1、 異丙苯制備及產(chǎn)物雜質(zhì)分離DesignandOptimizationontheIsopropylBenzeneTechnologyProcess一級(jí)學(xué)科：化學(xué)工程與技術(shù)學(xué)科專業(yè)：化學(xué)工程與工藝學(xué)生：徐爽學(xué)號(hào)：2011011052指導(dǎo)教授：王水北京化工大學(xué)化學(xué)工程學(xué)院二零一五年一月十二日目錄目錄一、設(shè)計(jì)任務(wù)與要求21、設(shè)計(jì)任務(wù)錯(cuò)誤！未定義書(shū)簽。二流程設(shè)計(jì)三、完成輸入設(shè)定4TOC o 1-5 h z HYPERLINK l bookmark12 o Current Document SETUP設(shè)置4 HYPERLINK l bookmark38 o Current Document 輸入組分4 H

2、YPERLINK l bookmark44 o Current Document 3.3物性方法選擇4 HYPERLINK l bookmark50 o Current Document 3.4Streams的輸入5 HYPERLINK l bookmark58 o Current Document 3.5主要Block的輸入5 HYPERLINK l bookmark60 o Current Document 3.5.1反應(yīng)器模塊輸入5換熱器模塊輸入7 HYPERLINK l bookmark90 o Current Document 閃蒸罐模塊輸入8 HYPERLINK l bookmar

3、k98 o Current Document 3.5.4壓縮機(jī)模塊輸入8 HYPERLINK l bookmark102 o Current Document 3.5.5精餾塔模塊輸入8 HYPERLINK l bookmark128 o Current Document 四模擬運(yùn)行結(jié)果10 HYPERLINK l bookmark170 o Current Document 五靈敏性分析14 HYPERLINK l bookmark182 o Current Document 六確定工藝參數(shù)16 HYPERLINK l bookmark184 o Current Document 七心得體會(huì)

4、16一、設(shè)計(jì)任務(wù)與要求1.異丙苯制備給定條件學(xué)號(hào)1234567890分子甲烷丙烯丙烷止丁烷正戊烷甲苯乙醇異丙苯正戊烷苯（1）進(jìn)口物料：壓力1.1atm，溫度120C流量：苯和丙烯各60kmol/s，其他組分分別為10kmol/s（2）反應(yīng)器：丙烯轉(zhuǎn)化率0.9，壓力降、熱負(fù)荷為：0（3）換熱器：壓力降-0.1atm（4）精餾塔：要求壓力為1atm（全塔），塔釜苯摩爾含量為0.0012、物性數(shù)據(jù)我的學(xué)號(hào)為2011011052，對(duì)應(yīng)以下物質(zhì)：甲烷CH4,沸點(diǎn)-161.5C丙烯C3H6，沸點(diǎn)-47.7C正戊烷C5H12,沸點(diǎn)36.1C苯C6H6，沸點(diǎn)80.1C異丙苯C9H12，152.4C二流程設(shè)計(jì)根

5、據(jù)合成及分離要求設(shè)計(jì)流程如下圖1所示：|S-OVER|圖1異丙苯制備及產(chǎn)物雜質(zhì)分離流程圖整個(gè)流程主要有六種化工設(shè)備組成：反應(yīng)器（REACTOR）、換熱器（HEATER）、閃蒸罐（SEP）、壓縮機(jī)（COMPR）、混合器（MIXER）及精餾塔（DSTWU）。原料（FEED）以及循環(huán)回來(lái)的苯進(jìn)入反應(yīng)器進(jìn)行反應(yīng)，丙烯和苯反應(yīng)生成異丙苯，連同未反應(yīng)的物質(zhì)一同進(jìn)入換熱器中進(jìn)行冷凝；從閃蒸罐出來(lái)的重組分正戊烷、苯、異丙苯液相經(jīng)泵加壓后進(jìn)入T1精餾塔中進(jìn)行分離，塔頂輕組分為正戊烷，塔底重組分為苯和異丙苯；T1塔底重組分進(jìn)入T2精餾塔分離，塔頂為苯，它將與T3塔的丙烯一起循環(huán)至進(jìn)料段，作為原料作為產(chǎn)品；經(jīng)過(guò)冷凝

6、器降溫后的混合物進(jìn)入閃蒸罐進(jìn)行閃蒸，閃蒸后的氣相經(jīng)過(guò)壓縮升溫加壓進(jìn)入T3精餾塔實(shí)現(xiàn)甲烷和丙烯的分離。三、完成輸入設(shè)定3.1SETUP設(shè)置SetupSpecificationsSimulationOptionsStreamClassSubstEsirnHCostingOptionstearnPriceUnits-SetsCustomUnitsReportOptionsPopertiesFlowsheettearnsBlocks/Global/Description.Accounting|DiagnosticsTitle:|:-:ushuang1991UnikofmeasurementMETTME

