2011 winprop tutorial

7/23/2019 2011 WinProp Tutorial

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WinProp

TutorialDry Gas, Wet Gas, Gas Condensate,

Volatile Oil, Black Oil, and Heavy Oil

Prepared for: Petroleum Institute Abu Dhabi

Instructor: Amir Moradi

December 2011


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Table of Contents

Exercise 1 Base Models of Five Different Fluid Types........................ 3

Basic Setup and Dry Gas Fluid Model Creation .................................................................................. 3

Additional Exercises ............................................................................................................................. 19

Exercise 2 Determination of MMP and MME.................................... 24

Addition of Injection Streams and Calculations ................................................................................ 24

Multi-Contact Miscibility Minimum Pressure Calculation .............................................................. 28

Exercise 3 Creation of Raleigh Black Oil........................................... 30

Setup of WinProp model with Plus Fraction Splitting ...................................................................... 30

Defining Calculations and Experimental Values ............................................................................... 32

Using Regression to Match WinProp model to Laboratory Results ................................................ 36

Matching Viscosity in WinProp to Laboratory Values ..................................................................... 39

Defining an IMEX Fluid Model Output ............................................................................................. 41

Exercise 4 Heavy Oil Fluid Model...................................................... 46

Setup of WinProp model with Plus Fraction Splitting ...................................................................... 46

Matching of WinProp Model to Laboratory Results ......................................................................... 48

Matching of WinProp Model Viscosity to Laboratory Viscosity ...................................................... 52

Creating a STARS PVT Model from WinProp .................................................................................. 56


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Exercise 1 Base Models of Five Different Fluid Types

The purpose of this exercise is to utilize WinProp to build 5 different types of fluid models. Ageneral understanding of the interface and associated windows should be gained in the process ofcreating fluid models for Dry Gas, Wet Gas, Gas Condensate, Volatile Oil, and Black Oil cases.

Basic Setup and Dry Gas Fluid Model Creation1. Double click on the WinPropicon in the Launcher and open the WinProp interface.

Please note that this courses images and descriptions are based on WinProp

version 2011.10 or newer.

2. Open the Titles/EOS/Unitsform and write Dry Gas in the Comment Linesection andthe Title Line 1section.

When inputting data for the other fluid models (Wet Gas, Gas Condensate,etc.) input the appropriate name for the model.

Select PR 1978 as the equation of state to be used in characterizing the fluid model,select Psia & deg F as the units and Feed as "Mole".

Figure 1: Title/EOS/Units Screen

3. Go to Component Selection/Propertiesform and insert the library components in thefollowing order:


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CO2, N2, C1, C2, C3, IC4, NC4, IC5, NC5, and FC6.

To do this click on the Ins Libbutton (Insert Library Component) and select the librarycomponents you wish to insert (select multiple components at a time by holding Shift or

Control) then click on the right arrowto add the components (Figure 3), and click OKto finalize.

If you need to inset a component you missed (Figure 4), select the component abovewhere you want to inset the new component (Figure 5), and then use Ins Lib again toinsert the new component directly under the current selection. (*Note: This feature isnot working properly in Windows. It works only if you insert missing C2H6 when

cursor is at CO2 location. It also works if you select one additional component).

Figure 2: How to Insert Library Components


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Figure 3: Selection of Components

Figure 4: Component Definition Missing C2 Compound


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Figure 5: Select CH4 then use Ins Lib to insert the missing C2H6 Compound

immediately below.

Note on Order:

The order of these components only matters in the input of compositions. In theseexamples the compositions will be copied from an Excel file in this order whichimplies that the order will be important.

4. In all cases, except Dry Gas, also characterize the C7+ fraction with a single

pseudocomponent by inserting a user defined component (Figure 6).

In theComponent Selection/Properties form select the last component on the list, thenclick on the Ins Ownbutton. Click the New Rowbutton, and enter the information forcomponent name, specific gravity (SG) and molecular weight (MW).

Use the properties given in the file Five Fluid Types Data.xls under the REQUIREDDATAfolder. Your component definition form should look like Figure 7 for Dry gasand Figure 8 in case of other fluid types. Click OKto close the Form.


