一萬噸年產(chǎn)量的乙苯脫氫法制苯乙烯的物料、熱量衡算計(jì)算過程案例目錄TOC\o"1-3"\h\u25764一萬噸年產(chǎn)量的乙苯脫氫法制苯乙烯的物料、熱量衡算計(jì)算過程案例 187131.1物料衡算 115721物料衡算匯總表 2123821.2熱量衡算 2316769熱量衡算匯總表 371.1物料衡算根據(jù)本文物系極性不強(qiáng)的特點(diǎn)，選用的是P-R狀態(tài)方程模擬計(jì)算。但在體系中還有水的存在，因此單純選擇狀態(tài)方程法不能滿足精度要求。由于NRTL方法能夠準(zhǔn)確地預(yù)測(cè)雙液相的出現(xiàn)，適合用于該模擬過程的特點(diǎn)，因此，對(duì)含水物系的組分及相平衡采用NRTL方程模擬計(jì)算本文流程所包括的單元主要包括：反應(yīng)器、蒸汽過熱爐、精餾塔、換熱器、混合器。反應(yīng)器模塊：根據(jù)各反應(yīng)器模型特點(diǎn)和主要目標(biāo)，選擇RStoic模型模擬苯乙烯反應(yīng)過程，其用于模擬化學(xué)平衡數(shù)據(jù)和動(dòng)力學(xué)數(shù)據(jù)未知或不重要的反應(yīng)器。在進(jìn)行計(jì)算時(shí)，需要規(guī)定反應(yīng)器的操作條件，規(guī)定涉及的反應(yīng)化學(xué)計(jì)量系數(shù)，并指定反應(yīng)的轉(zhuǎn)化率或產(chǎn)品流率。塔器模塊選擇：過程模擬包括的塔設(shè)備較多，主要為精餾塔。RadFrac模型不僅可以用于對(duì)精餾塔的模擬，還可以處理其他分離模型。RadFrac模型可以處理多種物系系統(tǒng)，并且AspenPlus軟件為不同的物系提供了不同的收斂方法，可方便各種系統(tǒng)求解。換熱模塊選擇：本模擬使用Heater和HeatX單元模塊對(duì)蒸汽過熱爐和換熱器進(jìn)行模擬。其可處理大部分雙物流，并可根據(jù)實(shí)際模擬需要分別提供簡(jiǎn)捷和嚴(yán)格計(jì)算兩種計(jì)算方式。本工作采用AspenPlus軟件建立了乙苯脫氫制苯乙烯工藝的流程模擬，如圖3.1所示圖3.1乙苯脫氫制苯乙烯脫氫工段模擬流程圖根據(jù)以上模擬流程圖繪制的脫氫工段物料衡算框圖如下：圖3.2乙苯脫氫制苯乙烯脫氫工段物料衡算框圖（一）脫氫工段1.設(shè)備：預(yù)混器M-101定開工時(shí)間8000h，苯乙烯年產(chǎn)量是1萬噸，工業(yè)乙苯原料純度＞99.0%余者為苯，且循環(huán)比=循環(huán)乙苯量/新鮮乙苯量=0.6。通過Aspen計(jì)算，為保證苯乙烯收率大于99.95%，苯乙烯產(chǎn)量：10000000/8000=1250kg/h所需乙苯用量：1250/（0.91*0.62）=2215.526kg/h初始模擬進(jìn)料全部使用工業(yè)乙苯原料，進(jìn)料為2215.526kg/h，模擬出脫乙苯塔中乙苯出料量719.397kg/h，根據(jù)AspenPlus模擬，當(dāng)程序收斂時(shí)，所使用的工業(yè)乙苯原料為1509kg/h，循環(huán)乙苯量為719.397kg/h。因此預(yù)混器中<1>輸入新鮮乙苯1509kg/h，<2>輸入循環(huán)乙苯量719.397kg/h。模擬過程所輸入的主要參數(shù)：<1>→溫度：25℃、壓力：1bar、乙苯進(jìn)料量：1509kg/h、進(jìn)料物質(zhì)中乙苯的質(zhì)量分率為0.99，其余為甲苯圖3.3預(yù)混器物料衡算框圖圖3.4預(yù)混器物料衡算模擬結(jié)果表3.1預(yù)混器M-101物料衡算表物質(zhì)名稱單位<1><2><3>ETHYL-01（乙苯）kg/hr1493.91719.3972213.307STYRE-01（苯乙烯）kg/hr00.3270.327H2（氫氣）kg/hr000BENZE-01（苯）kg/hr15.090.00032415.090TOLUE-01（甲苯）kg/hr00.2750.275H2O（水）kg/hr000NAPHT-01（萘）kg/hr000NAPHT-02（2-甲基萘）kg/hr000CO2（二氧化碳）kg/hr000METHA-01（甲烷）kg/hr000ETHAN-01（乙烷）kg/hr000CARBO-01（一氧化碳）kg/hr0002.