UniSim Design PIPESYS Tutorial

UniSim Design PI PESYS Tutorial

Co p y r i g h t June 2005 R350 Release The information in this help file is subject to change over time. Honeywell may make changes to the requirements described. Future revisions will incorporate changes, including corrections of typographical errors and technical inaccuracies. For further information please contact Honeywell 300-250 York Street London, Ontario N6A 6K2 Telephone: (519) 679-6570 Facsimile: (519) 679-3977 Copyright Honeywell 2005. All rights reserved.

Prepared in Canada.

Table of Contents 1

G a s C o n d e n s a t e T u t o r i a l ....................................... 1 - 1 1.1 Introduction .................................................... 1-2

2

1.2

Setting Up the Flowsheet .................................. 1-2

1.3

Adding a PIPESYS Extension .............................. 1-8

1.4

Applying a Global Change .................................1-18

G a s C o n d e n s a t e G a t h e r i n g S y s t e m ....................... 2 - 1 2.1 Introduction .................................................... 2-2

3

2.2

Setting Up the Flowsheet .................................. 2-6

2.3

Building the Case ............................................. 2-8

2.4

Viewing the Results .........................................2-19

O p t i m i z e G a s C o n d e n s a t e G a t h e r i n g S y s t e m ........ 3 - 1 3.1 Introduction .................................................... 3-2

A

3.2

Building the Case ............................................. 3-3

3.3

Viewing the Results .......................................... 3-9

R e f e r e n c e s ........................................................... A - 1

ii

iii

Gas Condensate Tutorial

1-1

1 Ga s Co n d e n sa t e Tu t o r i a l 1 . 1 I n t r o d u c t i o n ................................................................................... 2 1 . 2 S e t t i n g U p t h e F l o w s h e e t ............................................................... 2 1.2.1 Select the Unit Set ................................................................... 2 1.2.2 Define the Fluid Package ........................................................... 3 1.2.3 Enter the Simulation Environment .............................................. 1.3 Adding a PIPESYS Extension .......................................................... 8 1.3.1 Defining the Pipe Unit ............................................................. 11 1.3.2 Enter the PFD ........................................................................ 17 1 . 4 A p p l y i n g a G l o b a l C h a n g e ............................................................ 1 8

1 -1

1-2

I ntroduction

1 . 1 In t r o d u ct io n This example guides you through the construction of a gas condensate pipeline consisting of four Pipe Units. A Fluid System with a hypothetical component is used in a pressure drop calculation for a predetermined flow rate through the pipeline. All units for this example are Field.

1 . 2 Settin g Up th e Fl o w sh ee t To begin setting up the flowsheet, you must start UniSim Design and create a New case.

1 . 2 . 1 Sele ct th e Un it Set To change the unit set to Field: 1. Open the T o o l s drop-down menu in the menu bar. 2. Select the P r e f e r e n c e s command to open the Session Preferences view. 3. Go to the V a r i a b l e s tab and select the U n i t s page. 4. Select the F i e l d s in the Available Unit Sets group. 5. Click the Cl o se icon to close the Session Preferences view. Close icon

1-2


1-3

1 . 2 . 2 D efin e th e Fl u i d Pa ck a g e 1. Create a fluid package with the following information:

For more information on creating a Hypothetical Component, refer to Chapter 3 H y p o t h e t i c a l s in the UniSim Design Simulation Basis manual.

P r o p e r t y Pa c k a g e

C o mp o n e n t s

Peng-Robinson

C1, C2, C3, i-C4, n-C4, i-C5, n-C5, C6, Nitrogen, CO2, and H2S

In this tutorial, you will be creating a hypothetical component. 2. In the Component List view, select H y p o t h e t i c a l in the Add Component list. 3. Click the Q u i c k C r e a t e a H y p o C o m p . . . button. The Hypothetical Component Property View appears. 4. Enter C7 + into the C o m p o n e n t N a m e cell and make sure that Family/ Class is set to H y d r o c a r b o n . 5. Go to the C r i t i c a l tab and enter 1 2 2 into the Molecular Weight cell. 6. Enter 7 6 0 k g / m 3 into the Ideal Liquid Density cell by first selecting that cell and then typing 7 6 0 . Select units of kg/ m 3 and the program will automatically convert the liquid density to 47.45 lb/ft 3 .

1 -3

1-4

Setting Up the Flow sheet

7. Finally, click the E s t i m a t e U n k n o w n P r o p s button to complete specification of the hypothetical component. Verify that the C r i t i c a l tab appears as in the figure below before closing the view. Figure 1.1

8. Click the Cl o se icon to close the C7+ * view. Close icon

9. On the Component List view, select C7 + component in the Available Hypo Components list. 10. Click the A d d H y p o button to add C7+ to the Selected Components list to complete the specification of the fluid. 11. Click the Cl o se icon to close the Component List view.

Close icon

1-4


1-5

1 . 2 . 3 En te r th e Si m u la t io n En v i ro n m e n t 1. In the Simulation Basis Manager view, click the E n t e r S i m u l a t i o n E n v i r o n m e n t . . . button located at the bottom of the view. 2. Open the W o r k b o o k . Workbook icon

3. To change the Workbook display, select W o r k b o o k menu from the menu bar and then S e t u p command to display the Setup view as shown below. Figure 1.2

4. Click the A d d . . . button in the Variables group to display the Select Variable(s) For Main view. 5. Select Std Gas Flow in the Variable(s) list. 6. Click the OK button in the Select Variable(s) For Main view. 7. Click the Cl o se icon to close the S e t u p view. Close icon

1 -5

1-6


8. Create a new material stream. Name it C o n d e n s a t e and type 1 1 0 °F into the Temperature cell and 1 1 5 0 p s i a into the Pressure cell. Figure 1.3

