往届严格模拟大作业

一.分工情 二.问题描 三.直接分离序 四.间接分离序 五、直接、间接分离序列的比 七.问题讨论与记 八.Aspen报 直接序列操作单元报 直接序列流股报 间接序列操作单元报 间接序列流股报 一.分工情况直接序列设计：，王青直接序列流程模拟：间接序列设计：间接序列结果整合：，王青流股检验：后期排版：王青云，（45.4kml/hr（16.kmo/hr分离要求：要求三组分均以98%的分离分数分离。一、分离方案设计（C1：2：三.直接分离序列98%。此处设定丙烷摩尔回收率为98%；对于异丁烷，为了使保证二塔中流出的异丁烷的98991%；0%。ξ0塔顶流率010塔底流率ABABC12.52MPa。故塔一塔顶使用分凝器。设定进料条件：37.8℃，1.72MPa；丙烷45.4kmol/h，异丁烷136.1kmol/h，正丁烷50，2513bar46kmol/hr，摩尔回流比为5，塔板压降0.6KPa。0.980.01。可调设计变量：摩尔回流比1至20；4550kmol/hr。0 异丁烷，考虑到一塔中回收率为99%，为了使保证二塔中流出的异丁烷的分离分数达到要求98%，异丁烷回收率应达到99%；假定符合清晰分割，则二塔中丙烷的摩尔回收率为丙进料流率ξ1塔顶流率1塔底流率049℃时塔顶产品的泡点压力：80，258bar140kmol/hr，摩尔回流比5，塔板压降0.6KPa。0.990.02。可调设计变量：摩尔回流比1至20；135142kmol/hr。0 5.5bar。重复以上优化过程至收敛。塔板直接序B1-blocks-进料位Reboiler/BottomTemperture（公用工程品位HeatbottomsCondenser/TopHeat-DistillateRefluxReflux塔板B2-blocks-进料位Reboiler/BottomTemperture（公用工程品位HeatbottomsCondenser/TopHeat-DistillateRefluxRefluxMoleFlowMoleVAPOR44.492/45.4=98%，满足要求。同时，摩尔纯度0.967，也比较高；ISO133.3915/136.1=98%，满足要求。同时，摩尔纯度0.962，也比较高；NBUT222.0817/226.8=98%，满足要求。同时，摩尔纯度0.994，也比较高。压力压力0直接序列TOWER150

直接序列TOWER1 压力

直接序列TOWER2 直接序列TOWER2温度-塔板数关系00XXX四.间接分离序列9898%；对于异丁烷，为了使保证二塔中9899%；假100%。丙进料流率ξ1塔顶流率1塔底流率0Antoine丙ABC1设定进料条件：37.8℃，1.72MPa；丙烷45.4kmol/h，异丁烷136.1kmol/h，正丁烷为5，塔板压降0.6KPa。0.990.02。可调设计变量：摩尔回流比0.1至20；100200kmol/hr。6080，09998%，异丁烷塔底的回收率应达到99%；假定符合清晰分割，则二塔中正丙烷的摩尔回收率为0%。丙进料流率ξ0塔顶流率010塔底流率49℃时塔顶产品的泡点压力：计算49℃时塔二塔顶泡点压力，计算结果为1.59MPa，大于参考值1.48MPa；再计算露点压力，的结果1.516Mpa，故塔二塔顶使用分凝器。5，塔板压降0.6KPa。0.980.02。可调设计变量：摩尔回流比0.1至20；间接序列第二个塔NQ间接序列第二个塔NQ1934，至7.5bar。重复以上优化过程至收敛。塔板间歇序列B1-blocks-进料位Reboiler/BottomHeatbottomsCondenser/TopHeat-DistillateRefluxReflux塔板B2-blocks-进料位8Reboiler/BottomHeatbottomsCondenser/TopHeat-DistillateRefluxRefluxMoleFlowMole纯度0.971，也比较高；ISOBUTANE流股为异丁烷采出，摩尔回收率为133.39/136.1=98%，满足要求。同时，摩尔纯度0.961，也比较高；摩尔纯度0.994，也比较高。0000505 10XXX直接序间接序塔塔塔塔总塔板数求回流比操作费求求求流率进产进产丙分离效丙操作费：1007.07880.06，间接分离产品浓度：0.9670.9620.9939；间接分离丙烷0.9710.9610.994。经过比较，可知两种分离方案得到的异丁烷本来计划采用隔板塔分离该物系，同学经过长时间思索后并没有找到可行方案，压力。从10bar降低到7.5bar之后，为了避免产品温度过低，最终决定将操作压力定为七.Aspen报告BLOCK: MODEL: -FEED STAGE10OUTLETS- STAGEPROPERTYOPTION SOAVE-REDLICH-KWONGEQUATIONOF PLETEORINCONSISTENTKEYSPECS.APPROXIMATIONSAREUSED. TOTAL