設(shè)備：混合器M-102乙苯蒸汽與700℃的水蒸氣混合，其中因焦油是混合物，故在aspen中選擇以萘，2-甲基萘代表焦油，在混合器M-102添加焦油二氧化碳進(jìn)料為14.117kg/h，進(jìn)料量是根據(jù)焦油以及二氧化碳的選擇性為1%，乙苯轉(zhuǎn)化率為62%，苯乙烯年產(chǎn)量10000噸產(chǎn)生焦油/二氧化碳量：2215.526*0.62*0.01=14.117kg/h規(guī)定烴氣比為1：15（摩爾比）則輸入的水蒸氣進(jìn)料量為：（（1509+719.397）/106）*15*18=5676.1kg/h模擬過程所輸入的主要參數(shù)：<5>→溫度：25℃、壓力：1bar、萘：7.0587kg/h、2-甲基萘：7.0587kg/h、CO2：14.1174kg/h<6>→溫度：700℃、壓力：1bar、水的質(zhì)量流量：5767kg/h圖3.5混合器物料衡算框圖圖3.6混合器物料衡算模擬結(jié)果表3.2混合器M-102物料衡算表物質(zhì)名稱單位<5><6><7><8>ETHYL-01kg/hr2213.307002213.307STYRE-01kg/hr0.327000.327H2kg/hr0000BENZE-01kg/hr15.090015.09TOLUE-01kg/hr0.275000.275H2Okg/hr005987.285987.279NAPHT-01kg/hr07.05907.059NAPHT-02kg/hr07.05907.059CO2kg/hr014.117014.117METHA-01kg/hr0000ETHAN-01kg/hr0000CARBO-01kg/hr00003.設(shè)備：第一段脫氫反應(yīng)器R-101已知第一段絕熱式反應(yīng)器乙苯的轉(zhuǎn)化率是42%，乙苯的總體轉(zhuǎn)化率是62%（1）主反應(yīng)C6H5C2H5→C6H5C2H3+H2乙苯轉(zhuǎn)化率：0.42*0.91=0.38（2）副反應(yīng)C6H5CH2CH3+H2→C6H5CH3+CH4乙苯轉(zhuǎn)化率：0.42*0.04=0.168C6H5CH2CH3+H2→C6H6+C2H6乙苯轉(zhuǎn)化率：0.42*0.03=0.0126CH4+H2O→CO+3H2甲烷轉(zhuǎn)化率：0.25CO+H2O→H2+CO2一氧化碳轉(zhuǎn)化率：1（根據(jù)一氧化碳選擇性1%等假定轉(zhuǎn)化率為1）將以上各反應(yīng)的轉(zhuǎn)化率輸入，進(jìn)行模擬圖3.7第一段脫氫反應(yīng)器物料衡算框圖圖3.8第一段脫氫反應(yīng)器物料衡算模擬結(jié)果表3.3第一段脫氫反應(yīng)器R-101物料衡算表物質(zhì)名稱單位<8><9>ETHYL-01kg/hr2213.3071283.718STYRE-01kg/hr0.327847.127H2kg/hr015.129BENZE-01kg/hr15.0936.26TOLUE-01kg/hr0.27532.93H2Okg/hr5987.285987.28NAPHT-01kg/hr7.0597.059NAPHT-02kg/hr7.0597.059CO2kg/hr14.11714.117METHA-01kg/hr05.686ETHAN-01kg/hr08.149CARBO-01kg/hr004.設(shè)備：第二段脫氫反應(yīng)器R-102（1）主反應(yīng)C6H5C2H5→C6H5C2H3+H2乙苯轉(zhuǎn)化率：（（0.62-0.42）*0.91）/（1-0.42）=0.32（2）副反應(yīng)C6H5CH2CH3+H2→C6H5CH3+CH4乙苯轉(zhuǎn)化率：（（0.62-0.42）*0.04）/（1-0.42）=0.014C6H5CH2CH3+H2→C6H6+C2H6乙苯轉(zhuǎn)化率：（（0.62-0.42）*0.03）/（1-0.42）=0.011CH4+H2O→CO+3H2甲烷轉(zhuǎn)化率：0.25CO+H2O→H2+CO2一氧化碳轉(zhuǎn)化率：1（根據(jù)一氧化碳選擇性1%等假定轉(zhuǎn)化率為1）將以上各反應(yīng)的轉(zhuǎn)化率輸入，進(jìn)行模擬圖3.9第二段脫氫反應(yīng)器物料衡算框圖圖3.10第二段脫氫反應(yīng)器物料衡算模擬結(jié)果表3.4第二段脫氫反應(yīng)器R-102物料衡算表物質(zhì)名稱單位<10><11>ETHYL-01kg/hr1283.718840.837STYRE-01kg/hr847.1271250.115H2kg/hr15.12922.856BENZE-01kg/hr36.2646.65TOLUE-01kg/hr32.9348.528H2Okg/hr5987.285985.684NAPHT-01kg/hr7.0597.059NAPHT-02kg/hr7.0597.059CO2kg/hr14.11714.117METHA-01kg/hr5.6866.98ETHAN-01kg/hr8.14912.149CARBO-01kg/hr02.4825.