9. Enter 7 5 million standard cubic feet per day (MMSCFD) into the Molar Flow cell. UniSim Design will convert this value to 8235. lbmole/hr. Figure 1.4

1-6


1-7

10. Double-click the M o l a r F l o w cell and the I n p u t C o m p o s i t i o n f o r S t r e a m : C o n d e n s a t e view will appear. Complete the composition as shown below. Figure 1.5

11. Click OK button. The following table summarizes the Condensate stream information: Nam e

Condensate

Vapour Fraction

0.9576

Temperature [ F]

110* *

Pressure [ psia]

1150* *

Molar Flow [lbmole/hr]

8235* *

Mass Flow [ lb/ hr]

1.905e+ 05

Liq Volume Flow [barrel/ day]

3.399e+ 04

Heat Flow [Btu/hr]

-3.307e+ 08

Std Gas Flow [ MMSCFD]

75.00* *

Comp Mass Frac [ Methane]

0.76110* *

Comp Mass Frac [ Ethane]

0.07860* *

Comp Mass Frac [ Propane]

0.02820* *

Comp Mass Frac [ i-Butane]

0.0075* *

Comp Mass Frac [ n-Butane]

0.0142* *

Comp Mass Frac [ i-Pentane]

0.0072* *

Comp Mass Frac [ n-Pentane]

0.0070* *

Comp Mass Fac [ n-Hexane]

0.0114* *

Comp Mass Frac [ Nitrogen]

0.0096* *

Comp Mass Frac [ CO2]

0.0390* *

o

1 -7

1-8

Adding a PI PESYS Extension

Nam e

Condensate

Comp Mass Frac [ H2S]

0.0268* *

Comp Mass Frac [ C7+ * ]

0.0094* *

** signiﬁes required input

12. Create a second material stream, which will be the outlet stream of the pipeline. Name this stream O u t l e t . 13. Go to the Energy Streams tab of the Workbook view. 14. Define an energy stream by entering the name P i p e l i n e E n e r g y T r a n s f e r into the Name cell.

1 . 3 Ad d i n g a PI PESYS Ex te n si o n 1. Add the PIPESYS Extension to the UniSim Design case by selecting F l o w s h e e t menu and A d d O p e r a t i o n . . . command from the menu bar. The UnitOps view appears. 2. Select PI PESYS Extension from the Available Unit Operations list as shown below. Figure 1.6

3. Click the A d d button. The PIPESYS Extension view should now be on your screen, displaying the C o n n e c t i o n s tab. 4. Name the PIPESYS extension G a s C o n d e n s a t e P i p e l i n e. 5. From the Inlet drop-down list, select the C o n d e n s a t e stream. 1-8


1-9

6. Select the O u t l e t stream from the Outlet drop-down list. 7. Select P i p e l i n e E n e r g y T r a n s f e r from the Energy dropdown list. Ignore the UnitOp During Calculations checkbox allows you to disable the concurrent calculation of intermediate results while you are specifying data to the PIPESYS extension.

8. Click on the I g n o r e t h i s U n i t O p D u r i n g C a l c u l a t i o n s checkbox. Figure 1.7

9. Go to the M e t h o d s tab.

1 -9

1-10


10. Ensure that the G a s - b a s e d w i t h L i q u i d and the C a l c u l a t e P r o f i l e radio buttons are selected as shown. Figure 1.8

11. Select the E l e v a t i o n P r o f i l e tab. Here you will define the geometry and physical characteristics of the pipeline. 12. Enter 0 f t into the Distance field and 2 8 0 0 f t into the Elevation field in the Pipeline Origin group. 13. Select the cell in the Pipeline Unit column that reads < e m p t y > . Select P i p e from the drop-down list. A Pipe Unit will be added to the elevation profile matrix and the Pipe Unit view appears.

Pipeline Unit drop-down list

1 -1 0


1-11

1 . 3 . 1 D efin i n g th e Pi p e Un it 1. On the Pipe Unit view, go to the D i m e n s i o n s tab. 2. Select 1 2 I n c h e s from the Nominal Diameter drop-down list. 3. Select 4 0 from the Pipe Schedule drop-down list. When you are finished these steps, the Dimensions tab will appear as shown below. Figure 1.9

4. Go to the H e a t T r a n s f e r tab. Enter 4 f t for the Centre Line Depth parameter.

1 -1 1

1-12


5. Choose S a n d y S o i l ( M o i s t ) from the drop-down list for Soil Ty pe. Figure 1.10

6. Go to the P i p e C o a t i n g s tab. 7. Add a single layer of insulation consisting of PVC Foam with a thickness of 2 i n c h e s as shown below. Figure 1.11

8. Click the Cl o se button to return to the PIPESYS Extension view.

1 -1 2


1-13

Finish D e fining the Pipe Un it 1. Go to the E l e v a t i o n P r o f i l e tab. 2. Complete the specification for the first P i p e U n i t by entering 3 4 0 0 f t into the Distance column and 2 8 8 0 f t into the Elevation column. Figure 1.12

Using the Cop y and P a s t e buttons on the elevation profile, you can copy existing pipeline units from the Elevation Profile tab and create a new pipeline unit with identical properties. This saves time when creating a pipeline consisting of several identical pipe units. 3. Select the Pipe Unit that you want to copy; in this case it is Pipe # 1. 4. Click the Co p y button. You will notice that the P a s t e button (previously greyed out) becomes active. 5. Select the cell in the Pipeline Unit column with the < e m p t y > label and click the P a s t e button. A new Pipe Unit will be added to the profile. 6. Repeat the step above twice so that the elevation profile matrix has a total of four Pipe Units. The Copy and Paste procedure copies only the Pipe Units view data for the Pipe Units. So you are required to enter the elevation profile data for the remaining three pipe units. 1 -1 3

1-14


7. Use the data values shown in the figure below to fill in the Distance and Elevation parameters. Figure 1.13

For most cases, the PIPESYS default Stepsize and tolerance values are acceptable for the extension calculations.