***MASSANDENERGYBALANCE RELATIVEMOLE(KMOL/HR ENTHALPY(CAL/SEC - - ***CO2EQUIVALENTSUMMARYFEEDSTREAMSPRODUCTSTREAMSNETSTREAMSCO2EUTILITIESCO2ETOTALCO2E****INPUTDATA INPUT NUMBEROF ALGORITHM ABSORBER INITIALIZATION HYDRAULICPARAMETER INSIDELOOPCONVERGENCE DESIGNSPECIFICATIONMETHOD UMNO.OFOUTSIDELOOPITERATIONS UMNO.OFINSIDELOOP UMNUMBEROFFLASH FLASH OUTSIDELOOPCONVERGENCE MOLARVAPORDIST/TOTALMOLARREFLUXMOLARDISTILLATE 1PRES, ****RESULTS COMPONENTSPLIT OUTLET SUMMARYOFKEY TOPSTAGECBOTTOMSTAGECTOPSTAGELIQUIDBOTTOMSTAGELIQUIDTOPSTAGEVAPORBOILUPVAPORMOLARREFLUXMOLARBOILUPCONDENSERDUTY(W/O-REBOILER MANIPULATED MOLARREFLUXMOLARDISTILLATE DESIGN 1STREAMS: 2STREAMS: UMFINALRELATIVE DEWSTAGE=BUBBLESTAGE=COMPONENTMASSSTAGE=24ENERGYSTAGE= **NOTE**REPORTEDVALUESFORSTAGELIQUIDANDVAPORRATESARETHEFLOWSFROMTHESTAGEINCLUDINGANYSIDEPRODUCT.STAGEHEATC 1---2--3--4--5--66--7--8--9----------------------------------------FLOWRATE FEEDRATEPRODUCTRATE 123456789181819202122232425262728****MASSFLOWPROFILESFLOW FEEDPRODUCT 1.23456789280.2104E+05 123456789 123456789 123456789 123456789 1 2 3 4 56789*****COLUMNTARGETINGRESULTS***THERMALYSISSTAGECENTHALPYEXERGYCARNOT123456789BLOCK: MODEL: -LIQUID STAGE26OUTLETS- STAGEPROPERTYOPTION SOAVE-REDLICH-KWONGEQUATIONOFTOTAL

***MASSANDENERGYBALANCE RELATIVEMOLE(KMOL/HR ENTHALPY(CAL/SEC - - ***CO2EQUIVALENTSUMMARYFEEDSTREAMSPRODUCTSTREAMSNETSTREAMSCO2EUTILITIESCO2ETOTALCO2E****INPUTDATA INPUT NUMBEROF ALGORITHM ABSORBER INITIALIZATION HYDRAULICPARAMETER INSIDELOOPCONVERGENCE DESIGNSPECIFICATIONMETHOD UMNO.OFOUTSIDELOOPITERATIONS UMNO.OFINSIDELOOP UMNUMBEROFFLASH FLASH OUTSIDELOOPCONVERGENCE MOLARVAPORDIST/TOTALMOLARREFLUXMOLARDISTILLATE 1PRES, ****RESULTS COMPONENTSPLIT OUTLET SUMMARYOFKEY TOPSTAGECBOTTOMSTAGECTOPSTAGELIQUIDBOTTOMSTAGELIQUIDTOPSTAGEVAPORBOILUPVAPORMOLARREFLUXMOLARBOILUPCONDENSERDUTY(W/OREBOILER MANIPULATED MOLARREFLUXMOLARDISTILLATE DESIGN 1STREAMS: 2STREAMS: UMFINALRELATIVE DEWSTAGE=BUBBLESTAGE=COMPONENTMASSSTAGE=26ENERGYSTAGE= **NOTE**REPORTEDVALUESFORSTAGELIQUIDANDVAPORRATESARETHEFROMTHESTAGEINCLUDINGANYSIDE HEATDUTY1---2--3--------------FLOWRATEFEEDRATEPRODUCTRATE1 23****MASSFLOWPROFILESFLOW FEEDPRODUCT 10.9549E+0520.8748E+0530.8742E+05240.8411E+05250.8407E+05260.9827E+05270.9824E+05670.9761E+05680.1300E+05 123 123 123 123 123FEEDISOLIQUIDNBUTSTREAMFROM--- SUBSTREAM:COMPONENTS: COMPONENTS:MOLE2.5064-2.9566-COMPONENTS:3.8920- COMPONENTS:MASS1.9027-3.8561-5.0760-TOTALSTATEC-------------------7.7814-6.3482-2.8291-AVGSTREAM FROM --- SUBSTREAM:COMPONENTS: COMPONENTS:MOLECOMPONENTS:COMPONENTS:MASS 02 TOTALSTATEC-----AVG--STREAM FROM ---SUBSTREAM: COMPONENTS: COMPONENTS:MOLE COMPONENTS:COMPONENTS:MASSTOTALSTATEC-----AVGSTREAMFROM SUBSTREAM:COMPONENTS:COMPONENTS:MOLECOMPONENTS:COMPONENTS:TOTALSTATEC----AVGSTREAM FROM ---SUBSTREAM: COMPONENTS: 17 COMPONENTS:MOLEFRAC 19COMPONENTS:COMPONENTS:MASSTOTALSTATEC-----AVGSTREAM FROM ---SUBSTREAM: COMPONENTS: COMPONENTS:MOLE 02 03COMPONENTS:COMPONENTS:MASSTOTALSTATEC----AVGBLOCK: MODEL: -FEED STAGE27OUTLETS- NBUTANESTAGEPROPERTYOPTION SOAVE-REDLICH-KWONGEQUATIONOFTOTAL

