factors to select IGF package. 5.5.1 Methodology 5.6
Select IGF Model according to Attachment C and average feed flow rate. Vessels
5.6.1 Design Criteria Based on Basis and Design Criteria, Doc. No 015/BLK3/05 0 PFEED001301:
For vertical vessels, L/D ratio should be between 2.5 and 6. It is recommended L/D equal to 3.
For horizontal vessels, L/D ratio should be between 3 and 4.
For low operational pressure (0 17 barg), it is recommended L/D ratio equal to 3 in order to provide an economical design.
Retention time 1 to 3 min according to API Spec 12 J due to allow sizing smaller containers.
5.6.2 Methodology
Get process conditions from Heat & Mass Balance.
Determine liquid volume using API Spec 12J retention time for the liquids phases.
Assume that separator is half full of liquid and L/D ratio is 3.
Calculate minimum diameter and then select next large standard diameter (vessel diameter is generally expanded in 152.4 mm (6 inch) increments).
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PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 17 of 52
Rev.: A
Determinate seam to seam length.
Refer to Attachment D to see calculation notes. 5.7
Pumps System
5.7.1 Design Criteria Based on Basis and Design Criteria (Doc. No 015/BLK3/05 0 PFEED001301) and Total General Specification GS ECP 103:
The minimum margin between the normal and rated flow for a pump will be 10%.
Maximum suction velocity is 1.8 m/s.
In general, a minimum margin of 1 m between the Net Positive Suction Head Available (NPSHA) and the Net Positive Suction Head Required (NPSHR).
Design temperature is increased 15°C above nominal pumping temperature.
Pumps should be specified with a maximum head rise to shut in of 1.25 times design pump differential. The design pressure is the maximum head to shut in plus the maximum suction pressure. The design pressure shall be no less than 3.5 barg.
The minimum flow for pump protection is 30% of design flow.
5.7.2 Methodology
Get process conditions from Heat & Mass Balance.
Calculate the pump suction conditions, suction pressure, maximum suction pressure and NPSHA.
Determine the nominal discharge pressure requirements for the pump.
Calculate the pressure differential and pump head.
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PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 18 of 52
Determine the power requirements: Brake Horse Power (BHP).
Calculate design conditions.
Rev.: A
Refer to Attachment E to see calculation notes. 6
PROCESS DATA
6.1.1 Process conditions The following tables show the process conditions for the equipments on platform according to the production forecast supplied by Sonangol P&P: Table 1. Process conditions for PAC F2 Platform Feed. Parameter Total Gas (SCMD)1 Produced Liquid (SCMD) Pressure (barg) Temperature (°C)
Minimum 204,434 2,220 5.0 88
Maximum 315,849 3,901 7.0 120
Table 2. Well Composition for PAC F2 Platform2.
Component N2 CO2 C1 C2 C3 i C4 n C4 i C5 n C5 C6 C7 C8 1
Including gas lift injection rate.
2
Well Fluid Composition supplied by Sonangol P&P.
% Mol 0.2 0.7 37.8 8.3 7.2 1.3 3.5 1.7 1.8 3.6 3.7 3.3
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 19 of 52
C9 C10 C11+
2.6 1.8 22.5
Table 3. Oil Characterization for C11+.
Property Critical Temperature (ºC) Critical Pressure (barg) Acentric Factor Density @60°C (Kg/m3) Molecular Weight
Value 455 15.5 0.90 910.0 260.00
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 20 of 52
Rev.: A
Table 4. Gas Chromatography for COBO Gas Lift.
6.2
Forecast and Most Likelihood Estimation (MLE)
Production Forecast and Maximum Likelihood Estimation (MLE) envelopes are plotted to show the operating limits for oil, water and gas. Results of MLE are used to determine the design conditions (flow rate operating range) for PAC F2 surface facility equipment. The method takes in account the historical data for the individual well of each platform which is correlated with the average flow rate of each phase. Figure 6 presents gas and total liquid operating points, production forecast envelope and MLE.
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / BASIC ENGINEERING DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 21 of 52
Rev.: A
Figure 7 shows water and oil operating points, production forecast envelope and the corresponding MLE.
Figure 6. Liquid and Gas Forecast and MLE.
Technical Documents CONTENT DESCRIPTION
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 22 of 52
Rev.: A
Figure 7. Oil and Water Forecast and MLE.
