Aspen精馏塔
Aspen简捷法精馏塔设计计算
例5-2 简捷法精馏设计计算
5）DSTWU模型设置
这里轻关键组分为NC4， 重关键组分为I-C5。
对于轻关键组分NC4
Recov=29.7248/30=0.9908
重关键组分为I-C5 Recov=0.2247/20=0.01124
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例5-2 简捷法精馏设计计算
5） DSTWU模型设置
回流比的输入可随便输入一个值，该值如果小于Rmin,则系统安装 2Rmin作为回流比进行计算；如大于Rmin，就按照实际的值进行计 算。
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5 塔Columns模块---简捷蒸馏模块
Distl（简捷法精馏核算）
Distl模型可以模拟一个带有一股进料和两种 产品的多级多组分的蒸馏塔，塔可带有分凝 器或全凝器。模型假定恒摩尔流和恒相对挥 发度。用Edimister法进行产品组成。
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5 塔Columns模块---简捷蒸馏模块
Distl（简捷法精馏核算）
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5 塔Columns模块
进行简捷蒸馏的模型有DSTWU, Distl和
SCFrac
进行严格的多级分离的模块有RadFrac,
MultiFrac, PetroFrac, RateFrac
用于液-液萃取塔的严格模型有Extract
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5 塔Columns模块---简捷蒸馏模块 DSTWU(简捷法精馏设计) Distl（简捷法精馏核算）
第5页
5 塔Columns模块---简捷蒸馏模块
DSTWU(简捷法精馏设计)
采用Winn法估算最小级数，Underwood法估算 最小回流比，Gilliland法规定级数所必需的回 流比或规定回流比所必需的级数。
可确定最小回流比、最小级数或实际回流比、 实际级数。模型也估算最适宜的进料位置、冷 凝器和再沸器负荷。可生成回流比对于级数的 表和曲线。
aspen plus 讲义 精馏解析
馏
1、精馏原理 2、精馏塔 3、精馏过程的节能
塔
进行气相和液相或液相和液相间物质 传递的设备。按结构分板式塔和填料塔 两大类。板式塔内设有一定数量的塔板， 气体以鼓泡或喷射形式与塔板上液层相 接触进行物质传递。填料塔内装有一定 高度的填料，液体沿填料自上向下流动， 气体由下向上同液膜逆流接触，进行物 质传递。常应用于蒸馏、吸水、萃取等 操作中。
2、精馏塔
穿流式塔板：塔板间没有降液管，气、液 两相同时由塔板上的板上液层高度靠气体 速度维持。这种塔板结构简单，生产能力 较大，但板效率及操作弹性不及溢流塔板。
液相
穿流式塔板常见的板型有筛孔式、栅板式、 波纹板式等。
气相
2、精馏塔
2.1.2.1
泡罩塔板
（ Bubble-cap Tray ）
泡罩塔板1813年在工业上开始应用， 其主要元件由升气管和泡罩构成，泡 罩安装在升气管顶部，泡罩底缘开有 若干齿缝，升气管顶部应高于泡罩齿 缝的上沿，以防止液体从中漏下。 液体横向通过塔板经溢流堰流入降液 管。气体则沿升气管上升折流经泡罩 齿缝分散进入液层，形成两相混合的 鼓泡区。由于有升气管，泡罩塔板即 使在低气速下操作也不致产生严重的 漏液。泡罩塔板操作稳定，弹性大， 缺点是结构复杂，造价高，塔板压降 大，生产强度低，近几十年逐渐被筛 孔塔板、浮阀塔板等所取代。
（Jet Co-flow Valve Tray）
JCV浮阀塔板：阀笼与塔板固定，阀片在阀笼内上下浮动。它的一部分为鼓泡、 另一部分为喷射湍动传质，使分离效率和生产能力大大提高。JCV浮阀塔板具 有结构简单、阀片开启灵活、高效、高通量、寿命长、耐堵塞的特点。
JCV浮阀 （改进型双流喷射浮阀）
普通型JCV浮阀
aspen共沸精馏塔
MM "11.1" FLAVOR "NO" VERSION "11.1" DATETIME "Tue Nov 29 08:46:25 2005" MACHINE "WIN-NT/VC" ;startlibraryversion1NumLibs = 1Built-InNumCats = 9Mixers/SplittersactiveSeparatorsactiveHeat ExchangersactiveColumnsactiveReactorsactivePressure ChangersactiveManipulatorsactiveSolidsactiveUser Modelsactiveendlibrary;8>VERSION 0YT-501RadFracBuilt-InRADFRAC>VERSION 0YD-501DecanterBuilt-InDECANTER>VERSION 0YT-511RadFracBuilt-InRADFRAC>VERSION 0YE-500HeaterBuilt-InHEATER>VERSION 0YE-513HeaterBuilt-InHEATER>VERSION 0M1FSplitBuilt-InFSPLIT>VERSION 0M2FSplitBuilt-InFSPLIT>VERSION 0M3FSplitBuilt-InFSPLIT? SETUP MAIN ? \ "RUN-CLASS" RUN-CLASS = FLOWSHEET \ \ SIMULATE INTERACTIVE= NO MOLEFLOW = MOLEFLOW MASSFLOW = MASSFLOW MOLEFRAC = MOLEFRAC MASSFRAC =MASSFRAC TFFFILE = "GAS_E" VISITED = 1 \ ? SETUP GLOBAL ? \ "IN-UNITS" INSET= METCBAR \ \ "STREAM-CLASS" SCLASS = CONVEN \ ? SETUP DIAGNOSTICS ? ? SETUP"SIM-OPTIONS" ? ; "METCBAR_MOLE" ; ? SETUP "UNITS-SET" METCBAR ? \ DESCRIPTION DESCRIPTION = "Metric Units with C, BAR, MMKCAL/HR, and CUM" \ \MMLOCAL \ \ UNITSET BASESET = MET ( 3 3 3 3 3 3 3 3 3 3 3 7 7 3 3 53 3 3 5 34 3 3 3 3 1 3 3 3 4 3 7 3 3 3 1 1 4 4 3 3 3 3 3 3 3 3 3 3 3 35 3 3 3 3 3 3 33 3 34 3 3 3 3 3 3 3 3 3 35 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 33 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 ) \ ? SETUP "UNITS-SET" METCKGCM ? \DESCRIPTION DESCRIPTION = "Metric Units with C, KG/SQCM, MMKCAL/HR,and CUM"\ \ MMLOCAL \ \ UNITSET BASESET = MET ( 3 3 3 3 3 3 3 3 3 3 3 7 7 3 3 5 3 3 38 3 4 3 3 3 3 1 3 3 3 4 3 7 3 3 3 3 3 4 4 3 3 3 3 3 3 3 3 3 3 3 3 5 3 3 3 3 33 3 3 3 34 3 3 3 3 3 3 3 3 3 3 8 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 33 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 3 ) \ ? SETUP "UNITS-SET" "SI-CBAR" ? \ DESCRIPTION DESCRIPTION = "International System Units with C, BAR, and /HR"\ \ MMLOCAL \ \ UNITSET BASESET = SI ( 1 1 1 1 1 1 1 1 1 3 3 7 1 1 1 1 1 1 15 1 4 1 1 1 1 1 1 1 