8. Go to the S t e p s i z e tab of the PIPESYS Extension view. Make sure the P r o g r a m D e f a u l t s radio button is selected as shown below. Figure 1.14

9. Go to the T e m p e r a t u r e P r o f i l e tab.

1 -1 4


1-15

10. Enter 4 0 F into the Ambient Temperature field in the Pipeline Origin group as shown below. Figure 1.15

11. Return to the C o n n e c t i o n s tab. Since data entry is complete, you can instruct the program to begin calculations by removing the check in the I g n o r e t h i s U n i t O p D u r i n g C a l c u l a t i o n s checkbox. After a few seconds, the program will find a solution and announce success by displaying C o n v e r g e d on the status bar at the bottom of the PIPESYS Extension view.

1 -1 5

1-16


12. You can view the results for each Pipe Unit on the R e s u l t s tab on the Main PIPESYS View. Figure 1.16

You can view more detailed results by clicking the D e t a i l button on the Results tab. The Pipe Segm ent Results view appears with a comprehensive array of hydraulic data for each calculation segment.

The Results tab shows pressure losses, fluid temperatures and liquid holdup for each Pipe Unit. 13. You can check to see if the program encountered any difficulties during the calculation phase by going to the M e s s a g e s t ab. Figure 1.17

For this case, there should have been no difficulties. 1 -1 6


1-17

1 . 3 . 2 En te r th e PFD 1. To open the PFD view, click the PFD icon on the toolbar. PFD icon

2. Right-click anywhere on the PFD view and the Object Inspect menu appears. 3. Select C h o o s e L a b e l V a r i a b l e command from the menu. The Select Variable for PFD Labels view appears. You can use this view to display a number of process variables on the PFD. 4. Click the C h a n g e V a r i a b l e button and select P r e s s u r e from the Choose Label Variable view. 5. Click the OK button on the Choose Label Variable view and the inlet and outlet pressures will be displayed on the PFD. Figure 1.18

6. To print the PFD schematic, right-click anywhere on the PFD. The Object Inspect menu appears. 7. Select the P r i n t P F D command from the menu.

1 -1 7

1-18

Applying a Global Change

1 . 4 A p p l y i n g a Gl o b a l Ch a n g e By using the G l o b a l C h a n g e feature, you can quickly change the pipe size for all pipe units and then let PIPESYS recalculate the flow parameters for the extension. 1. On the PIPESYS Extension view, go to the E l e v a t i o n P r o f i l e tab. 2. Select the first pipe in the list and click the G l o b a l C h a n g e button. 3. On the Pipe Unit view, go to the D i m e n s i o n s tab. 4. Select 1 0 I n c h e s from the N o m i n a l D i a m e t e r drop-down list and select 4 0 from the P i p e S c h e d u l e drop-down list. You should notice that the Change checkbox beside the Nominal Diameter drop-down list became checked as soon as you made these changes. Figure 1.19

The C h a n g e checkbox is used to notify you that the program is aware that this parameter has changed and that this change can be duplicated for other pipe units in the pipeline. 5. Click the A p p l y button on the Pipe Unit view. The Global Change Dialog Box (GCDB) view will appear. 1 -1 8


1-19

6. The GCDB view allows you to specify which pipe units will be subject to the changes. In this case, you are changing all of them, so click the S e l e c t A l l button as shown below. Figure 1.20

7. Click the OK button. 8. Click the Cl o se button on the Pipe Unit view. The changes will be registered with the program but will not be implemented until this view is closed. 9. PIPESYS will immediately start to recalculate for the 10” diameter. When the status bar displays C o n v e r g e d , you can look at the calculated results and compare them with the values obtained for the 12” pipe. You have now completed the Gas Condensate pipeline example. For a more in-depth exercise in using the PIPESYS Extension, see C h a p t e r 2 - G a s C o n d e n s a t e G a t h e r i n g S y s t e m , and Chapter 3 - Optim ize Gas Condensate Gathering System .

1 -1 9

1-20

Applying a Global Change

1 -2 0

Gas Condensate Gathering System 2-1

2 Ga s Co n d e n sa t e Ga t h e r in g Sy st e m 2.1 I ntroduction ...................................................................................2 2.2 Setting Up the Flow sheet ............................................................... 2.3 Building the Case ........................................................................... 2.3.1 2.3.2 2.3.3 2.3.4 2.3.5 2.3.6 2.3.7 2.3.8

Add the First PIPESYS Extension................................................. Add the Second PIPESYS Extension ........................................... 12 Add the First Mixer ................................................................. 13 Add the Third PIPESYS Extension .............................................. 14 Add the Fourth PIPESYS Extension ............................................ 15 Add the Fifth PIPESYS Extension .............................................. 16 Add the Second Mixer ............................................................. 17 Define the Well Streams .......................................................... 18

2 . 4 Vi e w i n g t h e R e s u l t s ..................................................................... 1 9

2 -1

2-2

I ntroduction

2 . 1 In t r o d u ct io n In this PIPESYS Application, the performance of a small gas condensate gathering system is modeled. The following figure shows the physical configuration of this system superimposed on a topographic map. The system consists of three wells distributed over an area of approximately 1.0 square mile connected to a gas plant via a network of pipelines. Figure 2.1

Field data shows that the wells are delivering the following rates: We l l

R a te (M M S C F D )

A

8.6

B

7.4

C

10.1

All three wells have the same composition. The residue of all the heavier components in the condensate has a molecular weight 2-2


of 122 and a density of 760 kg/ m 3 . The characteristics of this component will be accounted for by using the hypothetical component facility in UniSim Design. The compositional analysis of the gas condensate resulted in the following information: C o mp o n e n t