***MASSANDENERGYBALANCE RELATIVEMOLE(KMOL/HR - - ***CO2EQUIVALENTSUMMARYFEEDSTREAMSPRODUCTSTREAMSNETSTREAMSCO2EUTILITIESCO2ETOTALCO2E****INPUTDATA INPUT NUMBEROF ALGORITHM ABSORBER INITIALIZATION HYDRAULICPARAMETER INSIDELOOPCONVERGENCE DESIGNSPECIFICATIONMETHOD UMNO.OFOUTSIDELOOPITERATIONS UMNO.OFINSIDELOOP UMNUMBEROFFLASH FLASH OUTSIDELOOPCONVERGENCE MOLARVAPORDIST/TOTALMOLARREFLUXMOLARDISTILLATE 123C12.4562-23.5776-38.5639-4.7658-45.5452-6.0405-54.0051-7.4319-63.2293-8.9669-72.8386-82.6389-92.5329-2.4721-2.4329-2.4038-2.3793-2.3568-2.3355-2.3148-2.2948-2.2756-2.2573-2.2401-2.2240-2.2093-2.1958-2.1836-2.1727-2.1629-2.1543-2.1467-2.1401-2.1344-2.1294-2.1251-2.1214-11.5267-22.4562-33.4661-44.5369-57.4282-5.6860-66.0392-6.9401-75.3409-8.3231-84.9909-9.8523-94.8138-4.7216-4.6706-4.6393-4.6173-4.5996-4.5838-4.5689-4.5545-4.5406-4.5272-4.5143-4.5022-4.4908-4.4803-4.4706-4.4618-4.4539-4.4468-4.4404-4.4348-4.4299-4.4256-4.4218-4.4185-****RESULTS COMPONENTSPLIT OUTLET SUMMARYOFKEY TOPSTAGECBOTTOMSTAGECTOPSTAGELIQUIDBOTTOMSTAGELIQUIDTOPSTAGEVAPORBOILUPVAPORMOLARREFLUXMOLARBOILUPCONDENSERDUTY(W/OREBOILER MANIPULATED MOLARDISTILLATEMOLARREFLUX DESIGN 1STREAMS: BASE-STREAMS:2STREAMS: BASE-STREAMS: UMFINALRELATIVE DEWSTAGE=BUBBLESTAGE=COMPONENTMASSSTAGE=27ENERGYSTAGE= **NOTE**REPORTEDVALUESFORSTAGELIQUIDANDVAPORRATESARETHEFLOWSFROMTHESTAGEINCLUDINGANYSIDEPRODUCT. HEATDUTY1---2------------------FLOWRATEFEEDRATEPRODUCTRATE1 2****MASSFLOWPROFILESFLOW FEEDPRODUCT 10.1139E+0620.1070E+06260.1072E+06270.1375E+06280.1379E+06290.1381E+06300.1382E+06310.1382E+06730.1371E+06740.1300E+05 C4H10-12 C4H10-12 C4H10-12 C4H10-12 C4H10-12*****HYDRAULICPARAMETERS***DEFINITIONSMARANGONIINDEX=SIGMA-SIGMATOFLOWPARAM=(ML/MV)*SQRT(RHOV/RHOL)QR=QV*SQRT(RHOV/(RHOL-RHOV))FFACTOR=QV*SQRT(RHOV)SIGMAISTHESURFACETENSIONOFLIQUIDFROMTHESTAGESIGMATOISTHESURFACETENSIONOFLIQUIDTOTHEMLISTHEMASSFLOWOFLIQUIDFROMTHESTAGEMVISTHEMASSFLOWOFVAPORTOTHESTAGERHOLISTHEMASSDENSITYOFLIQUIDFROMTHESTAGERHOVISTHEMASSDENSITYOFVAPORTOTHESTAGEQVISTHEVOLUMETRICFLOWRATEOFVAPORTOTHELIQUIDVAPOR12MASSLIQUIDFROMVAPORVOLUMELIQUIDFROMVAPORLIQUIDVAPOR10.11390E+060.23662E+0620.10696E+060.22314E+060.10717E+060.22360E+060.13746E+060.28677E+060.13793E+060.28797E+060.13814E+060.28854E+060.13821E+060.28875E+060.13821E+060.28877E+060.13710E+060.28687E+06 LIQUIDFROMVAPORTOFROMVAPORTOSURFACELIQUIDFROM12MARANGONIFLOWREDUCEDF-12BLOCK: MODEL: -MIX OUTLETS-PROPANE ISOBTUTASTAGEPROPERTYOPTION SOAVE-REDLICH-KWONGEQUATIONOFTOTAL