設(shè)備：過熱氣體降溫器M-103反應(yīng)氣與20℃的循環(huán)水或混合進(jìn)行降溫模擬過程所輸入的主要參數(shù)：<19>→溫度：20℃、壓力：1bar、水的摩爾流量：100kmol/h圖3.11過熱氣體降溫器物料衡算框圖圖3.12過熱氣體降溫器物料衡算模擬結(jié)果表3.5過熱氣體降溫器M-103物料衡算表物質(zhì)名稱單位<16><19><20>ETHYL-01kg/hr840.8370840.837STYRE-01kg/hr1250.11501250.115H2kg/hr22.856022.856BENZE-01kg/hr46.65046.65TOLUE-01kg/hr48.528048.528H2Okg/hr5985.6841801.5287787.212NAPHT-01kg/hr7.05907.059NAPHT-02kg/hr7.05907.059CO2kg/hr14.117014.117METHA-01kg/hr6.9806.98ETHAN-01kg/hr12.149012.149CARBO-01kg/hr2.48202.4826.設(shè)備：氣液分離器SEP1冷卻后的混合物在氣液分離罐中進(jìn)行氣液分離，得到的氣體直接燃燒，液體則進(jìn)入分相器進(jìn)行進(jìn)一步分離模擬過程所輸入的主要參數(shù)<22>→H2、CO2、CH4、C2H6、CO的分離分率設(shè)置為0圖3.13氣液分離器物料衡算框圖圖3.14氣液分離器物料衡算模擬結(jié)果表3.6氣液分離器SEP1物料衡算表物質(zhì)名稱單位<21><22><23>ETHYL-01kg/hr840.837840.8370STYRE-01kg/hr1250.1151250.1150H2kg/hr22.856022.856BENZE-01kg/hr46.6546.650TOLUE-01kg/hr48.52848.5280H2Okg/hr7787.2127787.2120NAPHT-01kg/hr7.0597.0590NAPHT-02kg/hr7.0597.0590CO2kg/hr14.117014.117METHA-01kg/hr6.9806.98ETHAN-01kg/hr12.149012.149CARBO-01kg/hr2.48202.4827.設(shè)備：分相器SEP2液體進(jìn)入分相器進(jìn)行進(jìn)一步分離。分離后，水層可以用做循環(huán)水，而油層是乙苯/苯乙烯精餾塔的進(jìn)料<24>→H2O分離分率設(shè)置為0圖3.15分相器物料衡算框圖圖3.16分相器物料衡算模擬結(jié)果表3.7分相器SEP2物料衡算表物質(zhì)名稱單位<22><24><25>ETHYL-01kg/hr840.837840.8370STYRE-01kg/hr1250.1151250.1150H2kg/hr000BENZE-01kg/hr46.6546.650TOLUE-01kg/hr48.52848.5280H2Okg/hr7787.21207787.212NAPHT-01kg/hr7.0597.0590NAPHT-02kg/hr7.0597.0590CO2kg/hr000METHA-01kg/hr000ETHAN-01kg/hr000CARBO-01kg/hr000（二）精制工段圖3.17乙苯脫氫制苯乙烯精制工段模擬流程圖根據(jù)以上模擬流程圖繪制精制工段物料衡算框圖如下：圖3.18乙苯脫氫制苯乙烯精制工段物料衡算框圖1.設(shè)備：脫乙苯塔T-201經(jīng)過DSTWU模塊進(jìn)行簡(jiǎn)捷計(jì)算，確定RADFRAC模塊的回流比為11、塔板數(shù)為87，進(jìn)料板位置為第46塊塔板，設(shè)定塔釜流量為1264.5kg/h，塔頂壓力0.3866bar等參數(shù)，然后進(jìn)行模擬運(yùn)行圖3.19脫乙苯塔物料衡算框圖圖3.20脫乙苯塔物料衡算模擬結(jié)果表3.8脫乙苯塔T-201物料衡算表物質(zhì)名稱<24><26><27>摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）ETHYL-010.374840.8370.875840.2370.0004670.6STYRE-010.5671250.1150.0003530.3320.9911249.783H2000000BENZE-010.028246.650.06646.652.05x10-361.939x10-33TOLUE-010.024948.5280.058348.5281.435x10-191.601x10-16H2O000000NAPHT-010.00267.0593.228x10-543.741x10-510.004557.059NAPHT-020.002357.0593.486x10-734.482x10-700.00417.059CO2000000METHA-01000000ETHAN-01000000CARBO-010000002.