Composition

C o mp o n e n t

Composition

Methane

0.623

n - Pe n t a n e

0.00405

Ethane

0.280

n-Hexane

0.00659

Propane

0.0163

C7 + *

0.00992

i-Butane

0.00433

Nitrogen

0.00554

n-Butane

0.00821

Carbon Dioxide

0.0225

i - Pe n t a n e

0.00416

H y d r o g e n S u l f i d e 0.0154

Pipe diameters for each of the branches are: Branch

Diam eter

Branch 1

3”

Branch 2

3”

Branch 3

3”

Branch 4

4”

Branch 5

6”

A schedule 40 steel pipe is used throughout and all branches are buried at a depth of three feet. All pipes are uninsulated. The following table summarizes the elevation data for each of the branches. The elevation given for the pipe units is for the endpoint of the pipe (i.e., the downstream end). Branch

Unit

Length (ft)

Elevation (ft)

Branch 1

Well A

n/a

2095

Pipe Unit 1

945

2110

Pipe Unit 2

1110

2089

Pipe Unit 3

1056

2090

Well B

n/a

2015

Pipe Unit 1

2822

2090

Branch 2

2 -3

2-4

I ntroduction

Branch

Unit

Length (ft)

Elevation (ft)

Branch 3

Well C

n/a

2085

Pipe Unit 1

528

2125

Pipe Unit 2

334

2080

Pipe Unit 3

670

2077

Branch 4

Pipe Unit 1

1167

2077

Branch 5

Pipe Unit 1

2110

1980

Branches that traverse undulating terrain have been subdivided into a number of segments with elevation points assigned at locations where there is a significant slope change. Such locations in the network are labelled on the schematic diagram with the elevation value in italics. For each of the branches, the resulting distance and elevation data as obtained from the topographic map is listed. With this data, you can simulate the performance of the given system using the PIPESYS extension and thereby calculate important parameters such as pressure losses, temperature changes and liquid-holdup amounts as well as predicting the flow regimes. In this simple example, the flow rate at each well is specified and is independent of the flow rate at each of the other wells. In cases such as this, the system can be modeled with only one pressure drop determination per branch. Simultaneous pressure and temperature calculations can be performed if the temperature at each wellhead is also known.

2-4


The PFD generated by UniSim Design for the completed case is shown below. Figure 2.2

Since pressures are continuous throughout the network, the pressure can be specified at only one point. For instance, the pressure can be fixed at any one well or at the final delivery point and PIPESYS will compute the pressure everywhere else. For this example, a pressure of 1060 psia will be specified for Well A. PIPESYS will then determine the pressures elsewhere in the network that are consistent with this specification. Heat transfer calculations should be performed in the direction of flow whenever possible. Furthermore, wellhead temperatures are generally known. For this example, the fluid temperatures at wells A, B and C are known and must be entered as fixed conditions. PIPESYS will then perform an iterative pipeline calculation in branches where the upstream temperature and downstream pressure are known. Temperatures of the blended fluids will be computed on a mass basis downstream of the junctions of two or more streams.

2 -5

2-6


2 . 2 Settin g Up th e Fl o w sh ee t To model the gathering system with PIPESYS: For additional information on UniSim Design views and conventions, refer to C h a p t e r 1 - I n t e r f a c e in t he U n i S i m D e s i g n U s e r Guide.

1. Start UniSim Design and create a N e w case. 2. In the Simulation Basis Manager, create a fluid package using the data in the following table. P r o p e r t y Pa c k a g e

Pure Components

Peng Robinson

C1, C2, C3, i-C4, n-C4, i-C5, n-C5, C6, Nitrogen, CO2, H2S

3. Create a hypothetical component, C7 + , with the following user-defined properties. Add it to the fluid package before entering the Main Simulation Environment. Nam e

C7+ * *

M o l e c u l a r We i g h t

122* *

I d e a l L i q u i d D e n s i t y [ l b / f t 3 ] 47.45* * ** signiﬁes required input

4. Open the Workbook and add the 10 Material Streams listed below: Material Streams • Well A • Well B • Well C

• • • • •

• FS4 • FS5

PS1 PS2 PS3 PS4 PS5

5. Enter the compositional data for W e l l A as specified in the following table: Component (mole frac.)

Data

Methane

0.623* *

Ethane

0.280* *

Propane

0.0163* *

i-Butane

0.00433* *

n-Butane

0.00821* *

2-6


Component (mole frac.)

Data

i - Pe n t a n e

0.00416* *

n - Pe n t a n e

0.00405* *

n-Hexane

0.00659* *

C7 +

0.00992* *

Nitrogen

0.00554* *

Carbon Dioxide

0.0225* *

Hydrogen Sulfide

0.0154* *

Because the stream composition is identical over the entire system, the composition of the stream specified for Well A may be copied to streams Well B and Well C. 6. Use the D e f i n e f r o m O t h e r S t r e a m . . . button on Well B’s stream view to define its composition by copying the stream specs from Well A. Repeat for Well C. 7. Open the E n e r g y S t r e a m s tab on the Workbook view. Enter the names of five energy streams: Energy Streams • • • • •

ES1 ES2 ES3 ES4 ES5

For this case, each of the five branches of the pipeline will be represented by a separate PIPESYS extension.

2 -7

2-8

Building the Case

2 . 3 Bu ild i n g th e Ca se In this section, you will: • • •

Add five PIPESYS Extensions. Add two mixers. Define streams.

2 . 3 . 1 Ad d th e Fi rst PI PESYS Ex te n si o n 1. Add a PI PESYS Extension to the flowsheet. For a description of all pages in the Main PI PESYS View, see Chapter 2 - PI PESYS Vi e w from the PI PESYS User Guide.