7、T匚時(shí)TInputdata:Outputresults:Globalsettings圖2SETUP設(shè)置圖3.2輸入組分進(jìn)入如圖所示界面，輸入各組分如下：Specifications叵占|AII-|LI蠱彎N*空夕K_|二衛(wèi)8-_J2G日0-:-E-S-SimulationOptionsStreamClassSubst閃msCostingOptionsStreamPriceUnits-SetsCustomUnitsReportOptionsSpecificationsAssay/BlendLight-EndPropertiesPetroCharacterizationPseudocomponen

8、tsEnterpriseDatabaseComponentIDTypeComponentnameAliasCH4CunventionalMETHANECH4C3H6-2CunventionalPROFYLENEC3H6-2C5H12-1CunventionalN-PENTANEC5H12-1C6H6CunventionalBENZENEC6H6C9H12-2CunventionalISOPROFYLBENZC9H12-2來(lái)/SelectionPetroleum|Noncon”巳門(mén)tio門(mén)日IDefinecomponents圖3組分輸入3.3物性方法選擇進(jìn)入Properties輸入界面，選擇合適

9、的物性方法，本次模擬選用選用RK-S0AVE物性方法,如圖：甲()甲(5(5()也OUNIFACGroupsComp-GroupsMComp-ListsrPolymersAttr-SealingProperties&SpecificationsMPropertyMethodsEstimation書(shū)IMolecularStructureMParameters1DataAnalysisMProp-SetsrAdvaned二|CAPE-OPENPackagesFlowsheet/GlobalFlowsh已已tSection$FleferencedPropertymethods&modelsProce

10、sstype:Basemethod:Henrycomponents:PetroleumcalculationoptionsFree-watermethod:Watersolubility:ElectrolytecalculationoptionsChemistryID:Usetruecomponents3Propertymethod:EOS:Dataset:Liquidgamma:Dataset:Liquidenthalpy:Liquidvolume:廠Heatofmixing廠Pointingcorrection廠Useliq.reference-stateenthalpyCUMMUNTRK

11、-S0AVESTEAM-TA3T|f；K.-S0AVE31*dHLMX107VLMX20ESRKSTD|圖4物性方法選擇3.4Streams的輸入在物性方法確定之后，在Streams輸入界面按照設(shè)計(jì)要求輸入進(jìn)口物料的溫度、壓力及各組分流率。注意各個(gè)參數(shù)的單位。如圖5所示：包S創(chuàng)B包nn包nnParametersDataAnalysisProp-SetsAdvan匸edCAPE-OPENPackagesFlowsheetSectionStreams倒他倒他心C-OUTIFEED母InputB3Results(JEOVariables應(yīng)CustomStreamHl-OUTH2-OUTMl-OUTP

12、Rnni.ICTResi/SpecificationsFlashOptions|FSD|CurripunentAttr.EOOptions|Costing|Substreamridme:|yMIXEDrStatevariablesSolvent:FiefTemperatureI-Ccimposition-|Mole-FlowC9H12-2New.IReactionsoccurinseriesC3H6+C6H6=C9H12。轉(zhuǎn)化率為0.9，關(guān)鍵組分為C3H6。界面如圖所示：ReactionNo.:ComponentCoefficientC3H6-2-1C6H61米R(shí)eactantsCompone

13、ntCoefficientC9H12-21來(lái)ProductsProductsgenerationIbmol/hr0.9ofcompon已ntC3H6-2CMolarextent:(*Fractionalconversion:曰HlTemperatureT10cFY已ssureT-0.1atmSpecificationsFlashOptions|UtilityFlashspecificationsValidphasesIVapor-Liquid=astionnuzitex.圖7反應(yīng)方程式輸入3.5.2換熱器模塊輸入設(shè)定換熱器Hl的壓力降及出口溫度，出口溫度暫設(shè)定為10C,壓力降0.1atm。如圖

14、8所示:茁川固國(guó)|I*|Aii|險(xiǎn)聲舊貯夕況直Streams申図Blocks申COMPRInputIHcurvesDynamicBlockOptionsResultsEOVariablesEOInputSpecGroupsPortsStreamResults圖8換熱器H1模塊輸入設(shè)定換熱器H2的壓力降及出口溫度，出口溫度暫設(shè)定為60C,壓力降0.1atm。如圖9所示:ComponentsPropertiesFlowsheetStreamsBlocks劃COMPR崗HlInputHcurvesDynamicBlockOptionsH2J/炒SpecificationsFlashUptions|U