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Figure 6: Definition of C7+ Variable for Black Oil Fluid Type

Figure 7: Example of Dry Gas Component Definition Screen


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Figure 8: Example of Black Oil Component Definition Screen

5. Open the Compositionformand input the mole fractions of the primary composition

as mentioned in the file Five Fluid Types Data.xls (Figure 9). The secondarycorresponds to the injection fluid (if applicable). The secondary stream concept will becovered in a later section.

(*Note: it is important that you enter a value of 0 for any components that are notpresent otherwise an empty space will cause the simulator to error.)

Figure 9: Example of Black Oil Composition Form with compositions copy/pasted

from excel file

6. Insert aTwo-phase Flashform into the WinProp interface. Make sure that in doingthis you have first selected the Composition form.


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It is important when adding new calculations to always click on the form you want toinsert the calculation after/into. If any calculations need to be moved in a differentorder they must be copied/pasted by right clicking on the item and selecting copy/pasteafter respectively.

Open the newly inserted form by clicking on it and under the comments section typeStandard condition flash. We will be performing a flash at 14.7 Psiaand 60 deg F.Leave other calculation options as default. The feed composition is subjected to mixed(i.e. primary and secondary composition). The Two-phase Flashform should look likeas shown in Figure 10.

Figure 10: Example of Two-Phase Flash Calculation Form

7. Insert a Saturation Pressure form into the WinProp Interface to perform asaturation pressure calculation at the reservoir temperature.

8. Open the Saturation Pressure Calculation form. Under the comments type Psat atreservoir temperature. Also, input the reservoir temperature and saturation pressure


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estimate as180 Fand1000 Psiarespectively(for Dry Gas). In the other cases insertthe temperature as given in the Excel filebut still use1000 Psia.

The input value of Saturation Pressure Estimate is used as an initial guess by WinPropduring the iteration processes for calculating the actual saturation pressure.

Figure 11: Example of Two-Phase Saturation Pressure Form for Dry Gas

9. We would also like to generate a pressure-temperature phase diagram. Insert a Two-

phase Envelope form. Open the form and type in P-T envelope under thecomments section. Input the data as shown in Figure 12.


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Figure 12: Example of Two-Phase Envelope Construction for Dry Gas

10. Create plots of phase properties vs. pressureat the reservoir temperatureusing the2-phase flash calculation.

Examples of properties which may be plotted are: Z-factors, phase fractions, densities,molecular weights, K-values, etc.

This can be done by adding another Two-phase Flash calculation form. Type in thecomments Phase properties as a function of Pressure. Input the reservoirtemperature as 180 deg F (for Dry Gas), temperature step as 0 and No. oftemperature steps as 1. Input the reservoir pressure as 250 Psia, pressure step of250 Psia and No. of pressure steps as 12 for dry and wet gas cases, and 24 for gascondensate, volatile oil and black oil. The reservoir temperature will also changedepending on the case you are modeling, as mentioned in the file Five Fluid TypesData.xls.


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Figure 13: Example of Two-Phase Flash Calculation used in setting up Plots for Dry

Gas. Other cases will have differing temperatures

11. In the plot control tab of the two-phase calculation form select the propertiesdepending on the case as follows:

No. Case Plot Property

1 Dry Gas Z compressibility factor2 Wet gas Z compressibility factor3 Gas Condensate, Volatile Oil & Black oil Phase volume fraction,

Z factor, K-values (y/x)


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12. For all the oil cases, add a single-stage separatorcalculation with separator pressureof 100 psiaandseparator temperatureof75 F. In order to do this add the Separator

Calculation . Click anywhere inside the table to allow you to click the button labeledInsert Sep.

Under Sat. Pres.make sure Pres. is2000 psiaand the Temp. is the same as in the fileFive Fluid Types Data.xls, for the specific fluid type, and click OK(Figure 14).

(*Note this is to be done only for oil cases)

Figure 14: Example of Separator Form for Black Oil

13. The final WinProp interface should look like Figure 15 for the Gaseous Cases. The oilcases will have a Separator Calculation added after the last Two-Phase FlashCalculation.


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Figure 15: WinProp interface for modeling Dry Gas case

14. Savethe WinProp file as drygas.dat and Runit.

15. Repeat Steps 1 to 14 and build a dat file for other types of fluid and save them aswetgas.dat, gascondensate.dat, volatileoil.dat, and blackoil.dat files respectivelyand then run.

After running these jobs analyze the Simulation Results for the different cases. These are

demonstrated in Figure 16 to 24.