7 7.1
RESULTS GLCC DS 205 Sizing
The design of the separator should cover all the expected operating points and the MLE. In this regard several run were done using maximum gas and total liquid flow rates, temperature, pressure and fluid properties presented above. Following figure shows GLCC operating envelope.
Technical Documents CONTENT DESCRIPTION
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 23 of 52
Rev.: A
Figure 8. GLCC Operating Envelope.
7.2
LLPS DS 204 Sizing
This separator was designed to handle the total liquid fluid (oil plus water) under the most critical conditions. No gas presence is considered for superficial velocities calculations. Results are presented in Figure 9. This operating envelope is defined by the superficial velocity given for the MLE; the minimum mixture velocity of 0.015 m/s which is 10 times less than the stratified flow pattern boundary; the velocity region for 30% of Water Cut and the oil flow rate corresponding to 0.010 m/s to warranty that the oil flow is under stratified flow pattern.
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 24 of 52
Rev.: A
Figure 9. LLPS Operating Envelope.
7.3
LLCC DS 206A/B Sizing
Design considerations for this type of separator include the following:
Maximum allowable pressure drop is 1.38 bar (20 psi)
The equipment is a set of 24 LLCCs of 50.8 mm (2 inches) in diameter inside an 813 mm (32 inches) drum.
Each LLCC will handle 106.52 SCMD (670 BPD) of liquid.
Figure 10 shows the liquid production forecast, the MLE and the performance of the LLCC. It is notice that two drums could cover the operations from years 2010 to about
Technical Documents CONTENT DESCRIPTION
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 25 of 52
Rev.: A
2015 and one drum is needed during the rest of the operation. However it is recommended using two drums to assure the expected system reliability.
Figure 10. LLCC Operating Envelope.
7.4
LLHC DS 207A/B Sizing
Design considerations for the Hydrocyclone package are as follows:
Maximum allowable pressure drop is 1.38 bar (20 psi)
The equipment is a set of 75 Hydrocyclones (Liner) of 25.4 mm (1 inch) in diameter inside a 762 mm (30 inches) drum. Each Liner has an orifice of 2 mm of diameter.
Each Hydrocyclone will handle 31.80 SCMD (200 BPD) of liquid.
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 26 of 52
Rev.: A
Figure 11 shows the liquid production forecast, the MLE and the performance of the LLHC. Under this operating condition two drums can cover the operations during the first five years and one drum is needed for the last ten years of operation. However it is recommended using two drums to assure the expected system reliability.
Figure 11. LLHC Operating Envelope.
7.5
IGF DS 208A/B Sizing
Design considerations for the Induced Gas Floatation Unit are as follows:
The equipment is a set of 2 Micro Bubble Floatation Units of 40 inches diameter. The system also includes two Gas Clean Drums and two Micro Bubble Generation Units.
Each Micro Bubble Floatation Unit will handle 1,512 SCMD (9,510 BPD) of liquid.
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 27 of 52
Rev.: A
Figure 12 shows the liquid production forecast, the MLE and the performance of the IGF. Under this operating condition, two units can cover the operations along the expected production period.
Figure 12. IGF Operating Envelope.
7.6
Sizing Summary
The sizing results for new equipments are shown in the followings tables:
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 28 of 52
Rev.: A
Table 5. Separators Sizing Results. Item Tag Type Design Pressure (barg) Working Temperature Design Max/Min (°C) Working Liquid Flow Rate (Sm3/d) Gas Flow Rate (Sm3/d) Internal Diameter (mm) Height or Length TL-TL (mm)
DS 204 Horizontal 8 4.86 135/110 5,700 1,067 5,330
DS 205 Vertical 8 5.0 135/110 7,200 390,000 1,067 5,338
DS 206A/B Vertical 8 3.47 135/109.9 5,113 813 2,440
DS 207A/B Vertical 8 6.3 135/109.7 4,770 762 1,220
DS 208A/B Vertical 8 0.6 135/109.7 3,984 1067 4,073
DS 209 Vertical 8 1.94 135/109.6 XXX XXX 610 2,286
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 29 of 52
Rev.: A
Table 6. Standardization Pumps Results 3. Item Tag Design Pressure (barg) Working Suction/Discharge Design Max/Min Temperature (°C) Working Normal Capacity (Sm3/d) Rated Capacity (Sm3/d) Differential Pressure (bar) Pump Head (m) NPSHA (m) Brake Horse Power (kW)
3
GX 411A/B 8.3 2.5/7.1 135/110 160 176 4.6 50 >7.6 30.0
GX 412A/B 9.0 0.7/7.3 135/110 160 176 6.6 71.8 2.9 45.0
Refer to Attachment E to see Calculation Notes and Standardization Pumps.