1 4 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 4 5 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 ) \ ? SETUP "SYS-OPTIONS" ? ? SETUP"ACCOUNT-INFO" ? \ ACCOUNT USER-NAME = "LEE" \ ? SETUP "RUN-CONTROL" ? ? SETUP DESCRIPTION ? \ DESCRIP DESCRIP = ("General Simulation with Metric Units :""C, bar, kg/hr, kmol/hr, MMKcal/hr, cum/hr." " " "Property Method: None" " ""Flow basis for input: Mole" " " "Stream report composition: Mole flow" ) \ ?DATABANKS ? \ DATABANKS \ ? COMPONENTS MAIN ? \ COMPONENTS CID = H2O ANAME =H2O OUTNAME = H2O TYPE = CONV DBNAME1 = "WATER" ANAME1 = "H2O" / CID = NBAANAME = C6H12O2-1 OUTNAME = NBA TYPE = CONV DBNAME1 = "N-BUTYL-ACETATE" ANAME1 = "C6H12O2-1" / CID = HAC ANAME = C2H4O2-1 OUTNAME = HAC TYPE = CONVDBNAME1 = "ACETIC-ACID" ANAME1 = "C2H4O2-1" / CID = MA ANAME = C3H6O2-3 OUTNAME = MA TYPE = CONV DBNAME1 = "METHYL-ACETATE" ANAME1 = "C3H6O2-3" /CID = PX ANAME = C8H10-3 OUTNAME = PX TYPE = CONV DBNAME1 = "P-XYLENE" ANAME1= "C8H10-3" \ ? COMPONENTS "COMP-LIST" GLOBAL ? ? SOLVE ? ? FLOWSHEET GLOBAL? \ BLOCK BLKID = "YT-501" BLKTYPE = RADFRAC IN = ( 45A M0-1 45B M0-1 142M0-1 143 M0-1 139 M0-1 ) OUT = ( 120 M0-1 121 M2-3 ) \ \ BLOCK BLKID = "YE-513"BLKTYPE = HEATER IN = ( 126 M0-1 ) OUT = ( 140 M0-1 ) \ \ BLOCK BLKID="YE-500" BLKTYPE = HEATER IN = ( 120 M0-1 ) OUT = ( 138 M0-1 ) \ \ BLOCK BLKID = "YT-511" BLKTYPE = RADFRAC IN = ( 140 M0-1 ) OUT = ( 145 M2-3 130M3-4 131 M1-2 ) \ \ BLOCK BLKID = "YD-501" BLKTYPE = DECANTER IN = ( 138 M0-1130 M0-1 129 M0-1 ) OUT = ( "126+139" M1-2 "142+143" M0-1 ) \ \ BLOCK BLKID= M1 BLKTYPE = FSPLIT IN = ( 45 M0-1 ) OUT = ( 45A M0-1 45B M0-1 ) \ \ BLOCKBLKID = M2 BLKTYPE = FSPLIT IN = ( "142+143" M0-1 ) OUT = ( 142 M0-1 143 M0-1) \ \ BLOCK BLKID = M3 BLKTYPE = FSPLIT IN = ( "126+139" M0-1 ) OUT = ( 126M0-1 139 M0-1 ) \ \ "DEF-STREAM" SCLASS = CONVEN \ ? PROPERTIES MAIN ? \GPROPERTIES GBASEOPSET = "NRTL-HOC" GOPSETNAME = "NRTL-HOC" PARCON = -2 \ ?PROPERTIES COMPARE ? ? PROPERTIES "OPTION-SETS" NRTL ? \ PARAM BASE = NRTL \? PROPERTIES "OPTION-SETS" "NRTL-2" ? \ PARAM BASE = "NRTL-2" \ ? PROPERTIES"OPTION-SETS" "NRTL-HOC" ? \ PARAM BASE = "NRTL-HOC" \ ? PROPERTIES "MOLEC-STRUCT" H2O ? ? PROPERTIES "MOLEC-STRUCT" HAC ? ? PROPERTIES "MOLEC-STRUCT" MA ? ? PROPERTIES "MOLEC-STRUCT" NBA ? ? PROPERTIES "MOLEC-STRUCT" PX ? ? PROPERTIES REGPAR ? \ FRED REGCASE = "R-R-1" PARNAME ="NRTL" COMPI = "H2O" COMPJ = "HAC" VALUE = ( "0.E0" "0.E0" "-2.42273094E+02""4.74523263E+02" "3.00000000E-01" "0.E0" "0.E0" "0.E0" "0.E0" "0.E0" "0.E0""1.00000000E+03" ) \ ? PROPERTIES ESTIMATION ? ; "METCBAR_MOLE" ; \ DIRECTORALLONLY = NONE UNCHOICE = NO TCHOICE = NO GRPCHOICE = NO \ ? PROPERTIES PARAMETERS BINARY SCALAR "HOCETA-1" ? ; "METCBAR_MOLE" ; \ PROP-LIST PARAMNAME = HOCETA SETNO = 1 UNITROW = 0 BDBANK = ( "EOS-LIT" ) \ \ BPVALPARAMNAME2 = HOCETA CID1 = H2O CID2 = H2O VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = H2O CID2 = NBA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = H2O CID2 = HAC VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = H2O CID2 = MA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2= HOCETA CID1 = NBA CID2 = H2O VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETACID1 = NBA CID2 = NBA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 =NBA CID2 = HAC VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = NBA CID2= MA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = NBA CID2 = PXVALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = HAC CID2 = H2O VALUE =EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = HAC CID2 = NBA VALUE = EOS-LIT \\ BPVAL PARAMNAME2 = HOCETA CID1 = HAC CID2 = HAC VALUE = EOS-LIT \ \ BPVALPARAMNAME2 = HOCETA CID1 = HAC CID2 = MA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2= HOCETA CID1 = HAC CID2 = PX VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETACID1 = MA CID2 = H2O VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = MACID2 = NBA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = MA CID2 = HACVALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = MA CID2 = MA VALUE =EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = MA CID2 = PX VALUE = EOS-LIT \ \BPVAL PARAMNAME2 = HOCETA CID1 = PX CID2 = NBA VALUE = EOS-LIT \ \ BPVAL PARAMNAME2 = HOCETA CID1 = PX CID2 = HAC VALUE = EOS-LIT \ \ BPVAL PARAMNAME2= HOCETA CID1 = PX CID2 = MA VALUE = EOS-LIT \ ? PROPERTIES PARAMETERS BINARY SCALAR "RKTKIJ-1" ? ; "ENG_MOLE" ; \ PROP-LIST PARAMNAME = RKTKIJ SETNO = 1 UNITROW = 0 \ ? PROPERTIES PARAMETERS BINARY "T-DEPENDENT" "ANDKIJ-1"? ; "ENG_MOLE" ; \ PROP-LIST PARAMNAME = ANDKIJ SETNO = 1 UNITROW = 0TUNITROW = 22 TUNITLABEL = F NEL = 2 \ ? PROPERTIES PARAMETERS BINARY "T-DEPENDENT" "ANDMIJ-1" ? ; "ENG_MOLE" ; \ PROP-LIST PARAMNAME = ANDMIJ SETNO = 1 UNITROW = 0 TUNITROW = 22 TUNITLABEL = F NEL = 2 \ ? PROPERTIES PARAMETERS BINARY "T-DEPENDENT" "HENRY-1" ? ; "METCBAR_MOLE" ; \ PROP-LISTPARAMNAME = HENRY SETNO = 1 UNITROW = 20 UNITLABEL = bar TUNITROW = 22TUNITLABEL = C BDBANK = ( BINARY HENRY ) NEL = 6 \ ? PROPERTIES PARAMETERS BINARY "T-DEPENDENT" "NRTL-1" ? ; "METCBAR_MOLE" ; \ PROP-LIST PARAMNAME =NRTL SETNO = 1 UNITROW = 0 TUNITROW = 22 TUNITLABEL = C BDBANK = ( "VLE-IG""LLE-ASPEN" "VLE-LIT" "VLE-HOC" ) NEL = 12 \ \ BPVAL PARAMNAME2 = NRTL CID1= H2O CID2 = NBA UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-IGVAL2 = VLE-IG VAL3 = VLE-IG VAL4 = VLE-IG VAL5 = VLE-IG VAL6 = VLE-IG VAL7 =VLE-IG VAL8 = VLE-IG VAL9 = VLE-IG VAL10 = VLE-IG VAL11 = VLE-IG VAL12 =VLE-IG / PARAMNAME2 = NRTL CID1 = H2O CID2 = HAC UNITROW2 = 0 TUNITROW2 = 22TUNITLABEL2 = C VAL1 = VLE-HOC VAL2 = VLE-HOC VAL3 = VLE-HOC VAL4 = VLE-HOCVAL5 = VLE-HOC VAL6 = VLE-HOC VAL7 = VLE-HOC VAL8 = VLE-HOC VAL9 = VLE-HOC VAL10 = VLE-HOC VAL11 = VLE-HOC VAL12 = VLE-HOC / PARAMNAME2 = NRTL CID1 =NBA CID2 = HAC UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-HOC VAL2 = VLE-HOC VAL3 = VLE-HOC VAL4 = VLE-HOC VAL5 = VLE-HOC VAL6 = VLE-HOC VAL7 = VLE-HOC VAL8 = VLE-HOC VAL9 = VLE-HOC VAL10 = VLE-HOC VAL11 = VLE-HOCVAL12 = VLE-HOC / PARAMNAME2 = NRTL CID1 = H2O CID2 = MA UNITROW2 = 0TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-IG VAL2 = VLE-IG VAL3 = VLE-IG VAL4= VLE-IG VAL5 = VLE-IG VAL6 = VLE-IG VAL7 = VLE-IG VAL8 = VLE-IG VAL9 =VLE-IG VAL10 = VLE-IG VAL11 = VLE-IG VAL12 = VLE-IG / PARAMNAME2 = NRTL CID1= NBA CID2 = MA UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-IGVAL2 = VLE-IG VAL3 = VLE-IG VAL4 = VLE-IG VAL5 = VLE-IG VAL6 = VLE-IG VAL7 =VLE-IG VAL8 = VLE-IG VAL9 = VLE-IG VAL10 = VLE-IG VAL11 = VLE-IG VAL12 =VLE-IG / PARAMNAME2 = NRTL CID1 = HAC CID2 = MA UNITROW2 = 0 TUNITROW2 = 22TUNITLABEL2 = C VAL1 = VLE-HOC VAL2 = VLE-HOC VAL3 = VLE-HOC VAL4 = VLE-HOCVAL5 = VLE-HOC VAL6 = VLE-HOC VAL7 = VLE-HOC VAL8 = VLE-HOC VAL9 = VLE-HOC VAL10 = VLE-HOC VAL11 = VLE-HOC VAL12 = VLE-HOC / PARAMNAME2 = NRTL CID1 =H2O CID2 = PX UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = LLE-ASPEN VAL2 = LLE-ASPEN VAL3 = LLE-ASPEN VAL4 = LLE-ASPEN VAL5 = LLE-ASPEN VAL6 =LLE-ASPEN VAL7 = LLE-ASPEN VAL8 = LLE-ASPEN VAL9 = LLE-ASPEN VAL10 =LLE-ASPEN VAL11 = LLE-ASPEN VAL12 = LLE-ASPEN / PARAMNAME2 = NRTL CID1 = HACCID2 = PX UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-HOC VAL2 =VLE-HOC VAL3 = VLE-HOC VAL4 = VLE-HOC VAL5 = VLE-HOC VAL6 = VLE-HOC VAL7 =VLE-HOC VAL8 = VLE-HOC VAL9 = VLE-HOC VAL10 = VLE-HOC VAL11 = VLE-HOC VAL12 =VLE-HOC \ ? PROPERTIES PARAMETERS BINARY "T-DEPENDENT" "NRTL-2" ? ; "METCBAR_MOLE" ; \ PROP-LIST PARAMNAME = NRTL SETNO = 2 UNITROW = 0 TUNITROW= 22 TUNITLABEL = C BDBANK = ( "VLE-IG" "LLE-ASPEN" "VLE-LIT" ) NEL = 12 \ \BPVAL PARAMNAME2 = NRTL CID1 = H2O CID2 = NBA UNITROW2 = 0 TUNITROW2 = 22TUNITLABEL2 = C VAL1 = VLE-IG VAL2 = VLE-IG VAL3 = VLE-IG VAL4 = VLE-IG VAL5= VLE-IG VAL6 = VLE-IG VAL7 = VLE-IG VAL8 = VLE-IG VAL9 = VLE-IG VAL10 =VLE-IG VAL11 = VLE-IG VAL12 = VLE-IG / PARAMNAME2 = NRTL CID1 = H2O CID2 =MA UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-IG VAL2 = VLE-IGVAL3 = VLE-IG VAL4 = VLE-IG VAL5 = VLE-IG VAL6 = VLE-IG VAL7 = VLE-IG VAL8 =VLE-IG VAL9 = VLE-IG VAL10 = VLE-IG VAL11 = VLE-IG VAL12 = VLE-IG / PARAMNAME2 = NRTL CID1 = H2O CID2 = PX UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = LLE-ASPEN VAL2 = LLE-ASPEN VAL3 = LLE-ASPEN VAL4 =LLE-ASPEN VAL5 = LLE-ASPEN VAL6 = LLE-ASPEN VAL7 = LLE-ASPEN VAL8 = LLE-ASPENVAL9 = LLE-ASPEN VAL10 = LLE-ASPEN VAL11 = LLE-ASPEN VAL12 = LLE-ASPEN /PARAMNAME2 = NRTL CID1 = NBA CID2 = MA UNITROW2 = 0 TUNITROW2 = 22 TUNITLABEL2 = C VAL1 = VLE-IG VAL2 = VLE-IG VAL3 = VLE-IG VAL4 = VLE-IG VAL5= VLE-IG VAL6 = VLE-IG VAL7 = VLE-IG VAL8 = VLE-IG VAL9 = VLE-IG VAL10 =VLE-IG VAL11 = VLE-IG VAL12 = VLE-IG \ ? PROPERTIES REGRESSION "R-1" ? \DATA-GROUPS GROUPID = "D-1" \ \ PARAMSPEC TYPE = "BI-PARAMETER" NEL = 8PARAMNAME = NRTL CIDI = H2O CIDJ = HAC ELEMNO = 2 PINIT = -242.2730940 <0><0> SCALE = 1.0 <0> <0> / TYPE = "BI-PARAMETER" NEL = 8 PARAMNAME = NRTLCIDI = HAC CIDJ = H2O ELEMNO = 2 PINIT = 474.5232630 <0> <0> SCALE = 1.0 <0><0> / TYPE = "BI-PARAMETER" NEL = 8 PARAMNAME = NRTL CIDI = H2O CIDJ = HACELEMNO = 3 PINIT = .3000000000 <0> <0> USAGE = FIX \ \ REPORT \ ? PROPERTIESDATA MIXTURE "D-1" ? ; "METCBAR_MOLE" ; \ "SYSTEM-DEF" STATESPEC = TXY CIDS= ( H2O HAC ) PRES = 760. <20> <9> \ \ "PHASE-EQ1" PEQTYPE1 = VL VLECIDS1 =( H2O HAC ) \ \ USING USE = "STD-DEV" / USE = DATA / USE = DATA / USE =DATA / USE = DATA / USE = DATA / USE = DATA / USE = DATA / USE = DATA /USE = DATA / USE = DATA / USE = DATA / USE = DATA / USE = DATA \ \ DATA 1PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 0.1 <0> <0> / 1 PROPLIST ="X_H2O" PROPLABEL = H2O VALUE = "0.1%" <0> <0> / 1 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = "1%" <0> <0> / 2 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 118.5 <0> <0> / 2 PROPLIST = "X_H2O" PROPLABEL = H2OVALUE = 0 <0> <0> / 2 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = 0 <0> <0>/ 3 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 109.7 <0> <0> / 3PROPLIST = "X_H2O" PROPLABEL = H2O VALUE = 0.208 <0> <0> / 3 PROPLIST ="Y_H2O" PROPLABEL = H2O VALUE = 0.331 <0> <0> / 4 PROPLIST = "TEMPERATURE_C"PROPLABEL = C VALUE = 107.2 <0> <0> / 4 PROPLIST = "X_H2O" PROPLABEL = H2OVALUE = 0.327 <0> <0> / 4 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = 0.441<0> <0> / 5 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 105.4 <0> <0>/ 5 PROPLIST = "X_H2O" PROPLABEL = H2O VALUE = 0.468 <0> <0> / 5 PROPLIST ="Y_H2O" PROPLABEL = H2O VALUE = 0.602 <0> <0> / 6 PROPLIST = "TEMPERATURE_C"PROPLABEL = C VALUE = 104.0 <0> <0> / 6 PROPLIST = "X_H2O" PROPLABEL = H2OVALUE = 0.592 <0> <0> / 6 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = 0.713<0> <0> / 7 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 102.7 <0> <0>/ 7 PROPLIST = "X_H2O" PROPLABEL = H2O VALUE = 0.688 <0> <0> / 7 PROPLIST ="Y_H2O" PROPLABEL = H2O VALUE = 0.787 <0> <0> / 8 PROPLIST = "TEMPERATURE_C"PROPLABEL = C VALUE = 101.7 <0> <0> / 8 PROPLIST = "X_H2O" PROPLABEL = H2OVALUE = 0.779 <0> <0> / 8 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = 0.852<0> <0> / 9 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 101.5 <0> <0>/ 9 PROPLIST = "X_H2O" PROPLABEL = H2O VALUE = 0.845 <0> <0> / 9 PROPLIST ="Y_H2O" PROPLABEL = H2O VALUE = 0.895 <0> <0> / 10 PROPLIST = "TEMPERATURE_C"PROPLABEL = C VALUE = 100.9 <0> <0> / 10 PROPLIST = "X_H2O" PROPLABEL = H2OVALUE = 0.884 <0> <0> / 10 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = 0.918<0> <0> / 11 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 100.7 <0> <0>/ 11 PROPLIST = "X_H2O" PROPLABEL = H2O VALUE = 0.919 <0> <0> / 11 PROPLIST= "Y_H2O" PROPLABEL = H2O VALUE = 0.943 <0> <0> / 12 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE = 100.3 <0> <0> / 12 PROPLIST = "X_H2O"PROPLABEL = H2O VALUE = 0.97 <0> <0> / 12 PROPLIST = "Y_H2O" PROPLABEL = H2OVALUE = 0.978 <0> <0> / 13 PROPLIST = "TEMPERATURE_C" PROPLABEL = C VALUE =100.2 <0> <0> / 13 PROPLIST = "X_H2O" PROPLABEL = H2O VALUE = 0.987 <0> <0>/ 13 PROPLIST = "Y_H2O" PROPLABEL = H2O VALUE = 0.991 <0> <0> / 14 PROPLIST= "TEMPERATURE_C" PROPLABEL = C VALUE = 100 <0> <0> / 14 PROPLIST = "X_H2O"PROPLABEL = H2O VALUE = 1 <0> <0> / 14 PROPLIST = "Y_H2O" PROPLABEL = H2OVALUE = 1 <0> <0> \ ? "PROP-SET" MAIN HXDESIGN ? ; "SI_MOLE" ; \ P1 ID =MASSVFRA \ \ P1 ID = MASSFLMX UNITS = ( "kg/sec" ) \ \ P1 ID = HMX UNITS= ("J/kg" ) \ \ P1 ID = RHOMX UNITS = ( "kg/cum" ) \ \ P1 ID = CPMX UNITS = ("J/kg-K" ) \ \ P1 ID = PCMX UNITS = ( "N/sqm" ) \ \ P1 ID = MUMX UNITS = ("N-sec/sqm" ) \ \ P1 ID = KMX UNITS = ( "Watt/m-K" ) \ \ P1 ID = SIGMAMX UNITS = ( "N/m" ) \ \ P1 ID = MWMX \ \ P2 PHASE = ( T V L ) \ \ DESCRIPTION DESCRIPTION = "Thermal and transport, for heat exchanger design" \ ? "PROP-SET"MAIN THERMAL ? ; "METCBAR_MOLE" ; \ P1 ID = HMX UNITS = ( "cal/gm" ) \ \ P1ID = CPMX UNITS = ( "cal/gm-K" ) \ \ P1 ID = KMX \ \ P2 SUBSTREAM = MIXEDPHASE = ( V L ) \ \ DESCRIPTION DESCRIPTION ="Enthalpy, heat capacity, and themral conductivity" \ ? "PROP-SET" MAIN TXPORT ? ; "METCBAR_MOLE" ; \ P1 ID = RHOMX UNITS = ( "kg/cum" ) \ \ P1 ID =MUMX \ \ P1 ID = SIGMAMX \ \ P2 SUBSTREAM = MIXED PHASE = ( V L ) \ \DESCRIPTION DESCRIPTION = "Density, viscosity, and surface tension" \ ?"PROP-SET" MAIN VLE ? ; "METCBAR_MOLE" ; \ P1 ID = PHIMX \ \ P1 ID = GAMMA \\ P1 ID = PL \ \ P2 SUBSTREAM = MIXED PHASE = ( V L ) \ \ DESCRIPTION DESCRIPTION = "Fugacity, activity, and vapor pressure" \ ? "PROP-SET" MAINVLLE ? ; "METCBAR_MOLE" ; \ P1 ID = PHIMX \ \ P1 ID = GAMMA \ \ P1 ID = PL \\ P2 SUBSTREAM = MIXED PHASE = ( V L1 L2 ) \ \ DESCRIPTION DESCRIPTION ="Fugacity, activity, and vapor pressure" \ ? "STREAM-NAMES" ? ? STREAM MATERIAL 45 ? ; "METCBAR_MOLE" ; \ SUBSTREAM SSID = MIXED TEMP = 70.<22> <4>PRES = 4.6 <20> <5> BASIS = "MASS-FLOW" TOTAL = 19672. <-80> <0> JUNK = 3 \ \MOLE-FLOW SSID1 = MIXED CID = H2O FLOW = 10918. <-80> <3> / SSID1 = MIXEDCID = HAC FLOW = 8647. <-80> <3> / SSID1 = MIXED CID = MA FLOW = 107. <-80><3> \ ? STREAM MATERIAL "126+139" ? ; "METCBAR_MOLE" ; \ SUBSTREAM SSID =MIXED TEMP = 40. <22> <4> PRES = 1. <20> <3> BASIS = "MASS-FLOW" TOTAL =11547. <-80> <0> JUNK = 4 \ \ MOLE-FLOW SSID1 = MIXED CID = H2O FLOW= 11128.<-80> <3> / SSID1 = MIXED CID = NBA FLOW = 280. <-80> <3> / SSID1 = MIXEDCID = HAC FLOW = 11. <-80> <3> / SSID1 = MIXED CID = MA FLOW = 128. <-80><3> \ ? STREAM MATERIAL 129 ? ; "METCBAR_MOLE" ; \ SUBSTREAM SSID = MIXEDTEMP = 30. <22> <4> PRES = 1. <20> <3> BASIS = "MASS-FLOW" TOTAL = 4.01 <-80><0> JUNK = 2 \ \ MOLE-FLOW SSID1 = MIXED CID = NBA FLOW = 4. <-80> <3> /SSID1 = MIXED CID = PX FLOW = 0.01 <-80> <3> \ ? STREAM MATERIAL "142+143" ?; "METCBAR_MOLE" ; \ SUBSTREAM SSID = MIXED TEMP = 40. <22> <4> PRES = 1.2<20> <3> BASIS = "MASS-FLOW" TOTAL = 31863. <-80> <0> JUNK = 4 \ \ MOLE-FLOWSSID1 = MIXED CID = H2O FLOW = 838. <-80> <3> / SSID1 = MIXED CID = NBA FLOW= 28776. <-80> <3> / SSID1 = MIXED CID = MA FLOW = 