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Figure 16: 2-Phase P-T diagram for Dry Gas case


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Figure 17: Vapor Z factor for Dry gas case

Figure 18: 2-Phase P-T diagram for Wet Gas case

Figure 19: Vapor Z factor for wet gas case


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Figure 20: 2-Phase P-T diagram for Gas condensate case

Figure 21: Phase volume fractions and Z factors for gas condensate


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Figure 22: K value for gas condensate case

Figure 23: 2-Phase P-T diagram for Volatile oil case


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Figure 24: 2-Phase P-T diagram for Black oil case

Additional Exercises

For the black oil data case, investigate the effect on the simulated separator calculation inducedby changing the following parameters:

Apply the volume shift correlations Set the hydrocarbon binary interaction parameters to zero Reduce the C7+ Pc by 20%

1. To set volume shift to correlations, open Component Selection/Properties and click onCalculate Volume Shift buttonthen save as 'blackoil1_volshift correlation value.dat' file(Figure 25). Go back to the Volume Shifttab again and click on Zero Volume Shiftandsave as 'blackoil1_volshift set to zero.dat' file.

Runboth data files and compare the results of the Separator calculations. These can befound at the bottom of the output file which can be opened in a text editor.


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Figure 25: Calculate volume shift values

The Separator Calculations should look like to the following outputs:

Separator output with Volshift set to zero:Oil FVF = vol of saturated oil at 2861.95 psia and 170.0 deg F per vol of stock tank oilat STC(4) = 1.111API gravity of stock tank oil at STC(4) = 58.10

Separator output with Volshift set to correlation value:Oil FVF = vol of saturated oil at 2861.95 psia and 170.0 deg F per vol of stock tank oilat STC(4) = 1.137API gravity of stock tank oil at STC(4) = 32.77


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2. Open blackoil.dat again and set hydrocarbon binary interaction parameterto zero. Dothis by clicking on Component Selection/Properties, click on the Int. Coef.tab (Figure26) and click on HC-HC Groups / Apply value to multiple non HC-HC pairs.

Check on HC-HCand change Exponent value to zero(Figure 27), and press OK. Save as

'blackoil1_int_coeff_zero.dat' and Runthe model. Observe the result from the Separatorcalculation in the output file. It should appear as follows:

Oil FVF = vol of saturated oil at 2014.47 psia and 170.0 deg F per vol of stock tank oilat STC(4)= 1.115API gravity of stock tank oil at STC(4) = 58.16

Figure 26: Int. Coef. Tab under Component Selection


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Figure 27: Step 17, Setting HC-HC Exponent to Zero

3.

Change the Critical Pressure of the heaviest componentto see its effects.

To reduce the C7+ Pc by 20%, in Component Selection/Properties change the Pcvalue of C7+ to 12.36 click Apply Change (Figure 28). Save as'blackoil1_int_coeff_reduce_Pc.dat' and Runit.

Observe the result from the Separator calculation in the output file. It should appear asfollows:

Oil FVF = vol of saturated oil at 1589.51 psia and 170.0 deg F per vol of stock tank oilat STC(4) = 1.103API gravity of stock tank oil at STC(4) = 104.81


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Figure 28: Changing the C7+ Component's Pc to 12.36 atm


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Exercise 2 Determination of MMP and MME

The purpose of this exercise is to utilize WinProp to determine the Minimum MiscibilityPressure (MMP) and Minimum Miscibility Enrichment (MME) for a rich gas injection into areservoir. This is generally related to enhanced oil recovery techniques such as CO2 floodingwhere a gas is injected at a pressure sufficient to become miscible with the native hydrocarbon.This can lead to a decrease in viscosity and interfacial tension which can increase mobility.

Addition of Injection Streams and Calculations

1. Open the black oil data set from Exercise 1 blackoil.dat and Delete all of thecalculations EXCEPT the Title/EOS/Units, Component Selection/Properties,Composition, and Saturation Pressure (Figure 29).

Figure 29: Exercise 2 Starting Parameters from Exercise 1 Black Oil Data

A variety of secondary injection streams will be added in order to determine their interactionswith the native hydrocarbons. These will include the following compositions:

Pure N2


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Pure CO2 Dry gas (from Exercise 1) A rich gas stream with the composition (in mole %):

CO2 1.4 IC4 3.8N2 1.0 NC4 9.6

C1 33.2 IC5 2.1C2 23.3 NC5 0.3C3 25.3

2. To do this, begin by opening the existing CompositionForm. Under the second columnlabeled Secondary enter 100.00 into the box relating to N2. Rename the form to be"Black Oil + N2" then hit OK (Figure 30).