GX 413A/B 153.0 7.3/127.2 135/110 80 88 119.9 1300 >7.6 390
GX 414A/B 6.6 1.6/5.6 135/110 12.7 14.0 4.0 52.6 3.2 2.1
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8
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 30 of 52
Rev.: A
ATTACHMENTS
ATTACHMENT A: Process Flow Diagram. ATTACHMENT B: Process Equipment Sizing Results: GLCC, LLPS, LLCC and LLHC. ATTACHMENT C: Induced Gas Flotation Unit Selection. ATTACHMENT D: Vessel Calculation Notes. ATTACHMENT E: Pumps Calculation Notes.
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 31 of 52
ATTACHMENT A: Process Flow Diagram
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 33 of 52
ATTACHMENT B: Process Equipment Sizing Results: GLCC, LLPS, LLCC, LLHC and IGF
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 34 of 52
Rev.: A
Technical Documents CONTENT DESCRIPTION
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 35 of 52
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 36 of 52
ATTACHMENT C: Induced Gas Flotation Unit Selection
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 37 of 52
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 38 of 52
ATTACHMENT D: Vessels Calculation Notes
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 39 of 52
DS-209 - Sizing: 1. Estimation of inlet flow rates, densities and viscosities of all phase: 3
Actual gas vol. flow rate:
m Qg 50.42 hr
Gas density @ P y T:
g 2.89
(from Hysys report)
kg m
(from Hysys report)
3
Gas viscosity:
g 0.011cP
Oil mass flow rate:
mo 7875
(from Hysys report)
kg
Oil density:
hr kg o 786.44 3 m
Oil vol. flow rate:
mo Qo o
Oil viscosity:
o 1.174cP
Water mass flow rate:
mw 481
Water density:
w 940.66
Water vol. flow rate:
(from mass balance) (from mass balance) 3
m Qo 10.013 hr (from Hysys report)
kg
(from mass balance)
hr kg m
3
mw
Qw w
(from mass balance) 3
m Qw 0.51 hr (from Hysys report)
Oil viscosity:
w 0.256cP
Liquid mass flow rate:
mL mo mw
mL 8356
Liquid vol. flow rate:
QL Qo Qw
m QL 10.52 hr
Liquid density:
L
kg hr 3
mL QL
2. Approximation of Separator Dimensions: Assumptions: H/D=3 Separator is half full of liquid (M=0.5) Liquid retention time (t r) is 1 min.
L 793.9
kg m
3
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 40 of 52
(API Spec 12J)
M 0.5
tr 1min
D 150mm
H 600mm
(guess values)
Given H D 4
D = inside diameter of separator H = height of separator M = fraction of vertical area filled with liquid
3 2
D M H
QL t r
20.867
Sol Find ( D H)
Re ( Sol)
Outside Diameter,
D 24in
in
62.601
D 610 mm
3. Gas Capacity - Sounder Brown K factor 0.35 ft
Sounder Brown K factor:
K
Maximum allowance velocity:
V max K
Minimum vapour area:
Amin
Minimum diameter:
Dmin
2
s
(API Spec 12J
o g g
Qg Vmax 4Amin
K 0.053
m s
V max 0.878
4Qg
V g
2
D
Dmin 5.61 in
V g 0.048
m s
Actual Vg
V L QL t r
Maximum liquid height:
HL
4VL 2
D
s
Amin 0.016 m
4. Gas Capacity - Drop Settling
Actual gas velocity:
m
V L 0.175 m HL 0.601 m
3
2
Rev.: A
Technical Documents CONTENT DESCRIPTION
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / PRE FEED DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS
DATE: 07/27/10
PROJECT Nº: 015/BLK3/05