15、tilityTemperatureT60CTPressure0.1atmFlashspecificationsValidphasesJVapor-LiquidHl圖9換熱器H2模塊輸入3.5.3閃烝罐模塊輸入根據(jù)分離要求，設(shè)定閃烝罐壓力為0.5atm,熱負(fù)何為0。如圖10所示:3-包H23-M1XER1j-包M1XER2j-包REACTOR(j-包SEPP已ssure0.5atmTHeatduty0Gcal/hrTFlashspecificationsValidphasesJVapor-Liquid/SpecificationsFlashOptions|Entrainment|Utilityj

16、InputHcurvesDynamicBlockOptionsResultsEOVariablesEOInput圖10閃蒸罐模塊輸入3.5.4壓縮機(jī)模塊輸入如圖11jStreamsfjBlocks-型COMPRSetupPerformanceCurvesUserSubroutineDynamic炒BlockOptionsQResults(JEOVariablesEOInputSpecGroups口PortsQStreamResults|CustomStreamResiMndplSiijmmairv/SpecificationsCalculationOptions|PowerLossModela

17、ndtypeModel:C*CompressorCTurbin皂Tyw：|IsentropicusingGFS.AmethodCPressureratio:CPowerrequired:Convergence|Integral：ionParameters|Utility-OutletspecificationHDischargepressure:?Pressureincrease:1.6MPa1.6MFakW|CUseperformancecurvestodeterminedischargeconditionsIsentropic:|Polytropic:|Mechanical:圖11壓縮機(jī)模

18、塊輸入3.5.5精餾塔模塊輸入在精餾塔T1模塊中，確定全塔壓力為latm,回流比設(shè)定為1.4，并根據(jù)任務(wù)確定塔頂輕組分正戊烷和重組分苯的摩爾分率分別為0.98和0.001。如圖12所示:笛3d出十bJilLN3，：-沁* QInputAllBlocks+(5(5(5(5(5COMPRHlH2MIXER1M1XER2REACTORColumnspecificationsNumberofstages:憶Refluxratio:SET1嫁azr”璽聲2出夕x圖14精餾塔T3模塊輸入四模擬運(yùn)行在所有輸入完成之后，將程序進(jìn)行運(yùn)行，運(yùn)行過(guò)程沒(méi)有錯(cuò)誤和警告，表示程序運(yùn)行成功。程序運(yùn)行結(jié)果及各模塊運(yùn)行結(jié)果如下

19、圖所示：創(chuàng)|H2-0LITB|Ml-OUT|Sl|PFIODUCTB|f：-olit創(chuàng)FcleJ|S-OUTB|S-OVEFl二|ti-outF|T1-OVERM|T2-0VER二|T3-0LITBR3-CH436000.00037097.498514.26337097.49837097.4981097.498514.26336583.235TRACE514.2631097.497354H&2215999.99823204.9907139.512232049.897TRACE23204.99016049.8997139.51216065.477TRACE7139.512TRACE16049.4

20、121EC5H12-136000.00041523.57636734.96441523.5760.03541523.5765523.57636734.9644788.612734.69936000.265734.6654788.612C6H6215999.998142849.154140338.734351694.0627009.920142849.154135694.063140338.7342510.420140198.395140.339133188.4762510.420C9H12-2209184.311209053.975339.403208844.921209184.311339.

21、403209053.975130.336209053.975209.054130.336MoleFracCH40.0710.0820.0010.0560.0820.0070.0010.609TRACE0.0120.0451C3H6-20.4290.0510.0180.350TRACE0.0510.1010.0180.267TRACE0.163TRACE0.65345C5H12-10.0710.0910.0930.063160PPB0.0910.0350.0930.0800.0020.8220.0050.195C6H60.4290.3150.3560.5310.0320.3150.8550.35

22、60.0420.4010.0030.9930.102C9H12-20.4610.531512PPM0.9680.4610.0020.5310.0020.5970.0020.005圖15主要物流摩爾分率REACTORI1Results7NX匿豪包M1XER1“4包M1XER2白僉REACTORResultsEOVariablesStreamResultsCustomStreamResiModelSummaryResultsEOVariablesStreamResultsCustomStreamResi匚ModelSummairvsassa莊sassE曰ults自EI3-丸T3-OUT卜創(chuàng)T3-O

23、VERJBlocks3-型COMPR曲aQMaHlMaMs.rB.-.-.-何-.-.-ResultsEOVariabl巳玉Stir巳自mResultsCustomStreamResiModelSummaryResultsEOVariabl昭StreamResultsCustomStreamResiSummaryBdlancePhaseEquilibriumReactionsI已lectivityIUtilityUsaq已FlStoicresultsOutlettemperature:Outletpressure:Heal：duty:Netheatduty:Vaporfraction:1stl