Figure 30: Addition of N2 Secondary Stream to Composition

3. Next add a 2-Phase Envelopecalculation and Name it "N2 Injection. Copy and Pastethe new Component and 2-Phase EnvelopeForms in the Menu so that you have twosets of them.

4. In the second set change the Secondary stream to 100.00 for CO2 and 0.00 for N2.Rename the Component form and 2-Phase form.


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5. Repeat the Copy/Paste and set the forms up for Dry Gas(which you get the properties offrom the Five Fluid Types Data.xls excel file) and Rich Gas.

The required forms and their arrangement of the calculation options in WinProp interface shouldlook as shown in Figure 31 for this Exercise. Save this file as

blackoil_richgas_MMP_MME.dat.

Figure 31: Addition of solvents in black oil

6.

7.

Implement a multi-contact miscibility (MCM) calculation to determine the MMP for purerich gas injection. Insert a Multiple Contacts calculation form by clicking on theCalculations drop down menu and going down to Multiple Contacts. Input the datashown in Figures 32 and 33.


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Figure 32: Input data for calculation of MMP

Figure 33: Rich gas (make-up gas) composition for calculation of MMP

Analyze the output file for results of single contact miscibility and multi-contact miscibilitypressures and mole fraction of make-up gas:

SUMMARY OF MULTIPLE CONTACT MISCIBILITY in *.OUT file

CALCULATIONS AT TEMPERATURE = 170.000 deg F


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______________________________________________

FIRST CONTACT MISCIBILITY ACHIEVEDAT PRESSURE 0.48250E+04 psia

MAKE UP GAS MOLE FRACTION = 0.10000E+01

MULTIPLE CONTACT MISCIBILITY ACHIEVEDAT PRESSURE = 0.37250E+04 psiaMAKE UP GAS MOLE FRACTION = 0.10000E+01

BY BACKWARD CONTACTS - CONDENSING GAS DRIVE

Multi-Contact Miscibility Minimum Pressure Calculation

Run a multi-contact miscibility calculation to determine the minimum amount of rich gasnecessary to add to the dry gas to achieve miscibility at 4500 psi (MME calculation).

1.

Insert a new Multiple Contactsform and input the following parameters.

Notice that in this case only one pressure value is used at which the miscibility isdesired. In the composition form the starting point for the make-up gas fraction isfrom 50%.

Figure 34: Input data for calculation of MME calculation


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Figure 35: Rich gas (make-up gas) composition for calculation of MME

Analyze the output file for results of single contact miscibility and multi-contact miscibilitypressures and mole fraction of make-up gas:

SUMMARY OF RICH GAS MME CALCULATIONS AT TEMPERATURE = 170.000 deg F

FIRST CONTACT MISCIBILITY PRESSURE

(FCM) IS GREATER THAN 0.45000E+04 psia

MULTIPLE CONTACT MISCIBILITY ACHIEVEDAT PRESSURE = 0.45000E+04 psiaMAKE UP GAS MOLE FRACTION = 0.90000E+00 psiaBY BACKWARD CONTACTS - CONDENSING GAS DRIVE


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Exercise 3 Creation of Raleigh Black Oil

The purpose of this exercise is to utilize WinProp in building a Black Oil fluid model. Thisexercise will introduce the concept of Plus Fraction Splitting of components and the tuning ofcomponent values and Equation of State to match laboratory experiments such as ConstantComposition Expansion (CCE), Separator Tests, and Differential Liberation (DL). This will bedone on a new WinProp model.

Setup of WinProp model with Plus Fraction Splitting

1. Initialize WinProp through CMG launcher.

2. In the Titles/EOS/Unitsform insert a title: Plus fraction characterization and selectPR (1978), Psia & deg F, and feed as moles.

3. In the Component Selection/Propertiesform add the following library components:

CO2, N2, and C1-C6(DON'T ADD C7+)

Under the Compositionform add the compositions as given in the file:Raleigh black oil-data1.xls.