2. Complete the C o n n e c t i o n s tab as shown in the figure below. Figure 2.3

3. Go to the E l e v a t i o n P r o f i l e tab. 4. Enter 0 f t into the Distance field and 2 0 9 5 f t into the Elevation field. 5. Add the first pipe unit for this extension on the E l e v a t i o n P r o f i l e Page. The Pipe Unit view appears. 6. Go to the D i m e n s i o n s tab.

2-8


7. Specify the pipe as 3 i n c h e s in diameter, and select S c h e d u l e 4 0 as shown below. Figure 2.4

8. Go to the H e a t T r a n s f e r tab. 9. Click on the Centre Line Depth cell and click the D e f a u l t button. Leave all other parameters at their default values as shown below. Figure 2.5

10. Click the Cl o se button to close the Pipe Unit view.

2 -9

2-10

Building the Case

11. Complete the Elevation Profile tab by entering 9 4 5 f t for the Run parameter and 2 1 1 0 f t for the Elevation parameter. All other parameters are automatically calculated as shown below. Figure 2.6

12. Add the remaining two pipe units. Because all the pipe units for the extension have identical properties to Pipe # 1, you can use the Cop y and P a s t e buttons as a time saving measure for adding the new units.

2 -1 0


13. Complete the elevation profile as shown by adding the E l e v a t i o n and R u n parameters for all units. Figure 2.7

14. Go to the T e m p e r a t u r e P r o f i l e tab and enter 4 0 °F in the Ambient Temperature field (in the Pipeline Origin group). Figure 2.8

This completes the first PIPESYS extension for your case.

2-11

2-12

Building the Case

2 . 3 . 2 Ad d th e Se co n d PI PESYS Ex te n si o n The second PIPESYS extension consists of a single Pipe Unit. 1. Enter the required information for the second extension as defined in the following table: Ta b

Object

Connections

Nam e

Branch 2

Inlet Stream

Well B

Outlet Stream

PS2

Energy Stream

ES2

Distance [ ft]

0

Elevation [ft]

2015

Pipeline Unit

Pipe # 1

Pipe # 1 Elevation [ft]

2090

Pipe # 1 Run [ft]

2822

Elevation Profile

Pipe Unit View

Te m p e r a t u r e P r o f i l e

Specification

Nominal Diameter [Inches] 3 Pipe Schedule

40

Centre Line Depth

Default

Ambient Temperature [F]

40

The third PIPESYS Extension will be added after the Mixer.

2 -1 2


2 . 3 . 3 Ad d th e Fi rst Mi x er For more information on unit operations, see the UniSim Design Operations Guide.

For this pipeline configuration, a UniSim Design Mixer is used to merge streams. Other UniSim Design operations can be used to merge streams but the Mixer is the simplest to use and the most suitable for this example. 1. Add a M i x e r to your simulation. Named J u n c t i o n 1 , it is used to merge streams PS1 and PS2 as shown below. Figure 2.9

2. On the P a r a m e t e r s page of the Mixer, select the E q u a l i z e A l l radio button in the Automatic Pressure Assignment group. Figure 2.10

2-13

2-14

Building the Case

2 . 3 . 4 Ad d th e Th ird PI PESYS Ex te n si o n This third PIPESYS extension is used to represent Branch 4. It consists of a single pipe unit. 1. Enter the data for the third PIPESYS extension as defined in the following table. Pa g e

Object

Specification

Connections

Nam e

Branch 4

Inlet Stream

FS4

Outlet Stream

PS4

Energy Stream

ES4

Distance [ ft]

0

Elevation [ft]

2090

Pipeline Unit

Pipe # 1


2077

Pipe # 1 Run [ft]

1167

Elevation Profile

Pipe Unit view



40

Centre Line Depth

Default


40

2 -1 4


2 . 3 . 5 Ad d th e Fo u r th PI PESYS Ex te n si o n Branch 3 of this pipeline system is represented by the fourth PIPESYS extension. Three Pipe Units in the elevation profile matrix correctly characterize the changes in elevation occurring over the length of the pipeline. 1. The following table contains the information required to complete the fourth PIPESYS extension:

To save time, add and define Pipe # 1 and then use the Copy and Paste buttons to create Pipe # 2 and Pipe # 3.

Ta b

Object

Specification

Connections

Nam e

Branch 3

Inlet Stream

Well C

Outlet Stream

PS3

Energy Stream

ES3

Distance [ ft]

0

Elevation [ft]

2125

Pipeline Unit

Pipe # 1


2077

Pipe # 1 Run [ft]

528

Pipeline Unit

Pipe # 2


2080

Pipe # 2 Run [ft]

334

Pipeline Unit

Pipe # 3


2077

Pipe # 3 Run [ft]

670

Elevation Profile

Pipe Unit view (All Pipe Units I dentical) Te m p e r a t u r e P r o f i l e


40

Centre Line Depth

Default


40

2-15

2-16

Building the Case

2 . 3 . 6 Ad d th e Fi fth PI PESYS Ex te n si o n The fifth and final PIPESYS extension for this case represents Branch 5 of the pipeline system. In this segment, the total gas flows from Wells A, B and C are merged and the endpoint of the extension is the gas plant. 1. Enter the information for the final extension as defined in the following table: Ta b

Object

Specification

Connections

Nam e

Branch 5

Inlet Stream

FS5

Outlet Stream

PS5

Energy Stream

ES5

Distance [ ft]

0

Elevation [ft]

2090

Pipeline Unit

Pipe # 1


1980

Pipe # 1 Run [ft]

2110

Elevation Profile

Pipe Unit View



40

Centre Line Depth

Default


40

2 -1 6


2 . 3 . 7 Ad d th e Se co n d Mi x er A second Mixer merges the streams from Branches 3 and 4 with the outlet stream entering Branch 5. 1. Add a Mixer named J u n c t i o n 2 to your simulation. Inlet streams for the mixer are PS3 and PS4 and the outlet stream is FS5 as shown in the figure below: Figure 2.11

2. On the P a r a m e t e r s page of the Mixer, select the E q u a l i z e A l l radio button in the Automatic Pressure Assignment group.