設(shè)備：乙苯回收塔T-202經(jīng)過DSTWU模塊進(jìn)行簡(jiǎn)捷計(jì)算，確定RADFRAC模塊的回流比為3.5、塔板數(shù)28，進(jìn)料板位置為第17塊塔板，塔頂壓力1bar，塔釜流量720kg/h，然后進(jìn)行模擬運(yùn)行圖3.21乙苯回收塔物料衡算圖圖3.22乙苯回收塔物料衡算模擬結(jié)果表3.10乙苯回收塔T-202物料衡算表物質(zhì)名稱<28><29><30>摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）ETHYL-010.875840.2370.504120.840.999719.397STYRE-010.0003530.3322.06940.004870.0004630.327H2000000BENZE-010.066146.650.26446.656.112x10-70.000324TOLUE-010.058348.52858410.232849548.25387010.0004485220.275H2O000000NAPHT-013.228x10-543.741x10-510000NAPHT-023.486x10-734.482x10-700000CO2000000METHA-01000000ETHAN-01000000CARBO-010000003.設(shè)備：苯/甲苯精餾塔T-203經(jīng)過DSTWU模塊進(jìn)行簡(jiǎn)捷計(jì)算，確定RADFRAC模塊的回流比為1.41、塔板數(shù)23，進(jìn)料板為第12塊塔板，D/F=0.567，然后進(jìn)行模擬運(yùn)行圖3.23苯/乙苯塔物料衡算框圖圖3.24苯/甲苯塔物料衡算模擬結(jié)果表3.12苯/甲苯精餾塔T-203物料衡算表物質(zhì)名稱<29><31><32>摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）ETHYL-010.504120.840.12617.1680.998103.672STYRE-012.069x10-50.004872.695x10-73.595x10-54.744x10-50.00483H2000000BENZE-010.26446.650.46646.6501.471x10-60.000112TOLUE-010.23248.2530.40848.100.00170.153H2O000000NAPHT-01000000NAPHT-02000000CO2000000METHA-01000000ETHAN-01000000CARBO-010000004.設(shè)備：苯乙烯精制塔T-204經(jīng)過DSTWU模塊進(jìn)行簡(jiǎn)捷計(jì)算，確定RADFRAC模塊的回流比為1、塔板數(shù)為18，進(jìn)料位置為第12塊塔板，控制塔頂收率為1250kg/h，然后進(jìn)行模擬運(yùn)行圖3.25苯乙烯精制塔物料衡算框圖圖3.26苯乙烯精餾塔物料衡算模擬結(jié)果表3.14苯乙烯精制塔T-204物料衡算表物質(zhì)名稱<27><33><34>摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）摩爾分率質(zhì)量流量（kg/h）ETHYL-010.0004670.67.066x10-78.134x10-60.0004710.6STYRE-010.9911249.7830.03610.4080.99951249.375H2000000BENZE-012.05x10-361.939x10-330000TOLUE-011.435x10-191.601x10-160000H2O000000NAPHT-010.004557.0590.5067.0341.624x10-50.025NAPHT-00.00417.0590.4587.0591.326x10-82.263x10-5CO2000000METHA-01000000ETHAN-01000000CARBO-01000000由最后模擬結(jié)果可知，苯乙烯摩爾分率99.95%，產(chǎn)量1250kg/h，達(dá)到任務(wù)書要求物料衡算匯總表表3.15物料衡算總表單位：kg/h物質(zhì)名稱<1><2><3><5><6><7><8><9><11><16><19><20><21><22>ETHYL-011