Page 41 of 52
6. Separator Height: ft
Maximum inlet nozzle velocity:
Ve 30
Minimum inlet nozzle area:
AN
Inlet nozzle diameter:
DN
Height seam to seam:
H HL 1ft 2DN D
Next largest standard size:
H 7.5ft
Ratio L/D:
H D
(from Design Basis)
sec
Qg QL
3
A N 1.851 10
Ve 4AN
m
2
DN 0.049 m
H 5.29 ft H 2286 mm
3.75
7. Weight Calculation: Working pressure:
P 8bar 1atm 1bar
Allowance stress for steel:
S 1200bar 1atm
Joint efficiency:
E 0.85 (initial work)
Shell tickness (including corrosion allowance equal to 3 mm):
t
t
P D
4
in
Inside Diameter:
ID D 2t
Empty vessel weight (including heads):
we 3.47
3
S 1.201 10 bar
3mm
t 5.978 mm
(commercial)
t 6.35 mm
2S E 0.8 P
16
P 10.013 bar
ID 23.5 in kg 2
cm m
ID H t
we 301 kg
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 42 of 52
ATTACHMENT E: Pumps Calculation Notes
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 43 of 52
GX 210: 2000 ppm Water Pump Calculation:
Oil Mass Flowrate:
kg mo 247.8 hr
Oil Density:
o 784.41
kg 3
m
kg Water Mass Flowrate: m 123643 w hr
kg Water Density: 939.72 w 3 m
Total Mass Flowrate:
mt mo mw
kg mt 123890.8 hr
Total Vol. Flowrate:
Q
Rated Capacity:
QRATED 1.1Q
Fluid Density:
mo o
mw w
3
Q 131.9
m
hr 3
mt
m QRATED 145.1 hr 939.3
Q
kg 3
m
1. Suction Section: Operating Pressure Vessel:
Po 2.44barg
Hidrostatic Height:
h 1 9in 2ft
h 1 0.8 m
(LLLL=9in minimum according to Design Basis & distance between vessel liquid nozzle and pump centerline d=2ft). Suction Pressure:
Ps Po g h 1
Maximum head at suction:
h max 8ft
Maximum Suction Pressure:
Psmax Ps g h max
Ps 2.5 barg
Psmax 2.7 barg
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 44 of 52
GX 211: Water Booster Pump Calculation:
Oil Mass Flowrate:
kg mo 0 hr
Oil Density:
o 780
kg 3
m
kg Water Mass Flowrate: m 123338 w hr
kg Water Density: 940.36 w 3 m
Total Mass Flowrate:
mt mo mw
kg mt 123338 hr
Total Vol. Flowrate:
Q
Rated Capacity:
QRATED 1.1Q
Fluid Density:
mo o
mw w
3
Q 131.2
m
hr 3
mt
m QRATED 144.3 hr 940.4
Q
kg 3
m
1. Suction Section: Operating Pressure Vessel:
Po 0.6barg
Hidrostatic Height:
h 1 9in 2ft
h 1 0.8 m
(LLLL=9in minimum according to Design Basis & distance between vessel liquid nozzle and pump centerline d=2ft). Suction Pressure:
Ps Po g h 1
Maximum head at suction:
h max 160in
Maximum Suction Pressure:
Psmax Ps g h max
Vapor pressure @ 110°C:
Pvp 0.4088barg
Ps 0.7 barg
Psmax 1.1 barg
Rev.: A
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NPSHA:
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 45 of 52
NPSHA
Ps Pvp g
NPSHA 2.9 m
2. Discharge Section: Discharge pressure:
Pd 7.3barg
3. Pump parameters: Differential Pressure:
P Pd Ps
Pump Height:
H
Shut off Pressure:
Pshutoff Psmax 1.2P
Pshutoff 9 barg
Hydraulic Power:
W hyd QRATED g H
W hyd 26.5 kW
Efficiency:
75% ( assumed )
Motor Power:
W BHP
Pd Ps
P 6.6 barg H 71.8 m
g
W hyd
W BHP 35.4 kW
Rev.: A
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Two operating pumps + 1 spare:
N 2
0 kg mo N hr
Water Mass Flowrate: m w
Oil Density:
123338 kg N
mt mo mw
Total Vol. Flowrate:
Q
Rated Capacity:
QRATED 1.1Q
Fluid Density:
mo o
o 780
kg 3
m
kg Water Density: 940.60 w 3 m