393. <-80> <3> / SSID1= MIXED CID = PX FLOW = 1856. <-80> <3> \ ? BLOCK FSPLIT M1 ? ; "METCBAR_MOLE"; ; DOT ; \ PARAM SID = 45A FRAC = 0.5 <0> <0> / SID = 45B \ \ STREAM-ORDER ORDER-STREAM = 45A / ORDER-STREAM = 45B \ ? BLOCK FSPLIT M2 ? ; "METCBAR_MOLE"; ; DOT ; \ PARAM SID = 142 FRAC = 0.9 <0> <0> / SID = 143 \ \ STREAM-ORDER ORDER-STREAM = 142 / ORDER-STREAM = 143 \ ? BLOCK FSPLIT M3 ? ; "METCBAR_MOLE"; ; DOT ; \ PARAM SID = 126 / SID = 139 FRAC = 0.048 <0> <0> \ \ STREAM-ORDER ORDER-STREAM = 126 / ORDER-STREAM = 139 \ ? BLOCK HEATER "YE-500"? ; "METCBAR_MOLE" ; ; HEATER ; \ PARAM TEMP = 40. <22> <4> PRES = 1.02 <20><5> \ ? BLOCK HEATER "YE-513" ? ; "METCBAR_MOLE" ; ; HEATER ; \ PARAM TEMP =65. <22> <4> PRES = 0.029 <20> <23> \ ? BLOCK DECANTER "YD-501" ? ; "METCBAR_MOLE" ; ; "H-DRUM" ; \ PARAM TEMP = 40. <22> <4> PRES = 1.<20> <3>KLL-CORR = PROPOPTSET LL-METH = "EQ-SOLVE" L2-COMPS = ( H2O ) \ \ PROPERTIESOPSETNAME = NRTL \ \ "BLOCK-OPTION" BLKOPFREWAT = NO \ ? BLOCK RADFRAC "YT-501"? ; "METCBAR_MOLE" ; ; STRIP1 ; \ PARAM NSTAGE = 60 ALGORITHM = NONIDEALEFF= MURPHREE INIT-OPTION = AZEOTROPIC MAXOL = 200 GAMMA-MODEL = COMBINED NO-PHASE = 2 DAMPING = NONE OPT-PRES = "DP-COL" VIEW-PRES = PROFILE CONV-METH= OTHERS \ \ "COL-CONFIG" CONDENSER = NONE REBOILER = THERMOSYPHON \ \ FEEDSFEED-SID = 45A FEED-STAGE = 30 / FEED-SID = 45B FEED-STAGE = 37 / FEED-SID= 142 FEED-STAGE = 1 / FEED-SID = 143 FEED-STAGE = 22 / FEED-SID = 139FEED-STAGE = 1 \ \ PRODUCTS PROD-STREAM = 120 PROD-STAGE = 1 PROD-PHASE = VP-S = N / PROD-STREAM = 121 PROD-STAGE = 60 PROD-PHASE = L P-S = N \ \P-SPEC PRES-STAGE = 1 STAGE-PRES = 1.02 <20> <5> / PRES-STAGE = 60 STAGE-PRES = 1.25 <20> <5> \ \ "P-SPEC2" PRES1 = 1.02 <20> <5> \ \ "COL-SPECS"DP-COL = 0.23 <75> <5> BASIS-RDV = 1.0 <0> <0> B-BASIS = MASS BASIS-B = 9192.<-80> <3> \ \ "DB:F-PARAMS" DB-STREAMS = ( 45A 45B ) DB-COMPS = ( HAC ) \ \THERMOSYPHON TH-TEMP = 120. <22> <4> TH-BASIS = MASS OPT-TH-REB = OUTLET \ \STAGE-EFF SEFF-STAGE = 1 STAGE-EFF = 0.6 <0> <0> / SEFF-STAGE = 60 STAGE-EFF= 0.6 <0> <0> \ \ T-EST TEMP-STAGE = 1 TEMP-EST = 90. <22> <4> / TEMP-STAGE= 60 TEMP-EST = 118. <22> <4> \ \ SPEC SPEC-NO = 1 SPEC-TYPE = "MASS-FLOW" VALUE = 11. <0> <0> SPEC-COMPS = ( HAC ) SPEC-STREAMS = ( 120 ) SPEC-HIDE =HIDDEN \ \ VARY VARY-NO = 1 VARTYPE = D LB = 30000. <0> <0> UB = 50000.<0><0> VARY-HIDE = HIDDEN \ \ "KLL-VECS" \ \ "BLOCK-OPTION" BLKOPFREWAT = NO \ \"TRSZ-VECS" \ \ "PCKSR-VECS" \ ? BLOCK RADFRAC "YT-511" ? ; "METCBAR_MOLE" ;; FRACT1 ; \ PARAM NSTAGE = 25 ALGORITHM = NONIDEAL EFF = MURPHREE INIT-OPTION = STANDARD MAXOL = 100 GAMMA-MODEL = COMBINED NO-PHASE = 2DAMPING = NONE OPT-PRES = "DP-COL" VIEW-PRES = PROFILE CONV-METH = OTHERS \ \"COL-CONFIG" CONDENSER = TOTAL REBOILER = THERMOSYPHON \ \ FEEDS FEED-SID =140 FEED-STAGE = 13 \ \ PRODUCTS PROD-STREAM = 145 PROD-STAGE = 25PROD-PHASE= L P-S = N / PROD-STREAM = 130 PROD-STAGE = 7 PROD-PHASE = L FLOW-BASIS =MASS PROD-FLOW = 510. <-80> <3> / PROD-STREAM = 131 PROD-STAGE = 1 PROD-PHASE = L P-S = N \ \ P-SPEC PRES-STAGE = 1 STAGE-PRES = 1.01 <20> <5>/ PRES-STAGE = 25 STAGE-PRES = 1.22 <20> <5> \ \ "P-SPEC2" PRES1 = 1.01 <20><5> \ \ "COL-SPECS" DP-COL = 0.21 <75> <5> BASIS-RDV = 0.0 <0> <0> D-BASIS =MASS BASIS-D = 97. <-80> <3> RR-BASIS = MASS BASIS-RR = 30. <0> <0> \ \"DB:F-PARAMS" DB-STREAMS = ( 140 ) DB-COMPS = ( MA ) \ \ "SC-REFLUX" SC-TEMP= 40. <22> <4> \ \ THERMOSYPHON TH-TEMP = 106. <22> <4> OPT-TH-REB = OUTLET\ \ STAGE-EFF SEFF-STAGE = 1 STAGE-EFF = 0.9 <0> <0> / SEFF-STAGE = 2STAGE-EFF = 0.6 <0> <0> / SEFF-STAGE = 25 STAGE-EFF = 0.6 <0> <0> \ \ T-ESTTEMP-STAGE = 7 TEMP-EST = 92. <22> <4> / TEMP-STAGE = 25 TEMP-EST = 105.3<22> <4> \ \ "KLL-VECS" \ \ "BLOCK-OPTION" BLKOPFREWAT = NO \ \ "TRSZ-VECS" \\ "PCKSR-VECS" \ ? "EO-CONV-OPTI" ? \ DMO-PARAMS MODE = DEFAULT \ \ DMO-PARAMS MODE = SIMULATION \ \ DMO-PARAMS MODE = "PARAMETER-ESTIMATION" \ \DMO-PARAMS MODE = RECONCILIATION \ \ DMO-PARAMS MODE = OPTIMIZATION \ \LSSQP-PARAMS MODE-L = DEFAULT \ \ LSSQP-PARAMS MODE-L = SIMULATION \ \LSSQP-PARAMS MODE-L = "PARAMETER-ESTIMATION" \ \ LSSQP-PARAMS MODE-L =RECONCILIATION \ \ LSSQP-PARAMS MODE-L = OPTIMIZATION \ ? "CONV-OPTIONS" ? \WEGSTEIN WEG-MAXIT = 30 \ ? CONVERGENCE BROYDEN "C-1" ? \ TEAR SID = "142+143"/ SID = "126+139" \ \ PARAM MAXIT = 30 \ ? "CONV-ORDER" ? ? SEQUENCE "S-1" ?\ SEQUENCE BLOCK-TYPE = BLOCK BLOCK-ID = M1 / RETURN = BEGIN BLOCK-TYPE =CONVERGENCE BLOCK-ID = "C-1" / BLOCK-TYPE = BLOCK BLOCK-ID = M2 / BLOCK-TYPE = BLOCK BLOCK-ID = M3 / BLOCK-TYPE = BLOCK BLOCK-ID = "YT-501" /BLOCK-TYPE = BLOCK BLOCK-ID = "YE-500" / BLOCK-TYPE = BLOCK BLOCK-ID ="YE-513" / BLOCK-TYPE = BLOCK BLOCK-ID = "YT-511" / BLOCK-TYPE = BLOCK BLOCK-ID = "YD-501" / RETURN = RETURNTO BLOCK-TYPE = CONVERGENCE BLOCK-ID ="C-1" \ ? REPORT REPORT ? ? REPORT "BLOCK-REPORT" ? ? REPORT "STREAM-REPOR" ?\ OPTIONS MOLEFLOW = MOLEFLOW MASSFLOW = MASSFLOW MOLEFRAC = MOLEFRAC MASSFRAC = MASSFRAC \ ? REPORT "FLOWSHEET-RE" ? ? REPORT "PROPERTY-REP" ? \OPTIONS PCES = PCES PROP-DATA = "NOPROP-DATA" DFMS = NODFMS \ ? REPORT "ADA-REPORT" ? ? REPORT "BATCH-OPERAT" ? ; "METCBAR_MOLE" ;GRAPHICS_BACKUPPFS V 5.00$CONFIGparamdata ENRTL-RKparamdata VLE-IGparamdata VLE-RKparamdata VLE-HOCparamdata LLE-LITparamdata LLE-ASPENparamdata VLE-LITparamdata BINARYparamdata EOS-LITparamdata HENRYpurebank PURE11purebank AQUEOUSpurebank SOLIDSpurebank INORGANICregdbank 1ftn_check 1autoblockid 0autostreamid 0showblockid 1showstreamid 1autoplacement 1grid 2gridresolution 0.100000scale 0streamprefixblockprefix Blabelscale 1.000000qwformat %.3ftempformat %.1fpresformat %.1fflowformat %.1f strmqwformat %.0f vflowformat %.0f mflowformat %.1f vfracformat %.2f pseudobatch 0partial 0animation 1runanyway 0tooldrawvisible 0 browserheight 6465 browserwidth 10770 browsertreewidth 3810 polyplusenabled 1 dynaplusenabled 1 bfracenabled 1rtfenabled 1pinchenabled 0linklimit 500material_color 0material_style 983041 material_width 1material_termidheat_color 0heat_style 983042heat_width 1heat_termid Qwork_color 0work_style 983043work_width 1work_termid Wconnections_color 9 connections_style 983044 connections_width 1 measurements_color 4 measurements_style 983044 measurements_width 1 displayeoconn 0 displayeomeas 1 displayeomeastype 2 showeoviews 0eoautosave 1。
甲醇装置预精馏塔Aspen模拟任务书
甲醇装置预精馏塔Aspen模拟任务书一、模拟计算依据：1、原料处理量：学号后三位XXX × 100 kg/h；2、粗甲醇液进料组成如表1所示(质量分数)；进料条件为：液相进料温度60℃，进料压力140kPa，塔顶（分凝器气相出料）冷凝器压力130kPa，再沸器压力150kPa；3、分离要求：塔顶甲酸甲酯摩尔回收率为99.99%，塔顶甲醇摩尔回收率为0.7%。
4、物性方法：BWRS表1 进料组成表二、任务1、按计算依据，用简捷法（DSTWU模块）模拟计算预精馏塔以分离粗甲醇中的轻组分（建议实际回流比取最小回流比的1.5倍）。
2、在简捷模拟计算中，通过回流比随理论板数变化曲线，确定适宜回流比、理论板数。
及相应的进料位置、塔顶产品与进料的摩尔流量比（D/F)、最小回流比、最小理论板数、实际理论板数、进料位置以及塔顶温度。
3、根据简捷计算的结果，利用严格法（RadFrac模块）对预精馏塔进行严格计算，进料条件、冷凝器形式、冷凝器压力、再沸器压力、再沸器采用釜式再沸器、产品纯度要求以及物性方法与简捷法相同，用严格法核算任务2中的结果（简捷计算结果）是否达到回收率要求。
4、通过严格法（RadFrac模块）设计规定功能，调整回流比、馏出与进料量比以达到分离要求；5、通过Aspen灵敏度分析功能，在严格法中求取回流比随理论板数据的变化曲线，重新确定适宜回流比、理论板数。
6、绘制塔内温度分布曲线、塔内液相质量组成分布曲线、塔内的气相组成分布曲线。
7、书写模拟报告。
以下为选做部分（评优学生必做）6-1、通过Aspen灵敏度分析功能，在严格法中求取进料板位置与再沸器热负荷的关系曲线，重新确定进料板位置。
6-2、设实际塔板的塔板默弗里效率为60%，在严格法中重新设定塔板数、进料板位置；然后在严格法中初步设定塔板类型为浮阀，查看塔板的水力学性质；6-3、对塔进行校核计算，确定塔的结构尺寸、水力学性能、负荷性能。
Aspen plus模拟精馏塔说明书
Aspen plus模拟精馏塔说明书一、设计题目根据以下条件设计一座分离甲醇、水、正丙醇混合物的连续操作常压精馏塔：生产能力：100000吨精甲醇/年；原料组成：甲醇70%w，水%w，丙醇%w；产品组成：甲醇≥%w；废水组成：水≥%w；进料温度：；全塔压降：；所有塔板Murphree 效率。
二、设计要求对精馏塔进行详细设计，给出下列设计结果并利用AutoCAD绘制塔设备图，并写出设计说明。
(1).进料、塔顶产物、塔底产物、侧线出料流量；(2).全塔总塔板数N；最佳加料板位置N F；最佳侧线出料位置N P；(3).回流比R；(4).冷凝器和再沸器温度、热负荷；(5).塔内构件塔板或填料的设计。
三、分析及模拟流程1.物料衡算（手算）目的:求解Aspen 简捷设计模拟的输入条件。