493.91719.3972213.3072213.307002213.3071283.718840.837840.8370840.837840.837840.837STYRE-0100.3270.3270.327000.327847.1271250.1151250.11501250.1151250.1151250.115H2000000015.12922.85622.856022.85622.8560BENZE-0115.090.00032415.09015.090015.0936.2646.6546.65046.6546.6546.65TOLUE-0100.2750.2750.275000.27532.9348.52848.528048.52848.52848.528H2O000005987.285987.2795987.285985.6845985.6841801.5287787.2127787.2127787.212NAPHT-0100007.05907.0597.0597.0597.05907.0597.0597.059NAPHT-0200007.05907.0597.0597.0597.05907.0597.0597.059CO2000014.117014.11714.11714.11714.117014.11714.1170METHA-0100000005.6866.986.9806.986.980ETHAN-0100000008.14912.14912.149012.14912.1490CARBO-01000000002.4822.48202.4822.4820（續(xù)表）物質(zhì)名稱<23><22><24><25><26><27><28><29><30><31><32><33><34>ETHYL-010840.837840.8370840.2370.6840.237120.84719.39717.168103.6728.134x10-60.6STYRE-0101250.1151250.11500.3321249.7830.3320.004870.3273.595x10-50.004830.4081249.375H222.856000000000000BENZE-01046.6546.65046.651.939x10-3346.6546.650.00032446.6500.00011200TOLUE-01048.52848.528048.5281.601x10-1648.52848.2530.27548.100.15300H2O07787.21207787.212000000000NAPHT-0107.0597.05903.741x10-517.0593.741x10-5100007.0340.025NAPHT-0207.0597.05904.482x10-707.0594.482x10-7000007.0592.263x10-5CO214.117000000000000METHA-016.98000000000000ETHAN-0112.149000000000000CARBO-012.4820000000000001.2熱量衡算（一）脫氫工段1.設(shè)備：乙苯蒸發(fā)器E-101新鮮乙苯與混合乙苯混合后進(jìn)入乙苯蒸發(fā)器，經(jīng)換熱后變成150℃的乙苯蒸汽。模擬過程所輸入的主要參數(shù)：溫度：150℃、壓力1bar圖3.27乙苯蒸發(fā)器熱量衡算結(jié)果表3.16預(yù)熱器E-101物流相關(guān)物性參數(shù)性質(zhì)單位<3><4>Temperature（溫度）C63.641150Pressure（壓力）bar11MolarEnthalpy（摩爾焓）J/kmol-4254591.52349673500.679MassEnthalpy（質(zhì)量焓）J/kg-40172.672469026.75MolarEntropy（摩爾熵）J/kmol-K-417697.62-282486.693MassEntropy（質(zhì)量熵）J/kg-K-3943.981-2667.294MolarDensity（摩爾密度）kmol/cum7.8330.0284MassDensity（質(zhì)量密度）kg/cum829.5833.01EnthalpyFlow（焓流）Watt-24873.579290405.729AverageMW（平均摩爾質(zhì)量）105.908105.908由aspen運(yùn)行模擬可得Calculatedheatduty（計(jì)算熱負(fù)荷）為315.279KW。2.