***MASSANDENERGYBALANCE RELATIVEMOLE(KMOL/HR - - ***CO2EQUIVALENTSUMMARYFEEDSTREAMSPRODUCTSTREAMSNETSTREAMSCO2EUTILITIESCO2ETOTALCO2E****INPUTDATA INPUT NUMBEROF ALGORITHM ABSORBER INITIALIZATION HYDRAULICPARAMETER INSIDELOOPCONVERGENCE DESIGNSPECIFICATIONMETHOD UMNO.OFOUTSIDELOOPITERATIONS UMNO.OFINSIDELOOP UMNUMBEROFFLASH FLASH OUTSIDELOOPCONVERGENCE MOLARVAPORDIST/TOTALMOLARREFLUXMOLARDISTILLATE 1PRES, ****RESULTS COMPONENTSPLIT OUTLET SUMMARYOFKEY TOPSTAGECBOTTOMSTAGECTOPSTAGELIQUIDBOTTOMSTAGELIQUIDTOPSTAGEVAPORBOILUPVAPORMOLARREFLUXMOLARBOILUPCONDENSERDUTY(W/OREBOILER MANIPULATED MOLARDISTILLATEMOLARREFLUX DESIGN NOSPEC- STREAMS:PROPANE STREAMS:ISOBTUTA BASE-STREAMS: UMFINALRELATIVE DEW 0.31042E-04STAGE=BUBBLE 0.39621E-04STAGE=COMPONENTMASSBALANCE 0.24206E-07STAGE=8COMP=C4H10-01ENERGYBALANCE 0.46343E-04STAGE=4 **NOTE**REPORTEDVALUESFORSTAGELIQUIDANDVAPORRATESARETHEFLOWSFROMTHESTAGEINCLUDINGANYSIDEPRODUCT. HEATDUTY1---2--3--6--7--8--9--------FLOWRATE FEEDRATEPRODUCTRATE 1236789****MASSFLOWPROFILESFLOW FEEDPRODUCT 1.20.1124E+0530.1133E+0560.1202E+0570.1223E+0580.2145E+0590.2159E+05200.2307E+05210.2311E+0522 C4H10-1236789 C4H10-1236789 C4H10-1236789 1 236789 C4H10-1236789*****HYDRAULICPARAMETERS***DEFINITIONSMARANGONIINDEX=SIGMA-SIGMATOFLOWPARAM=(ML/MV)*SQRT(RHOV/RHOL)QR=QV*SQRT(RHOV/(RHOL-RHOV))FFACTOR=QV*SQRT(RHOV)SIGMAISTHESURFACETENSIONOFLIQUIDFROMTHESTAGESIGMATOISTHESURFA