2-17

2-18

Building the Case

2 . 3 . 8 D e fin e th e Well St re am s To finish the case and have PIPESYS complete the calculation, the following stream parameters for the wells are required. 1. Finish specifying streams Well A, Well B and Well C with following data: Stream

Object

Specification

We l l A

Temperature [F]

105

Pressure [ psia]

1060

Molar Flow [ MMSCFD]

8.6

Temperature [F]

115


7.4

Temperature [F]

110


10.1

We l l B We l l C

2. Save your case as n e t w o r k . u s c .

2 -1 8


2 . 4 Vi ew in g th e Re su lts Go to the M a t e r i a l S t r e a m s tab of the main Workbook. The results calculated for the product streams should appear as follows: Figure 2.12

To optimize the performance of the gas condensate gathering system created in this example, see C h a p t e r 3 - O p t i m i z e G a s C o n d e n s a t e G a t h e r i n g S y s t e m which discusses optimizing the gas condensate gathering system.

2-19

2-20

View ing the Results

2 -2 0

Optimize Gas Condensate Gathering System 3-1

3 O p t i m i z e Ga s Co n d e n sa t e Ga t h e r in g Sy s t e m 3 . 1 I n t r o d u c t i o n ................................................................................... 2 3.2 Building the Case ........................................................................... 3 3.2.1 3.2.2 3.2.3 3.2.4

Add an Adjust .......................................................................... Add an Inline Compressor ......................................................... Compare Compressors ..............................................................6 Adjust Flow Rates.....................................................................

3.3 View ing the Results ....................................................................... 9

3 -1

3-2

I ntroduction

3 . 1 In t r o d u ct io n This application is a continuation of C h a p t e r 2 - G a s C o n d e n s a t e G a t h e r i n g S y s t e m , in which you modelled the performance of a small gas condensate gathering system given fixed wellhead rates and plant delivery requirements. As the next step, you will attempt to increase production from the wells by adding a compressor to the fifth PIPESYS extension. Using supplied wellhead performance curves, the effect of lowering the pressure at the wellheads will be gauged in terms of the resulting increased flow rates. The following figure shows the PFD for the completed application. Figure 3.1

3-2

Optimize Gas Condensate Gathering System 3-

3 . 2 Bu ild i n g th e Ca se You must complete the Chapter 2 - Gas Condensate Gathering S y s t e m before you can work on this application.

Start UniSim Design and load the case file n e t w o r k . u s c that you saved upon completion of the first application.

3 . 2 . 1 Ad d a n Ad ju st The first modification you make will be to add an ADJUST operation. The adjust will be used to maintain a constant pressure of 1000 psia at the gas plant with the pressure at Well A being the adjusted variable. 1. Add an ADJUST operation with the following specifications. Object

Specification

Nam e

Adjust

A d j u s t e d Va r i a b l e - O b j e c t

Well A

A d j u s t e d Va r i a b l e - Va r i a b l e

Pressure

Ta r g e t Va r i a b l e - O b j e c t

PS5

Ta r g e t Va r i a b l e - Va r i a b l e

Pressure

S p e c i f i e d Ta r g e t Va r i a b l e

1000 psia

Method

Secant

To l e r a n c e

0.10 psi

S t ep Si z e

100 psi

M a x . I t e r.

25

2. Click the S t a r t button at the bottom of the Adjust property view to begin the adjust calculations. (UniSim Design may need several minutes to reach a solution.) The entire PIPESYS network must be recalculated for each iteration. Upon convergence, the well pressures should be: We l l

Pressure (psia)

A

1093

B

1077

C

1052

3 -3

3-4

Building the Case

3 . 2 . 2 Ad d a n In l in e Co m p re sso r For more information on adding and defining compressor parameters, see C h a p t e r 5 - I n l i n e C o m p r e s s o r from the PI PESYS User Guide .

The next step will be to add an inline compressor at the upstream end of PIPESYS Branch 5. If this addition reduces the pressure at the wells to an extent that production can be significantly increased, then the additional cost of the compressor is justifiable. It is also useful to look at the incremental performance increase of a larger compressor in order to get a feel for sizing the compressor. The performance of a 1000 hp compressor to that of a 750 hp compressor will be compared for this application. To add a Compressor to the upstream end of the PIPESYS extension Branch 5: 1. Go to the E l e v a t i o n P r o f i l e tab of Branch 5. 2. Modify the pipe extension, so that the C o m p r e s s o r is placed before the P i p e . See the figure below for placement of the pipe units: Figure 3.2

The performance of the 1000 hp compressor will be evaluated first.

3-4


3. Open the Inline Compressor view: Figure 3.3

4. Use the following information to complete the tabs as specified on the Inline Compressor view. Object

Specification

O n t h e Pa r a m e t e r s t a b Brake Power - Specified

1000 hp

Max. Discharge Temp

100 F

Max. Interstage Temp

100 F

Number of Stages

2

Adiabatic Efficiency

0.73

Interstage delta P

10 psi

On the Mechanical Losses tab Overall Efficiency

0.95

The solution process may take several minutes to perform the iterative calculation for the PIPESYS network and converge. When the process is complete, the well pressures should be as follows: We l l

Pressure (psia)

A

686.7

B

655.9

C

619.5

3 -5

3-6

Building the Case

To compare the performance between two compressors, the same calculations are repeated using a 750 hp compressor. 5. On the Inline Compressor view, go to the P a r a m e t e r s tab. 6. In the Brake Power group, change the 1 0 0 0 h p in the Specified cell to 7 5 0 h p . When UniSim Design completes the iteration, the new pressures are: We l l