Figure 36: Black oil composition for Raleigh oil


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4. To add and split the C7+ fraction into pseudo-components select Compositionthen clickCharacterization|Plus Fraction Splitting.

On the General Tab specify Gamma distribution function, the first single carbonnumber in plus fraction as 7, 4Pseudocomponents, Lumping Method as Gaussian

Quadrature, and leave the other properties as default.

Figure 37: Plus fraction splitting for Raleigh Oil General Tab

5.Go to

Sample 1Tab and input the

MW+as

190,

SG+as

0.8150,and

Z+(mole fractionof C7+ fraction) as 0.2891. Make sure alpha is equal to 1.

Figure 38: Plus fraction splitting for Raleigh Oil Sample 1 Tab


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6. Savethe dataset as raleigh oil.dat and Runit.

After running the data set, use the Update component propertiesin the File menuanddelete Plus Fraction Splitting. Save the data set as raleigh oil_plus fractionsplitting.dat. You will now notice that 4 hypothetical pseudo components have been

added in the components form.

Defining Calculations and Experimental Values

1. In order to match the CCE, Differential liberation and separator test, use the data given inthe file Raleigh black oil-data1.xls.

Add Saturation Pressure, Constant Composition Expansion, Separator, andDifferential Liberationforms in sequence. Input the experimental data given in the file

Raleigh black oil-data1.xls (Figures 39-44). (You can also input all above forms, fromanother WinProp dataset by copy/pasting).

Figure 39: WinProp Forms Inserted in Step 7


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Figure 40: Saturation Pressure Form with Data from Excel File

Figure 41: Constant Composition Expansion Form with Values for Pressure and

Exp. ROV Copy/Pasted from Excel


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Figure 42: Separator Form Populated with data from Excel file


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Figure 43: Experimental Tab of Separator Form Populated with Data from Excel

file


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Figure 44: Differential Liberation Pressure Levels Tab with Excel Data (entire excel

table can be copied and pasted directly into this)

2.

In the Component Selection/Properties form, click the Calculate Volume ShiftButton and hit Apply Change to calculate the volume shifts using correlation values.Save your model as raleigh oil_experimental data.dat and Run it once to validateyour model and check for errors in the input data.

Using Regression to Match WinProp model to Laboratory Results

3. Select Differential Liberation then click on Regression Start on the top menu toplace Regression Parametersafter everything else. In Regression Parametersgo to theComponent Propertiestab.

Select Pcand Tcfor the Heaviest Component.

For all of the C7+ pseudocomponents and C1 select the volume shifts(Figure 45).

Figure 45: Component Properties for experimental data matching


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In the Interactions Coefficients tab, select the hydrocarbon interaction coefficientexponent(Figure 46). Set the convergence tolerance to 1.0E-06 in Regression Controlstab (Figure 47).

Figure 46: Interaction Coefficients tab setting Hydrocarbon Interaction Coefficient

Exponent

Figure 47: Regression Control tab displaying where to change the Convergence

tolerance

4. Select Differential Liberation and Delete/Cut, and then click on RegressionParametersandPaste into Reg-Block.

SelectSeparatorandDelete/Cut then click onRegression ParametersandPaste intoReg-Block.


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Do this for both Constant Composition Expansion andSaturation Pressureas well.Your window should now look like Figure 48. Runand check for errors in the output file.

Figure 48: WinProp Calculations Layout including Regression Parameters

5. Adjust the weight of some key experimental data points. Try setting the weight for theAPI gravity

to5.0

in theSeparator -> Experimental Data

tab; 10.0in theSaturation

Pressure form; and in the Differential Liberation form set the API gravity at STDconditionsto 0.0. Re-runthe regression.

6. In some cases, you may have to change the lower and upper bounds of the regressionparameters depending on whether these bounds are reached during the regression. In thiscase the following bounds were used:


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Figure 49: Variable bounds used during the regression

Analyze the *.out file and refer to the Summary of Regression Resultsfor comparisonof the experimental versus calculated values.

7. After completing the match to the PVT data, Update component properties and Savethe file under a new name as raleigh oil_experimental data_vis.dat in preparation forviscosity matching.

Matching Viscosity in WinProp to Laboratory Values1. For viscosity matching, temporarily exclude the Saturation Pressure, Constant

Composition Expansion andSeparator calculations from the data set by right-clicking oneach option and select Excludefrom the pop-up menu (Figure 50).