設(shè)備：原料預(yù)熱器E-102乙苯蒸汽進(jìn)入原料預(yù)熱器與反應(yīng)產(chǎn)物經(jīng)換熱后被預(yù)熱到430℃模擬過程所輸入的主要參數(shù)：冷物流出口溫度：430℃圖3.28原料預(yù)熱器熱量衡算結(jié)果表3.17原料預(yù)熱器E-102物流相關(guān)物性參數(shù)性質(zhì)單位<4><6><11><12>TemperatureC150430603.186534.502Pressurebar110.4580.458MolarEnthalpyJ/kmol49673500.679112313241.943-187551204.573-191153334.194MassEnthalpyJ/kg469026.751060483.238-8325844.376-8485751.484MolarEntropyJ/kmol-K-282486.693-170610.7492959.725-1319.951MassEntropyJ/kg-K-2667.294-1610.94131.389-58.596MolarDensitykmol/cum0.02840.01710.006290.00682MassDensitykg/cum3.011.8120.1420.154EnthalpyFlowkW290.406656.616-19067.374-19433.584AverageMW105.908105.90822.52622.526經(jīng)aspen模擬得原料預(yù)熱器E-102的熱負(fù)荷是366.21KW。3.設(shè)備：第一段脫氫反應(yīng)器R-101從乙苯/蒸汽混合器內(nèi)出來的氣體，首先進(jìn)入第一段反應(yīng)器，發(fā)生負(fù)壓絕熱反應(yīng)，進(jìn)口壓力94.23kpa，出口溫度523℃，壓降是20kpa，則出口壓力73.96kpa。模擬過程所輸入的主要參數(shù)：溫度：523℃、壓力：0.7396bar圖3.29第一段脫氫反應(yīng)器物料衡算結(jié)果表3.18第一段絕熱式反應(yīng)器R-101物流相關(guān)物性參數(shù)性質(zhì)單位<8><9>TemperatureC616.113523Pressurebar0.00950.7396MolarEnthalpyJ/kmol-197427845.214-192993000.621MassEnthalpyJ/kg-8472695.632-8472695.632MolarEntropyJ/kmol-K29645.404-5243.904MassEntropyJ/kg-K1272.244-230.216MolarDensitykmol/cum0.0001280.0106MassDensitykg/cum0.002990.242EnthalpyFlowkW-19403.685-19403.685AverageMW23.301722.778經(jīng)過aspen模擬計(jì)算得第一段反應(yīng)器R-101的熱負(fù)荷是-190.881KW4.設(shè)備：中間預(yù)熱E-103第一段生成氣通過中間預(yù)熱器后溫度再次升高到628℃模擬過程所輸入的主要參數(shù)：溫度：628℃、壓力：73.96kpa圖3.30中間預(yù)熱器熱量衡算結(jié)果表3.19中間預(yù)熱器E-103物流相關(guān)物性參數(shù)性質(zhì)單位<9><10>TemperatureC523628Pressurebar0.73960.7396MolarEnthalpykJ/mol-192.993-189.648MassEnthalpykJ/kg-8472.696-8325.844MolarEntropykJ/mol-K-0.00524-0.0014MassEntropykJ/kg-K-0.23-0.0614MolarDensitykmol/cum0.01060.00987MassDensitykg/cum0.2420.225EnthalpyFlowkW-19403.685-19067.373AverageMW22.77822.778經(jīng)過aspen模擬計(jì)算得中間預(yù)熱器的熱負(fù)荷是541.166KW。5.設(shè)備：第二段脫氫反應(yīng)器R-102經(jīng)加熱后的反應(yīng)器進(jìn)入第二段反應(yīng)器R-102，其出口壓力119.2kpa，溫度為583℃模擬過程所輸入的主要參數(shù)：溫度：583℃壓力：1.192bar圖3.31第二段脫氫反應(yīng)器熱量衡算結(jié)果表3.20第二段脫氫反應(yīng)器R-102物流相關(guān)物性參數(shù)性質(zhì)單位<10><11>TemperatureC628603.186Pressurebar0.73961.192MolarEnthalpykJ/mol-189.648-187.551MassEnthalpykJ/kg-8325.844-8325.844MolarEntropykJ/mol-K-0.0014-0.00499MassEntropykJ/kg-K-0.0614-0.222MolarDensitykmol/cum0.009870.0164MassDensitykg/cum0.2250.369EnthalpyFlowkW-19067.373-19067.374AverageMW22.77822.526經(jīng)過aspen模擬計(jì)算得第二段反應(yīng)器R-102的熱負(fù)荷是-100.09KW。