hr
Total Mass Flowrate:
kg mt 61669 hr 3
mw
Q 65.6
w
m
hr 3
m QRATED 72.1 hr
mt
940.6
Q
kg 3
m
1. Suction Section: Suction Pressure:
Ps 7.3barg
Maximum Suction Pressure:
Psmax 9barg
Vapor pressure @ 110°C:
Pvp 0.4088barg
NPSHA:
NPSHA
Ps Pvp g
2. Discharge Section: Discharge pressure:
DATE: 07/27/10 Page 46 of 52
GX 212: Water Injection Pump Calculation:
Oil Mass Flowrate:
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301
Pd 127.2barg
NPSHA 74.7 m
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 47 of 52
3. Pump parameters: Differential Pressure:
P Pd Ps
Pump Height:
H
Shut off Pressure:
Pshutoff Psmax 1.2P
Pshutoff 152.9 barg
Hydraulic Power:
W hyd QRATED g H
W hyd 240.2 kW
Efficiency:
75% ( assumed )
Total Motor Power:
W BHP
Pd Ps
P 119.9 barg
H 1299.9 m
g
W hyd
W BHP 320.3 kW
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301
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DATE: 07/27/10
PROJECT Nº: 015/BLK3/05
Page 48 of 52
GX 213: Oil Recirculation Pump Calculation:
Oil Mass Flowrate:
kg mo 7806 hr
Oil Density:
o 784.42
kg 3
m
kg Water Mass Flowrate: m 456.3 w hr
kg Water Density: 943.68 w 3 m
Total Mass Flowrate:
mt mo mw
kg mt 8262.3 hr
Total Vol. Flowrate:
Q
Rated Capacity:
QRATED 1.1Q
Fluid Density:
mo o
mw w
3
Q 10.4
m
hr 3
mt
m QRATED 11.5 hr 791.8
Q
kg 3
m
1. Suction Section: Operating Pressure Vessel:
Po 1.3barg
Hidrostatic Height:
h 1 9in 3m
h 1 3.2 m
(LLLL=9in minimum according to Design Basis & distance between vessel liquid nozzle and pump centerline d=2m).
Rev.: A
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DOCUMENT NUMBER 015/BLK3/05 2 FEED11301
PROJECT Nº: 015/BLK3/05
DATE: 07/27/10 Page 49 of 52
Suction Pressure:
Ps Po g h 1
Maximum head at suction:
h max 7.5ft
Maximum Suction Pressure:
Psmax Ps g h max
Vapor pressure @ 105°C:
Pvp 1.3barg
NPSHA:
NPSHA
Ps 1.6 barg
Psmax 1.7 barg
Ps Pvp
NPSHA 3.2 m
g
2. Discharge Section: Operating Pressure Vessel:
P1 4.86barg
Hidrostatic Height:
h 2 42in
Valve pressure drop:
Pvalve 0.7barg
Discharge pressure:
Pd P1 Pvalve g h 2
Pd 5.6 barg
Differential Pressure:
P Pd Ps
P 4.1 barg
Pump Height:
H
Shut off Pressure:
Pshutoff Psmax 1.2P
Pshutoff 6.6 barg
Hydraulic Power:
W hyd QRATED g H
W hyd 1.3 kW
Efficiency:
75% ( assumed )
Motor Power:
W BHP
h 2 1.1 m
3. Pump parameters:
Pd Ps
H 52.7 m
g
W hyd
W BHP 1.7 kW
Rev.: A
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / PRE FEED DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 50 of 52
Rev.: A
Similar calculations (as shown above) are done for the pumps located in BUF F1 and PAC F4. The standardization criterion of pumps for same service in the different platforms is applied. For this, the bigger pump, in relation to capacity and power, is selected as the standard pump.
Technical Documents CONTENT DESCRIPTION
PROJECT: ENGINEERING, PROCUREMENT, INSTALLATION & CONSTRUCTION “BLOCK 3/05 TOPSIDE FACILITIES UPGRADE (BUF F1 – PAC F2 – PAC F4)” PHASE: D&D / PRE FEED DOCUMENT: SIZING EQUIPMENT (UPDATE) – PAC F2 DISCIPLINE: PROCESS PROJECT Nº: 015/BLK3/05
DOCUMENT NUMBER 015/BLK3/05 2 FEED11301 DATE: 07/27/10 Page 51 of 51
Rev.: A