Pressure (psia)

A

753.2

B

726.3

C

693.5

3 . 2 . 3 Co m p a r e Co m p re sso rs The PIPESYS calculations indicate that when a 1000 hp compressor is used the wellhead pressure is lower than when a 750 hp compressor is used. However, this may not result in an economically significant higher production rate, especially if these pressures are located on the steeper region of the wellhead performance curve. F i g u r e 3 . 4 , F i g u r e 3 . 5 and F i g u r e 3 . 6 at the end of this application show the wellhead performance curves for Well A, Well B and Well C, respectively. These curves can be used to evaluate compressor size that would be most economical for use in a particular pipeline network. Locate 686.7 psia and 753.2 psia on the Well A wellhead curve and you should find that these correspond to flows of 11.1 MMSCFD and 10.8 MMSCFD, respectively. This indicates that the 1000 hp compressor would increase production by less than 5% , over that of the 750 hp compressor. It is therefore reasonable to conclude that adding compression to the system is worthwhile since both compressors lower the wellhead pressures by a large amount, but the small increase in production may not be enough to justify the choice of the 1000 hp compressor. For this example, assume that economic and engineering considerations favour installing the 750 hp compressor.

3-6


3 . 2 . 4 Ad ju st Fl o w Ra te s In the previous section, it was determined that compression would significantly improve production and that the 750 hp compressor was the better candidate for doing so. Now you must find the actual flow rates and wellhead pressures that correspond to having the compressor in the system. This will be a process of adjusting the flow rates at each of the wells to manually converge on a particular point on the wellhead curves. 1. Locate the flow rates on the wellhead performance curves that correspond to the pressures calculated on the Mechanical Losses page. Reading from the curves these should be: We l l

Pressure ( psia)

F lo w (M M S C F D )

A

753.2

10.8

B

726.3

9.6

C

693.5

12.4

2. Click the S t o p icon in the toolbar. Stop icon

Go icon

3. Enter the flow rates from the above table into the stream data for the wells. Specify a value of 10.8 MMSCFD for the Molar Flow of Well A. Sim ilarly, enter the flow rates for Well B and Well C. 4. Click the Go icon in the toolbar and let PIPESYS complete the iterations. When the program is finished solving the network, the new well pressures calculated by PIPESYS should be: We l l

Pressure ( psia)

A

868.5

B

838.0

C

783.0

3 -7

3-8

Building the Case

5. Find the flow rates that correspond to these pressures from the wellhead curves. These values should be: We l l

F lo w (M M S C F D )

A

10.3

B

9.0

C

11.9

6. Once again, click the S t o p button and enter the flow rates from the previous table into the well stream data. 7. Click the Go button. When the program is finished, the well pressures should read: We l l

Pressure ( psia)

A

842.5

B

810.9

C

763.8

You will find that the flow rate and pressure for Wells B and C are close enough to the curves and can consider these to be a valid solution. However, the point 10.3 MMSCFD and 844.5 psia on the Well A Wellhead Performance curve is still some distance from the graph. You will need to do one or two more iterations to find the solution. 8. Find the flow rate on the Well A curve that corresponds to 844.5 psia, (this should be 10.5 MMSCFD). Click the S t o p button and enter 10.5 MMSCFD into the flow rate parameter for the Well A stream. 9. Click the Go button. When the program is finished, pressures at the wells should be: We l l

Pressure ( psia)

A

849.0

B

813.1

C

765.3

3-8


3 . 3 Vi ew in g th e Re su lts Now the pressure/ flow rate for Well A is reasonably close to the curve. The pressures for B and C have changed a little but not significantly from the last iteration. Fortunately, the pressure at a given well is fairly insensitive to pressure changes at any of the other wells. This process can be repeated to obtain a solution of any arbitrary precision subject to the limits imposed by the computer, but this solution is accurate enough for further analysis. Compression has increased flow rates by a considerable amount: We l l

Flow Without Compression ( MMSCFD)

Flow With Compression ( MMSCFD)

A

8.6

10.5

B

7.4

9.0

C

10.1

11.9

The engineering analysis shows that adding the compressor increased production by about 20% at each of the wells. These results can be used in an economic study to further examine the value of adding compression to the pipeline system.

3 -9

3-10


Figure 3.4

3 -1 0


Figure 3.5

3 -1 1

3-12


Figure 3.6

3 -1 2

References

A-1

A Re f e r en ce s 1

2

3

4

5

6

7

8

9

American Petroleum Institute, “Subsurface Controlled Subsurface Safety Valve Sizing Computer Program”, API Manual 14BM, Second Ed., p. 38, API, January (1978) American Petroleum Institute, Technical Data Book - Petroleum Refining, API, New York (1982) Aziz, K., Govier, G.W., and Fogarasi, M.,“Pressure Drop in Wells Producing Oil and Gas”, Journal of Canadian Petroleum Technologists., Vol. 11, p. 38, July (1972) Baker, O. “Simultaneous Flow of Oil and Gas”, Oil & Gas Journal, Vol. 54, No. 12, p. 185, July (1954) Baker, O. “Experience with Two-Phase Pipelines”, Canadian Oil & Gas Industry, Vol. 14, No. 3, p. 43, March (1961) Beggs, H.D ., and Brill, J.P. “A Study of Two-Phase Flow in Inclined Pipes”, Journal of Petroleum Technologists, p. 607, May (1973) Bendiksen, K.H., Maines, D ., Moe, R., and Nuland, S., “The Dynamic Two Fluid Model OLGA: Theory and Application”, SPE Paper No. 19451, SPE Production Engineering, May (1991) Burke, N.E., and Kashou, S.F., “History Matching of a North Sea Flowline Startup Using OLGA Transient Multi-phase Flow Simulator”, SPE Paper No. 24789, Presented at the 67th Annual SPE Technical Conference and Exhibition, Washington, DC, October (1992) Chen, N.H., “An Explicit Equation for Friction Factor in Pipe”, Ind. Eng. Chem. Fund., Vol. 18, No. 3, p. 296 (1979)

