Download - Oil Stab Op Tim Ization
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 1
OilStabilizationOptimization
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 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:[email protected] 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:[email protected] 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:[email protected] 5
Tostarttheprogram,FromStartMenu,SelectAllPrograms>>AspenTech>>ProcessModelingV8>>>>AspenHYSYS>>AspenHYSYS
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 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:[email protected] 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:[email protected] 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:[email protected] 9
From the palette:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 10
Addaheaterwithadutyof4.25*105kJ/hrandpressuredropof0.0
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 11
Addthefirstseparator
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 12
Theliquidstreamisthenheated,addasecondheaterwithapressuredropof0.0&dutyof3.15*105
Addavalvewithoutletpressureof2050kPa
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 13
Addthesecondseparator
Theliquidfromthesecondseparatorisnowfedtoathirdheaterwithapressuredropof0.0&dutyof1.13*105
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 14
Addasecondvalvewithanoutletpressureof350kPa
Addthethirdseparator
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 15
Thevaporfromthesecondseparatorisfedtoacompressortoraisethepressureto4125kPa
Addacompressorfromthepalette
Thevaporfromthethirdseparatorisfedtoasecondcompressortoraisethe
pressureto4125kPa
Addasecondcompressorwithanoutletpressureof4125kPa
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 16
Thethreevaporstreamswillbemixedusingamixer
TheRVPoftheLiquidProductstreamshouldbeabout96.5kPatosatisfythe
pipelinecriterion.
UsecoldpropertiesanalysistoseethecurrentReidVaporPressurefortheliquidproductfromthethirdseparator:
Fromtheattachmentstab,selectAnalysisandthenCreate:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 17
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 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:[email protected] 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:[email protected] 20
Thevariablestobeoptimizedinordertomaximizetheprofitshouldbeaddednow,thesevariablesare:
The3HeatersdutiesandValvesoutletpressures
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 21
Afteraddingallthe5variables,settheupperandlowerrangesforeachvariableasfollows:
TheOptimizerhasitsownSpreadsheetfordefiningtheObjectiveandConstraintfunctions.
Nowwehavetostartbuildingtheprofitmoduleusingthespreadsheetoperation:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 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:[email protected] 23
TheRVPspecfortheliquidshouldbeaddedinthespreadsheetinordertouseitasaconstraint.RVPspec=96.5kPaFirstweneedtoincreasethenumberofrowsinthespreadsheettobe20fromtheparameterstab:
Nowreturntothespreadsheettabagainandaddalltheprofitequationparameters&variables.
Afteraddingthelabels,importthevariablesineachlabeledcell:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 24
Addalldutiesforheaters&compressorsthesamewayaswedidinthepreviousstep.
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 25
DothesameforOil&gasproductionflowrates
TheRVPcurrentvalueshouldbeimportedfromtheAnalysis:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 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:[email protected] 27
Aftercalculatingtheoperatingprofit@currentconditions,usethe
optimizertomaximizetheprofitbychangingthe5variableswhichweaddedbefore
OpentheoptimizerandgotoFunctionstab:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 28
YoumayneedtopresstheStartbutton2or3timestoensurereachingtheoptimumsolutionasfollows:
YoumayseethenewvaluesforthevariablesfromtheVariablestab:
Nowyoucanreturnbacktothespreadsheettoobservetheresults:
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 29
SaveYourCase!
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Optimization
By:Eng.AhmedDeyabFareshttp://www.adeyab.com Mobile:00201227549943Email:[email protected] 30
Exercise:
OnethingyoumaynoticewiththeOptimizedsolutionisthatthePressureof V3 has been decreased to 70 kPa (10 psia) which is less thanatmospheric.Thisisnotadesiredconditionfortheinletofacompressor.Theinletofthesecondcompressor,cannotbelessthan125kPa(19psia).Whatisthemaximumprofitifyouadheretothisguideline?