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Figure 50: WinProp Calculations with Exclusions as per Step 15

2. In Differential Liberation set the weight for the viscosity data to 1.0, and all otherweights to 0.0(Figure 51).

Figure 51: Differential Liberation with Weighting Factors of everything except

Viscosity set to 0


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3. In Regression Parameters remove all previously selected parameters from theComponent Properties andInteraction Coefficients tab.

On the Viscosity Parameters tab select C1 and the C7+ pseudo components asregression variables(Figure 52). Runthe data set. Check for errors in the output file.

Figure 52: Viscosity Regression Parameters for C1 and C7+ Pseudo-Components

4.

After completing the match to the viscosity data, Update component properties andSave the file under a new name raleigh oil_Blackoil PVT.dat in preparation forgenerating the IMEX PVT table.

Defining an IMEX Fluid Model Output

1. Select Regression Parameters and Delete/Cut. The Saturation Pressure, ConstantComposition Expansion andSeparatoroptions should still be on the side bar, right-click

on each and choose Include from the pop-up menu. Now select the bottommostcalculation form and Add After -> Simulator PVT -> Black Oil PVT Data(Figure 53).


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Figure 53: WinProp Calculations Layout for Step 19

2. In Black Oil PVT Data, enter the saturation pressure data, desired pressure levelsand the separator data (Figure 54). Enter mole fractions of 0.1, 0.2, and 0.3 for theswelling data(Figure 55).

Figure 54: Black oil PVT export for IMEXSaturation Pressure Tab Inputs


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Figure 55: Pressure levels for back oil PVT


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Figure 56: Water properties for back oil PVT

3. Leave the Oil Properties controls at the defaults, and then select Use solution gascomposition for the swelling fluid specification on the Gas Propertiestab. Runthedata set and check the output file.

If you see the following messages in the output file:

Then do the following: Open the *.dat file in Textpad Search for the keyword JSAT-SWEL Make sure that the numbers on the line directly below are only integers (it should be 2

instead of 2.0) Save the file and run the data set again. The messages should be cleared.


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Exercise 4 Heavy Oil Fluid Model

The purpose of this exercise is to utilize WinProp in building a Heavy Oil Model. Commonly,such models will be used in STARS for thermal applications. Because of this thermal propertiesmay play a larger role than observed in Black-Oil fluid models (such as Exercise 3). This fluidmodel will be created by incorporating similar techniques implemented in Exercise 3, includingmatching laboratory data, as well as some new concepts, such as Plus Fraction Splitting.

Setup of WinProp model with Plus Fraction Splitting

1. Open WinProp through CMG launcher.

2. In the Titles/EOS/Units form insert a title: Fluid Model for STARS and select PR(1978), kPa & deg C, and feed as moles.

3. In the Component Selection/Properties add the library component C1. Open theComposition form and add the composition for C1 as given in the file Heavy Oil forSTARS-Data1.xls. (The mole fraction of C1 is 0.08223).

4. The laboratory has supplied a C6+ component which now needs to be split intopseudocomponents.

In order to split the C6+ fractions, insert a Plus fraction Splittingform in the WinPropinterface after the Compositionform. The first single carbon number in plus fractionshould be 6. Specify the number of Pseudo-components to 4 and select Gamma,

Gaussian Quadrature, andLee-Kesler(Figure 57).

Figure 57: Plus Fraction Splitting for Heavy Oil


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5. In the Sample 1 tab, input SG+ as 0.989and the global mole fractions and molecularweights for liquid component as given in the file Heavy Oil for STARS-Data.xls(Figure 58).

Figure 58: Plus fraction splitting for Heavy Oil

6. Add a Saturation Pressureform (Figure 59). Savethe dataset as S1-char.dat and Runit. After running the data set, Update component properties and Save the data set asS2-regression psat.dat.

You will now notice that 4 hypothetical pseudo components have been added in thecomponents form.


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Figure 59: Saturation Pressure Calculation added per Step 6

Matching of WinProp Model to Laboratory Results

Due to splitting the component into 4 pseudocomponents a regression/tuning must beperformed to match the WinProp model to the experimental data.

1. The first experimental value to match is the Saturation Pressure. Delete Plus FactionSplitting,and thenadd Regression Parametersbelow Composition.

Then select Saturation PressureandDelete/Cutand clickRegression ParametersandPaste into Reg-Block.

