oil stab op tim ization
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 1
OilStabilizationOptimization
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 2
Workshop A poor-boy stabilization scheme is used to separate an oil and gas mixture into a stabilized oil and a saleable gas. A simple three-stage separation with heating between each stage is used and the object of the exercise is to select the let-down pressure and temperatures such that the products revenue less the utilities cost is maximized. A special tool in HYSYS, the Optimizer, will be used to find the optimum operating conditions. HYSYS includes additional modelling and decision support tools that can be used to enhance the usability of your models. In this module, you will use the HYSYS optimization tool available in HYSYS to investigate the debottlenecking and optimization of a crude column. Learning Objectives Once you have completed this section, you will be able to: Use the Optimizer tool in HYSYS to optimize flowsheets Use the Spreadsheet to perform calculations
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 3
OilStabilizationAfeedstream@10oC,4125kPawithaflowrateof1MMSCFDisfedtoaheater (duty=4.25*105kJ/hr)beforeentering the first separatorwheretheseparated liquid isheated inasecondheater(duty=3.15*105kJ/hr).Theoutlet from theheater is thensent toa letdownvalve inorder todecreasethepressureto2050kPabeforeenteringthesecondseparatorwheretheseparatedliquidisheatedthroughathirdheater(duty=1.13*105kJ/hr).Theoutletfromthethirdheateristhenthrottledthroughavalve(outletpressure=350kPa)andthenfedtoathirdseparatortoobtainthefinalliquidoilproduct.Each gas stream from the 2nd & 3rd separators is fed to a separatecompressor to raise thepressure to4125kPaand thenmixed (usingamixer)with thegas stream from the 1st separator toget the finalgasproductstream.Notes:
Pressuredropacrossallheatersandseparatorsare0.0.Calculate:
Thetotalliquidproduct=barrel/hr Thetotalgasproduct=m3_gas/hr
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 4
OilStabilizationOptimizationIn this case, we want to maximize the total operating profit whileachievinganRVPofLiquidProductlessthan96.5kPa.TheincomesfromthePlantareboththeGasandLiquidProducts.Theoperatingcostsarethe Steam Costs for each Heater plus the Power Cost for eachCompressor.Profit=IncomeCost Profit=(GasProduct+LiquidProduct)(SteamCosts+CompressionCost) Prices&costs:OilPrice=15$/bblGasPrice=0.106$/m3_gasSteamCost=0.682$/kWhCompressionCost=0.1$/kWhThevariablestobeadjusted:
Heaterduties(forthe3heaters).Userangeof01e6kJ/hr Valvesoutletpressures.
Userangeof6503500kPaforthefirstvalveUserangeof701000kPaforthesecondvalve
Calculate:
Theoptimumvaluesfortheadjustedvariables Themaximumprofit..$/hr
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 5
Tostarttheprogram,FromStartMenu,SelectAllPrograms>>AspenTech>>ProcessModelingV8>>>>AspenHYSYS>>AspenHYSYS
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 6
1- First, Start a new case
2- Add the Components
3- Choose the system components from the databank:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 7
Now, select the suitable fluid package
In this case, select Peng-Robinson
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 8
Now you can start drawing the flow sheet for the process by clicking the Simulation button:
Now add a material stream to define the feed stream composition and conditions
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 9
From the palette:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 10
Addaheaterwithadutyof4.25*105kJ/hrandpressuredropof0.0
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 11
Addthefirstseparator
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 12
Theliquidstreamisthenheated,addasecondheaterwithapressuredropof0.0&dutyof3.15*105
Addavalvewithoutletpressureof2050kPa
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 13
Addthesecondseparator
Theliquidfromthesecondseparatorisnowfedtoathirdheaterwithapressuredropof0.0&dutyof1.13*105
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 14
Addasecondvalvewithanoutletpressureof350kPa
Addthethirdseparator
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 15
Thevaporfromthesecondseparatorisfedtoacompressortoraisethepressureto4125kPa
Addacompressorfromthepalette
Thevaporfromthethirdseparatorisfedtoasecondcompressortoraisethe
pressureto4125kPa
Addasecondcompressorwithanoutletpressureof4125kPa
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 16
Thethreevaporstreamswillbemixedusingamixer
TheRVPoftheLiquidProductstreamshouldbeabout96.5kPatosatisfythe
pipelinecriterion.