6.設(shè)備：第二段廢熱鍋爐E-104反應(yīng)的生成氣要經(jīng)過三段廢熱鍋爐進(jìn)行降溫，同時(shí)回收熱量模擬過程所輸入的主要參數(shù)：熱物流出口溫度：400℃圖3.32第二段廢熱鍋爐熱量衡算結(jié)果表3.21第二段廢熱鍋爐E-104物流相關(guān)物性參數(shù)性質(zhì)單位<12><13><14><15>TemperatureC534.502400100100.018Pressurebar1.1921.1921.013251.01325MolarEnthalpykJ/mol-191.153-197.913-279.978-263.484MassEnthalpykJ/kg-8485.751-8785.837-15541.145-14625.603MolarEntropykJ/mol-K-0.00927-0.0184-0.146-0.102MassEntropykJ/kg-K-0.412-0.818-8.099-5.645MolarDensitykmol/cum0.01780.021350.9730.0805MassDensitykg/cum0.40.48918.2921.45466EnthalpyFlowkW-19433.584-20120.824-11665.754-10978.514AverageMW22.52622.52618.01518.015經(jīng)過aspen模擬計(jì)算得第二段廢熱鍋爐E-104的熱負(fù)荷是544.955KW。7.設(shè)備：第三段廢熱鍋爐E-105經(jīng)過三段廢熱鍋爐降溫后的反應(yīng)器為120℃。同時(shí)，三段冷卻器回收的熱量可以分別用于預(yù)熱循環(huán)乙苯原料、產(chǎn)生蒸汽等模擬過程所輸入的主要參數(shù)：熱物流出口溫度：120℃圖3.33第三段廢熱鍋爐熱量衡算結(jié)果表3.22第三段廢熱鍋爐E-105物流相關(guān)物性參數(shù)性質(zhì)單位<13><16><17><18>TemperatureC400120100100.018Pressurebar1.1921.1921.013251.01325MolarEnthalpykJ/mol-197.913-210.573-279.978-249.089MassEnthalpykJ/kg-8785.837-9347.827-15541.145-13826.553MolarEntropykJ/mol-K-0.0184-0.0426-0.146-0.0631MassEntropykJ/kg-K-0.818-1.889-8.099-3.504MolarDensitykmol/cum0.02130.036550.9730.043MassDensitykg/cum0.480.821918.2920.775EnthalpyFlowkW-20120.824-21407.86-11665.754-10378.718AverageMW22.52622.52618.01518.015經(jīng)過aspen模擬計(jì)算得第三段廢熱鍋爐E-105的熱負(fù)荷是1239.19KW8.設(shè)備：冷卻器E-106換熱后的反應(yīng)氣送至氣液混合器與20℃的循環(huán)水混合，使反應(yīng)器迅速降溫冷凝。得到的氣液混合物經(jīng)過冷卻器被冷卻到60℃。模擬過程所輸入的主要參數(shù)：溫度：60℃、壓力：1bar圖3.34冷卻器熱量衡算結(jié)果表3.23冷卻器E-106物流相關(guān)物性參數(shù)性質(zhì)單位<20><21>TemperatureC97.31660Pressurebar1.013251.01325MolarEnthalpykJ/mol-226.796-257.657MassEnthalpykJ/kg-10520.097-11951.634MolarEntropykJ/mol-K-0.0672-0.152MassEntropykJ/kg-K-3.117-7.046MolarDensitykmol/cum0.04260.41MassDensitykg/cum0.9188.831EnthalpyFlowkW-29357.039-33351.841AverageMW21.55821.558經(jīng)過aspen模擬計(jì)算得冷卻器E-106的熱負(fù)荷是-3780.9KW9.