10

11

12

Dukler, A.E., Wicks, M., and Cleveland, R., “Frictional Pressure Drop in Two-Phase Flow: B. An Approach Through Similarity Analysis”, AIChE Journal, Vol. 10, No. 1, p. 44, January (1964) Dukler, A.E., “Gas-Liquid Flow in Pipelines”, Monograph, Project NX28, AGA/API, May (1969) Duns, H., Jr., and Ros, N., “Vertical Flow of Gas and Liquid Mixtures in Wells”, Paper No. 22, Section II, World Petroleum Conference, Frankfurt, Germany (1963)

A-1

A-2

13

14

15

16

17

18

19

20

21

22

23

24

25

Eaton, B.A., Andrews, D. E., Knowles, C.R., Silberberg, I.H., and Brown, K.E., “The Prediction of Flow Patterns, Liquid Holdup and Pressure Losses Occurring During Continuous Two-Phase Flow in Horizontal Pipelines”, Journal of Petroleum Technologists, p. 815, June (1967) Flanking, O., “Effect of Uphill Flow on Pressure Drop in Design of TwoPhase Gathering Systems”, Oil & Gas Journal, p. 132, March (1958) Fuchs, P., “The Pressure Limit for Terrain Slugging”, Paper B.4, Proc. of the 3rd International Conference on Multi-phase Flow, BHRA, The Hague, Netherlands (1987) Govier, G.W., and Aziz, K., The Flow of Complex Mixtures in Pipes, Van Nostrand-Reinhold, (1972), reprinted by Robert E. Krieger Publishing Co., Huntingdon, New York (1977) Govier, G.W., and Fogarasi, M., “Pressure Drop in Wells Producing Gas and Condensate”, Journal of Canadian Petroleum Technologists, October (1975) Gregory, G.A., “Estimation of the Overall Heat Transfer Coefficient for Calculating Heat Loss/ Gain in Flowing Wells”, Technical Note No. 4, Neotechnology Consultants Ltd., Calgary, Canada, March (1991) Gregory, G.A., Mandhane, J., and Aziz, K. “Some Design Considerations for Two-Phase Flow in Pipes”, Journal of Canadian Petroleum Technologists, January-March (1975) Gregory, G.A., “Comments on the Prediction of Minimum Unloading Velocities for Wet Gas Wells”, Technical Note No. 14, Neotechnology Consultants Ltd., Calgary, Canada, December (1989) Gregory, G.A., “Estimation of the Overall Heat Transfer Coefficient for the Calculation of Pipeline Heat Loss/ Gain”, Technical Note No.3, Neotechnology Consultants Ltd., Calgary, Canada, October (1984), 1st Revision September (1990), 2nd Revision March (1991) Hooper, W.B., “The Two-K Method Predicts Heat Losses in Pipe Fittings”, Chemical Engineering, p. 96, August (1981) Hughmark, G.A., “Holdup and Heat Transfer in Horizontal Slug GasLiquid Flow”, Chem. Eng. Sci., Vol 20, p. 1007 (1965) Hughmark, G.A. “Holdup in Gas-Liquid Flow”, Chem. Eng. Prog., Vol. 58, No. 4, p. 62, April (1962) Lockhart, R.W., and Martinelli, R.C. “Proposed Correlation of Data for Isothermal Two-Phase, Two-Component Flow in Pipes”, Chem. Eng. Prog., Vol. 45, No. 1, p. 39, January (1949)

A-2

References

26

27

28

29

30

31

32

33 34

35

A-3

Mandhane, J., Gregory, G., and Aziz, K., “A Flow Pattern Map for GasLiquid Flow in Horizontal Pipes”, International Journal of Multi-phase Flow, Vol. 1, p. 537 (1974) Mandhane, J.M., Gregory, G.A., and Aziz, K., “Critical Evaluation of Friction Pressure-Drop Prediction Methods for Gas-Liquid Flow in Horizontal Pipes”, Journal of Petroleum Technologists, p. 1348, October (1977) Mukherjee, H., and Brill, J.P., “Liquid Holdup Correlations for Inclined Two-Phase Flow”, Journal of Petroleum Technologists, p. 1003, May (1983) Oliemans, R.V.A., “Two-Phase Flow in Gas-Transmission Pipelines”, Paper No. 76-Pet-25, Joint Petroleum Mechanical Engineering & Pressure Vessels and Piping Conference, Mexico City, Mexico, September (1976) Oliemans, R.V.A., “Modeling of Gas Condensate Flow in Horizontal and Inclined Pipes”, Proc., ASME Pipeline Eng. Symp., ETCE, p. 73, Dallas, Texas, February (1987) Pots, B.F.M., Bromilow, I.G., and Konijn, M.J.W.F., “Severe Slug Flow in Offshore Flowline/ Riser Systems”, SPE Prod. Eng., p. 319, November (1987) Salama, M.M and Venkatesh, E.S., “Evaluation of API RP 14E Erosional Velocity Limitations for Offshore Gas Wells”, Paper No. OTC 4485, presented at the 15 t h Annual Offshore Technology Conference, Houston, May (1983) Singh, B., and Gregory, G.A., unpublished work (1983) Taitel, Y., and Dukler, A. “A Model for Predicting Flow Regime Transitions in Horizontal and Near Horizontal Gas-Liquid Flow”, AIChE J., Vol. 22, No. 1, p. 47, January (1976) Tennessee Gas Pipeline Co., private communication (1979)

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UniSim Design PIPESYS Tutorial

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