On the Regression Parameters form, select Pc and Tc for the heaviestpseudocomponent. In the Interactions Coefficients tab select the hydrocarboninteraction coefficient exponent.

Runthe dataset. After running the dataset, Update component propertiesand Savethedata set as S3-lumping.dat.

2. Delete Regression Parameters, than add a Component Lumping form and lump thelast three heavy components by highlighting all three then selecting the bottom-mostcomponent. The Component Lumpingform should look like Figure 60.

3.


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Figure 60: Component Lumping form for Heavy Oil

4. Runthe dataset. After running the dataset, Update component propertiesand Savethedata set as S4-regression.dat.

5. Delete Component Lumpingand add Regression Parameters. Then select SaturationPressureandDelete/Cutand clickRegression ParametersandPaste into Reg-Block.

SelectRegression Parameters

andAdd into Reg-Block -> Lab -> Separator

. Entersaturation pressure, reservoir temperature, GORand APIdata from Heavy Oil forSTARS-Data1.xls (Figures 61-63).


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Figure 61: Saturation Pressure Form Populated with Excel Values

Figure 62: Separator Form Populated with values from Excel File


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Figure 63: Separator Form Experimental Tab Populated with Excel Values

6. In Regression Parameters under theComponent Properties tab select Pcand Tc forthe Heaviest component, and Vol. shift for the 2 Heaviest components. Run thedataset. Check for match in regression summary. After running the dataset, Updatecomponent propertiesand Savethe data set as S5-regression_visc.dat.

7.

Figure 64: Regression Parameters Set per Step 11


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Matching of WinProp Model Viscosity to Laboratory Viscosity

We will repeat the regression to match Viscosityat 10 deg C(Figures 65 and 66) and 100deg C(Figures 67 and 68) as given in Heavy Oil for STARS-Data.xls.

1.

Insert 2 Two Phase Flashforms to input experimental viscosity data (Figures 65 and 66)

Figure 65: Two-Phase Flash Calculations for viscosity data of Heavy Oil (10 deg)


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Figure 66: Two-Phase Flash Experimental Data viscosity of Heavy Oil (10 deg)


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Figure 67: Two-Phase Flash Calculations viscosity data of Heavy Oil (100 deg)


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Figure 68: Two-Phase Flash Experimental Data viscosity of Heavy Oil (100 deg)

2. In Component Selection/Propertieson theViscosity tab, set viscosity model type toPedersen Corresponding State Model and the corresponding states model toModified Pedersen (1987), (Figure 69).

In Regression Parameters, Viscosity Parameters tab,select all check boxes. Runthedataset. After running the dataset, check for a match.

You may have to change variable bounds to improve the match.

When an acceptable match has been found Update component propertiesand Savethedata set as S6-STARS PVT.dat.


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Figure 69: Viscosity Component Definition Tab showing changes to Modified

Pedersen

Creating a STARS PVT Model from WinProp

1. Delete Regression Parametersthen insert 2CMG STARS PVT Dataforms from theSimulator PVTdrop down menu.

2. On the firstCMG STARS PVT Dataform, on the Calc. Typetab select Basic STARSPVT Data. Then on the Basic PVT tab enter the initial reservoir conditions (3200kPa and 12 C) as the reference conditions.

Generate a Component liquid viscosity tablefrom 10 Cto 360 Cwith 8 stepsand usethe WinProp viscosity model (Figure 70). Set lower pressure at 500 kPa, upperpressureat 5500 kPa and number of stepsas 10.


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Figure 70: STARS PVT Data Generator with Initial Reservoir Conditions

3. On the second CMG STARS PVT Data form, on the Calc. Type tab select Gas-Liquid K-value Tables. On the K-Value tab enter 500 kPafor both the PressureandPressure Stepand 9for the No. of pressure steps. Also enter 10 Cfor Temperature, 50Cfor Temperature Step, and 8for No. of temperature steps.

Entering a minimum K-value threshold of 1.0E-06 will improve STARS numericalstability without materially affecting the simulation results (Figure 71). This option setsany K-Value less than this threshold to 0.


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Figure 71: STARS PVT Data Generator K-Value Data Entries

4. Savethe dataset under a new name and Runit. The information obtained is now capableof being imported to a STARS dataset and Ran.

2011 winprop tutorial

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