内容:(1)生产能力:一年按8000 hr计算，进料流量为100000/(8000*= t/hr。
(2)原料、塔顶与塔底的组成（题中已给出）：原料组成：甲醇70%w，水%w，丙醇%w；产品:甲醇≥%w；废水组成：水≥%w。
(3).温度及压降：进料温度：；全塔压降：；所有塔板Murphree 效率。
2.用简捷模块（DSTWU）进行设计计算目的:对精馏塔进行简捷计算，根据给定的加料条件和分离要求计算最小回流比、最小理论板数、理论板数和加料板位置。
3.灵敏度分析目的:研究回流比与塔径的关系（N T-R），确定合适的回流比与塔板数；研究加料板位置对产品的影响，确定合适的加料板位置。
方法:作回流比与塔径的关系曲线（N T-R），从曲线上找到期望的回流比及塔板数。
4. 用详细计算模块（RadFrac）进行计算目的:精确计算精馏塔的分离能力和设备参数。
方法:用RadFrac模块进行精确计算，通过设计规定(Design Specs)和变化(Vary)两组对象进行设定，检验计算数据是否收敛，计算出塔径等主要尺寸。
5. 塔板设计目的：通过塔板设计(Tray sizing)计算给定板间距下的塔径。
aspen精馏塔设计
2）输入 C3H6
2）点击 Find now
输入组分，1）点击 Find 选 DSTWU
1）输入 C3H6
选择
点 Add
` 点击 下拉菜单， 选择物性方法
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点击 打开物性 方法对话框
` ` 然后点next按钮， 一直点击，系统 会自动调入所需 的物性数据
从下拉菜单中 选择 CHAOSEA物性方法
输入完后，一直点 按钮，运行软件。 运行完后，点 按钮，察看结果。
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根据DSTWU模型计算的结果，得到 回流比R，理论板N，进料位置FN，采出量D 选择RadFrac模块，进行严格计算。
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运行软件，检查结果，看分离是否满足要求。
若不满足设计要求，可改变回流比、采出量、 进料位置。 也可以采用designe规定，
精馏塔设计
要求设计一个精馏塔，实现丙烷和丁烷的分 离。 进料温度323k 压力 20atm 进料量 1kmol/sec 进料组成（wt%） 分离目标 丙烷 0.4 塔顶 丙烷> 99% 丁烷 0.6 塔釜 丁烷>99%
先用DSTWU求最小理论板数和回流比
点击
选择基 本单位
先点击 Report Option，再点Stream，然后选择 mass，和mass fraction
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结果是否满足设计要求。
使用设计规定
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1）先点 Design Specs, 2) 再点new；3）点对话 框中的ok
从类型的下拉菜单中选择mass purity
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运行后，查看结果。
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塔径计算 Pack sizing
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Aspen简捷法精馏塔设计计算解析
第 9页
5 塔Columns模块---简捷蒸馏模块
SCFrac (简捷法多塔蒸馏)
对每个塔段必需规定产品压力和基于进料流率
的产品流率或分率，对所有产品，除馏出物外 必须规定蒸汽与产品的比值。
计算中由于进行蒸汽计算，所以水必须被定义
为一个组分。所以水都与塔顶产品一起离开。
该模型不能处理固体，游离水计算可在冷凝器
5 简捷法精馏塔设计计算
1
第 1页
5 塔Columns模块
塔设备是化工生产中应用最为广泛的操作设备 之一，通常在其中进行蒸馏（精馏）、吸收和 萃取单元操作。吸收和蒸馏实际都是气液相平 衡的单元操作，只是蒸馏过程的热量平衡相对 更为复杂。
对塔设备可分为三大类：简捷法计算的蒸馏塔 、严格法计算的蒸馏塔和液-液萃取塔三类。
第 6页
5 塔Columns模块---简捷蒸馏模块
Distl（简捷法精馏核算）
Distl模型可以模拟一个带有一股进料和两种 产品的多级多组分的蒸馏塔，塔可带有分凝 器或全凝器。模型假定恒摩尔流和恒相对挥 发度。用Edimister法进行产品组成。
第 7页
5 塔Columns模块---简捷蒸馏模块
中完成。
第10页
5 塔Columns模块---简捷蒸馏模块
SCFrac (简捷法多塔蒸馏)
SCFrac估算：
产品组成和流率
每一段的级数
每一段的热或冷负荷
该模型不能处理固体，游离水计算可在冷凝器 中完成。
第11页
例5-1 简捷法精馏设计计算
• 利用精馏方法对附表中进料流 股进行分离，其压强为445830 Pa， 处于饱和液体状态。规定 该分离操作的轻、重关键组分 分别为N-Butane和I-Pentane， 塔顶产品中轻、重关键组分的 回收率（recovery）分别为0.99 08和0.0112，并规定操作采用 回流比为最小回流比的1.8倍。 体系热力学性质计算采用“SR K”模型方程。 试确定：该条件下的最小回流 比、理论板数、最小理论板数 及适宜的进料位置。 组分 Propane I-Butane N-Butane I-Pentane 流量 / kmol/s 0.0006 0.0013 0.0038 0.0025
14-ASPEN_酯化反应精馏-动力学
酯化反应精馏塔的模拟计算
一、工艺流程简述
酯化反应精馏塔,其工流流程如图26-1所示，在精馏塔内乙酸与乙醇发生酯化反应，生成乙酸乙酯和水，该反应为可逆反应。
图26-1 酯化反应精馏塔模拟计算流程图
二、需要输入的主要参数
1、 装置进料数据
表26.1 进料数据
物流号 FEED
温度，℃ 70
压力，atm 5.0 组份流量，kmol/h
乙酸（AA） 50
乙醇（ETOH） 50
2、 单元操作参数
DA501塔操作压力atm 1.00
全塔压降MPa 0.03
理论板数 15
进料板7
冷凝器类型 全凝器
塔顶产品 30kmol/h
回流比 0.70
3、反应数据
乙酸（AA）+乙醇(ETOH)←→乙酸乙酯(EA)+水
正反应
R=1.9E8-5.95E7/RT[AA][ETOH]
逆反应
R=5.0E7-5.95E7/RT[AA][ETOH]
浓度单位 kmol/m3
反应速率单位 kmol/m3.S
活化能J/kmol
液相反应，滞液量再沸器1.0L,其它板0.3L.
三、软件版本
采用ASPEN PLUS 软件V7.2版本，保存文件名KINETICS.APW。
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例：设计一个脱乙烷精馏塔，进料流量为100kmol/hr ，进料摩尔分数：氢气0.00014、甲烷0.0016、乙烯0.75746、丙烯0.00075、乙烷0.24003.进料压力18atm ，泡点进料，要求乙烯在塔顶的回收率达到0.95，并且塔顶的流出物中乙烯的纯度达到0.99，塔顶设一全凝器，操作压力为17.8atm ，塔釜有再沸器，操作压力为18.2atm ，回流比取3，热力学模型选reng-robinson 方程试用简捷法确定精馏塔的理论塔板数、进料位置以及产品流股的组成。
提示：乙烷回收率计算如下
塔顶乙烯量=100x0.75746x0.95=71.9587kmol
塔顶氢气量=100x0.00014=0.014kmol （全部回收）
塔顶甲烷量=100x0.00162=0.162kmol （全部回收）
塔顶丙烯量=0
乙烯浓度：
x 9587.71162.0014.09587
.7199.0乙烷量塔顶乙烯量+++=
X=0.550855kmol
乙烷回收率=0.022949
选着模板和米制单位进入Aspen plus界面，用dstwu模块建立流程，如下图：
点击next键，进入全局设定，为模拟命名：
点击next键，输入包含的物质：
点击next键，选着物性方法peng-rob：
点击next键，进入二元交互参数界面，此处不需改动：
点击next键，输入进料物流信息（泡点进料即气相分率为0）：
点击next键，输入精馏塔信息：
点击next键，开始运行模拟：
查看物流结果：
查看精馏塔结果：。