設(shè)備：氣液分離器SEP1冷卻后的氣液混合物在氣液分離器中進(jìn)行氣液分離，得到的氣體直接燃燒，液體則進(jìn)入分相器進(jìn)行進(jìn)一步分離。圖3.35氣液分離器熱量衡算結(jié)果表3.24氣液分離器SEP1物流相關(guān)物性參數(shù)性質(zhì)單位<21><22><23>TemperatureC606060Pressurebar1.013251.013251.01325MolarEnthalpykJ/mol-257.657-264.696-15.017MassEnthalpykJ/kg-11951.634-12016.594-3226.244MolarEntropykJ/mol-K-0.152-0.157-0.000585MassEntropykJ/kg-K-7.046-7.149-0.126MolarDensitykmol/cum0.410.6430.0366MassDensitykg/cum8.83114.1740.17EnthalpyFlowkW-33351.841-33337.566-52.501AverageMW21.55822.0284.655經(jīng)過aspen模擬計(jì)算得氣液分離器SEP1的熱負(fù)荷是-38.1526KW10.設(shè)備：分相器SEP2液體進(jìn)入分相器進(jìn)行進(jìn)一步分離。分離后，水層可以作為循環(huán)水，而油層進(jìn)入脫乙苯塔。圖3.36分相器熱量衡算結(jié)果表3.25分相器SEP2物流相關(guān)物性參數(shù)性質(zhì)單位<22><24><25>TemperatureC606060Pressurebar1.013251.013251.01325MolarEnthalpykJ/mol-264.69662.166-283.156MassEnthalpykJ/kg-12016.594597.612-15717.522MolarEntropykJ/mol-K-0.157-0.343-0.155MassEntropykJ/kg-K-7.149-3.297-8.592MolarDensitykmol/cum0.6438.20253.262MassDensitykg/cum14.174853.209959.522EnthalpyFlowkW-33337.566365.249-33998.798AverageMW22.028104.02418.015經(jīng)過aspen模擬計(jì)算得分相器SEP2的熱負(fù)荷是-296.192KW（二）精制工段1.設(shè)備：脫乙苯塔T-201脫氫液進(jìn)入乙苯/苯乙烯精餾塔圖3.37脫乙苯塔熱量衡算結(jié)果表3.26脫乙苯塔塔T-201性質(zhì)單位<24><26><27>TemperatureC6094.824112.479Pressurebar1.013250.38660.3866MolarEnthalpykJ/mol62.1666.879119.931MassEnthalpykJ/kg597.61266.4681148.575MolarEntropykJ/mol-K-0.343-0.38-0.279MassEntropykJ/kg-K-3.297-3.673-2.674MolarDensitykmol/cum8.2027.7277.86MassDensitykg/cum853.209799.666820.673EnthalpyFlowkW365.24917.277403.437AverageMW104.024103.497104.418經(jīng)aspen模擬計(jì)算得脫乙苯塔T-201塔頂?shù)臒嶝?fù)荷是1708.51KW，塔釜熱負(fù)荷是1763.98KW2.設(shè)備：乙苯回收塔T-202圖3.38乙苯回收塔熱量衡算結(jié)果表3.27脫乙苯塔T-202物流相關(guān)物性參數(shù)性質(zhì)溫度<28><29><30>TemperatureC94.971108.288135.66Pressurebar1.111MolarEnthalpykJ/mol6.9124.99111.096MassEnthalpykJ/kg66.769261.684104.524MolarEntropykJ/mol-K-0.38-0.316-0.378MassEntropykJ/kg-K-3.672-3.307-3.557MolarDensitykmol/cum7.7258.2037.165MassDensitykg/cum799.526783.4187