UsecoldpropertiesanalysistoseethecurrentReidVaporPressurefortheliquidproductfromthethirdseparator:
Fromtheattachmentstab,selectAnalysisandthenCreate:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 17
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 18
ChangingtheUnitsWeneedtochangethedefaultunitsettofitthiscase
Changetheunitsasfollows:
Molarflow:m3_gas/hr
Liq.Vol.Flow:barrel/hr
Std.Vol.Flow:barrel/hr
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 19
OptimizationHYSYS contains amultivariableSteadyStateOptimizer.Once your flowsheethasbeen built and converged, you can use the Optimizer tool to find the operatingconditionswhichminimizeormaximizeanObjectiveFunction.TheOptimizerownsitsownSpreadsheet fordefiningtheObjectiveFunctionsaswellasanyconstraintexpressions to be used. This allows you to construct Objective Functions whichmaximizeprofit,minimizeutilitiesorminimizeexchangerUA.
Inthiscase,wewanttomaximizethetotaloperatingprofitwhileachievinganRVPofLiquidProductlessthan96.5kPa.TheincomesfromthePlantareboththeGasandLiquidProducts.TheoperatingcostsaretheSteamCostsforeachHeaterplusthePowerCostforeachCompressor.Profit=IncomeCost Profit=(GasProduct+LiquidProduct)(SteamCosts+CompressionCost)
UsetheOptimizertool:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 20
Thevariablestobeoptimizedinordertomaximizetheprofitshouldbeaddednow,thesevariablesare:
The3HeatersdutiesandValvesoutletpressures
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 21
Afteraddingallthe5variables,settheupperandlowerrangesforeachvariableasfollows:
TheOptimizerhasitsownSpreadsheetfordefiningtheObjectiveandConstraintfunctions.
Nowwehavetostartbuildingtheprofitmoduleusingthespreadsheetoperation:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 22
Profit=IncomeCostProfit=(GasProduct+LiquidProduct)(SteamCosts+CompressionCost) Prices&costs:OilPrice=15$/bblGasPrice=0.106$/m3_gasSteamCost=0.682$/kWhCompressionCost=0.1$/kWh
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 23
TheRVPspecfortheliquidshouldbeaddedinthespreadsheetinordertouseitasaconstraint.RVPspec=96.5kPaFirstweneedtoincreasethenumberofrowsinthespreadsheettobe20fromtheparameterstab:
Nowreturntothespreadsheettabagainandaddalltheprofitequationparameters&variables.
Afteraddingthelabels,importthevariablesineachlabeledcell:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 24
Addalldutiesforheaters&compressorsthesamewayaswedidinthepreviousstep.
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 25
DothesameforOil&gasproductionflowrates
TheRVPcurrentvalueshouldbeimportedfromtheAnalysis:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 26
ThePricesshouldnowaddedmanuallywithoutimportingit
CalculatetheIncome,Cost&Profitusingthecurrentformulas:
Income:=d7*b7+d8*b8
Cost:=(b1+b2+b3)*d1+(b4+b5)*d4
Profit:=d12d13
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 27
Aftercalculatingtheoperatingprofit@currentconditions,usethe
optimizertomaximizetheprofitbychangingthe5variableswhichweaddedbefore
OpentheoptimizerandgotoFunctionstab:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 28
YoumayneedtopresstheStartbutton2or3timestoensurereachingtheoptimumsolutionasfollows:
YoumayseethenewvaluesforthevariablesfromtheVariablestab:
Nowyoucanreturnbacktothespreadsheettoobservetheresults:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 29
SaveYourCase!
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:eng.a.deab@gmail.com 30
Exercise:
OnethingyoumaynoticewiththeOptimizedsolutionisthatthePressureof V3 has been decreased to 70 kPa (10 psia) which is less thanatmospheric.Thisisnotadesiredconditionfortheinletofacompressor.Theinletofthesecondcompressor,cannotbelessthan125kPa(19psia).Whatisthemaximumprofitifyouadheretothisguideline?
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