24、iquid/Totalliquid:354.133614J1.01325|barJ0|Gcal/hrJ0|Gcal/hrJ圖16反應(yīng)器模塊結(jié)果如*Results-N*SummaryBalancePhaseEquilibrium|UtilityUsageBlockresultssummaryOutlettemperature:Outletpressure:Vaporfraction:Heatduty:Netduty:1stliquid/Totalliquid:Fressure-dropcorrelationpdrameter:圖17換熱器H1模塊結(jié)果10C0.911925bar0.1159296

25、-9824.3564Gcal/hrT-9824.3564Gcal/hr10.000261037型節(jié)肝出7X矇EE1H1s(1qq1h2s1sq1mxmixModelSummaryResultsEOVariablesStreamResultsCustomStreamResiModelSummiaryResultsEOVariablesStreamResultsCustomStreamResiModelSummarySummaryBalancePhaseEquilibriumIJhlityUsage60匚T0.4053barT0.120100651177.86001Gcal/hrT1177.860

26、01Gcal/hrT10.00192349BlockresultssummaryOutlettemperature:Outletpressure:Vaporfraction:Heatduty:Netduty:1stliquid/Totalliquid:Fressure-dropcorrelationparamete匚茁SEP圖18換熱器H2模塊結(jié)果7n*r；x匿EOVariables|StreamResults|CustomStreamResi0ModelSummaryMIXER1REACTORq1qq3sepResultsEOVariablesStreamResultsCustomStrea

27、mResiModelSummaryResultsSummaryE：alancEPhaseEquilibriumIUtilityLI：汨9已BlockresultssummaryOutletternperature:Outletpressure:Vaporfraction:Heatduty:Netduty:1stliquid/Totalliquid:7.5710305CT0.506625bar0.132371530Gcal/hrT0Gcal/hr1圖19閃蒸罐模塊結(jié)果|Results-Dim超審出/XI|CustomStearnResi(JModelSummiairyMIXER1iiq1qq1s

28、eResultsEOVariablesStearnResultsCustomStreamResiModelSummarySummaryE：alanc已|PhaseEquilibriumUtilitvUsageBlockresultssummaryOutlettemperature:Outletpressure:Vaporfraction:Heatduty:Netduty:1stliquid/Totalliquid:7.5710305CT0.506625barT0.132371530Gcal/hrT0Gcal/hrT1S1SQ1ResultsEOVariablestearnResultsCust

29、omStreamResiModelSummary圖20SEP模塊結(jié)果匚jResults(愆聲N*空夕X醫(yī)MaSEQa口QaTlQa口QaT2QpCustomStreamResi*ModelSummaryResultsEOVariablesStreamResultsCustomStreamResiModelSummaryResultsEOVariablesStreamResultsCustomStreamResiModelSummaryResultsFnVsrishlRSummaryBalance|RefluxRatioProfileMinimumrefluxratio:2.35847232Ac

30、tualrefluxratio:3Minimumnumberofstages:9.10677S17Numberofactualstages:17.2633721Feedstage:12.0051S88Numberofactualstagesabovefeed:11.0051S88F；eboilerh已a(bǔ)tirigrequired:1240.80948Gcal/hrCondensercooling已quiEi士607.709072Gcal/hrDistillatetemperature:31.4097019cBottomtemperature:106.616923cDistillatetofee

31、dfraction:0.11121494HETF1:Results圖21精餾塔T1模塊結(jié)果自dr刁e*O型轉(zhuǎn)N*QaQMaT2QlQQlT3QlQQl曰：R-ResultsEOVariablesStreamResultsCustomStreamR.esiModelSummaryResultsEOVariablesStreamResultsCustomStreamR.esiModelSummaryResultsEOVariablesStreamResultsCustomStreamResiModelSummarySummaryBalanceFlefluxRatioProfileMinimumre

32、fluxratio:0.37025889Actualrefluxratio:1.55Minimumnumlj已rofstages:3.90114969Numberofactualstages:5.31151935Feedstage:4.01063399Numberofactualstagesabovefeed:3.01063399Fleboilerh已a(bǔ)tingrequired:3105.43967Gcal/hrCondensercoolingrequired:1728.78676Gcal/hrDistillatetemperature:80.9023079cBottomtemperature

33、:146.985709cDistillatetofeedfraction:0.383249HETRResults圖22精餾塔T2模塊結(jié)果9Results勺衛(wèi)|Results-I更聲肝出夕X肉.“図：一.：“.“.“.：“國(guó)：“.：Results*EOVariablesStreamResultsCustomStreamResiModelSummaryResultsEOVariablesStreamResultsCustomStreamResiModelSummaryResultsEOVariablesStreamResultsCustomStrearnResiRJi11Cimnrj五靈敏性分析SummaryBalanc已|Fleflu:-:FldtioProfileMinimumrefluxratio:1.41067012Actualrefluxratio:3Minimumnumberofstages:1.65863008Numberofactualstage