年产25万吨苯酚联产16万吨丙酮项目设计说明书.doc

年产25万吨苯酚联产16万吨丙酮项目设计说明书附录附录一 物料衡算一览表1.1 丙烷脱氢工段1.1.1移动床反应器（R0101）项目INOUT温度/600600压力/bar2.02.0气相分率1.0001.000液相分率0.0000.000摩尔流量kmol/hr979.3581238.709质量流量kg/hr22292.08222292.082体积流量cum/hr35570.28944989.910密度kg/m0.6260.495焓Gcal/hr-1.6225.517质量流量kg/hr丙烷20882.0829572.256氢气10001499.520丙烯41011096.175甲烷044.624乙烯079.156乙烷00.351质量分率%丙烷93.742.940氢气4.56.734丙烯1.849.771甲烷00.200乙烯00.355乙烷00总质量流量kg/hr22292.08222292.0821.1.2移动床反应器（R0102）项目INOUT温度/600600压力/bar2.02.0气相分率1.0001.000液相分率0.0000.000摩尔流量kmol/hr1238.7091361.37质量流量kg/hr22292.08222292.082体积流量cum/hr44989.91049444.958密度kg/m0.4950.451焓Gcal/hr5.5178.632质量流量kg/hr丙烷9572.2564400.848氢气1499.5201735.146丙烯11096.17515914.706甲烷44.62483.760乙烯79.156147.135乙烷0.3510.487质量分率%丙烷42.94019.7氢气6.7347.8丙烯49.77171.4甲烷0.2000.4乙烯0.3550.7乙烷00总质量流量kg/hr22292.08222292.0821.1.3移动床反应器（R0103）项目INOUT温度/600600.0压力/bar2.02.0气相分率1.0001.000液相分率0.0000.000摩尔流量kmol/hr1361.371408.846质量流量kg/hr22292.08222292.082体积流量cum/hr49444.95851169.704密度kg/m0.4510.436焓Gcal/hr8.63211.635质量流量kg/hr丙烷4400.8481942.274氢气1735.1461846.101丙烯15914.70618072.852甲烷83.760156.734乙烯147.135273.511乙烷0.4870.609质量分率%丙烷19.78.7氢气7.88.3丙烯71.481.1甲烷0.40.7乙烯0.71.2乙烷00总质量流量kg/hr22292.08222292.0821.1.4急冷塔（T0201）项目INOUT温度/20.0600.025.025.0压力/bar2.02.02.02.0气相分率0.0001.0001.0000.000液相分率1.0000.0000.0001.000摩尔流量kmol/hr1110.1691408.8461427.7181091.297总质量流量kg/hr20000.00022292.08222632.05119660.031体积流量cum/hr20.02551168.70417639.97919.780密度kg/m998.7520.4351.283993.934焓Gcal/hr-76.40411.635-0.179-74.999质量流量kg/hr丙烷01942.2741942.2740氢气01846.1011846.1010丙烯018072.85218072.8420.012甲烷0156.734156.7340乙烯0273.511273.5100乙烷00.6090.6090水200000339.98219660.017质量分率%丙烷08.78.60氢气08.38.20丙烯081.179.90甲烷00.70.70乙烯01.21.20乙烷0000水10001.5100总质量流量kg/hr42292.08242292.0821.1.5闪蒸罐（V0201）项目INOUT温度/25.025.025.0压力/bar2.02.02.0气相分率1.0001.0000.975液相分率0.0000.0000.025摩尔流量kmol/hr1427.718925.549502.169总质量流量kg/hr22632.0512002.83520629.216体积流量cum/hr17639.97911482.7665891.976密度kg/m1.2830.17430.124焓Gcal/hr-0.179-0.174-0.153质量流量kg/hr丙烷1942.27401942.274氢气1846.1011846.1010丙烯18072.842018072.842甲烷156.734156.7340乙烯273.5100273.510乙烷0.60900水339.9820339.982质量分率%丙烷8.609.4氢气8.292.20丙烯79.9087.6甲烷0.77.80乙烯1.201.3乙烷000水1.501.7总质量流量kg/hr22632.05122632.0511.1.6脱乙烷塔（T0202）项目INOUT温度/-109.0-85.9-31.0压力/bar2.02.02.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr502.16910.616491.553总质量流量kg/hr20629.216333.31620295.900体积流量cum/hr30.1240.57834.044密度kg/m684.809576.671596.167焓Gcal/hr-3.3490.060-2.650质量流量kg/hr丙烷1942.2746.5941935.680氢气000丙烯18072.84299.27217973.570甲烷000乙烯273.510227.26446.246乙烷00.1870.423水339.9820339.982质量分率%丙烷9.42.09.5氢气000丙烯87.629.888.6甲烷000乙烯1.368.20.2乙烷000水1.701.7总质量流量kg/hr20629.21620629.2161.2 异丙苯生产工段1.2.1烷烃化反应器（R0301）项目INOUT温度/120.027.6120.0压力/bar2.12.12.1气相分率1.0001.0000.075液相分率0.0000.0000.925摩尔流量kmol/hr427.600471.019471.496质量流量kg/hr33401.39319909.25053310.642体积流量cum/hr6347.2345435.947604.011密度kg/m5.2623.6688.261焓Gcal/hr9.3640.962-2.890质量流量kg/hr丙烷01935.6801935.682丙烯017973.5700苯33401.3930704.614异丙苯0049284.124二异丙苯001386.224质量分率%丙烷09.73.6丙烯090.30苯10001.3异丙苯0092.4二异丙苯002.6总质量流量kg/hr53310.64253310.6421.2.2 精馏塔（T0301）项目INOUT温度/-50.0174.7-24.2压力/bar2.12.12.1气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr471.496429.06242.435质量流量kg/hr53310.64251439.4211871.222体积流量cum/hr59.45271.5593.339密度kg/m896.701718.839560.414焓Gcal/hr-6.749-0.481-1.280质量流量kg/hr丙烷1935.68264.4581871.222丙烯000苯704.614704.6140异丙苯49284.12449284.1240二异丙苯1386.2241386.2240质量分率%丙烷3.60.1100丙烯000苯1.31.40异丙苯92.495.80二异丙苯2.62.70总质量流量kg/hr53310.64253310.6421.2.3 精馏塔（T0302）项目INOUT温度/25.0183.960.9压力/bar2.12.12.1气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr429.062410.62918.432质量流量kg/hr51439.42149714.7591724.662体积流量cum/hr60.05969.9802.141密度kg/m856.481710.414805.504焓Gcal/hr-4.056-0.3420.017质量流量kg/hr丙烷64.458064.458丙烯000苯704.6140704.614异丙苯49284.12448328.538955.586二异丙苯1386.2241386.2210.003质量分率%丙烷0.103.7丙烯000苯1.4040.9异丙苯95.897.255.4二异丙苯2.72.80总质量流量kg/hr51439.42151439.4211.2.4 精馏塔（T0303）项目INOUT温度/80.0239.3183.2压力/bar2.12.12.1气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr410.6298.987401.642质量流量kg/hr49714.7591438.81448275.944体积流量cum/hr61.3182.13667.910密度kg/m810.769673.602710.881焓Gcal/hr-2.913-0.112-0.203质量流量kg/hr丙烷000丙烯000苯000异丙苯48328.53855.91548272.623二异丙苯1386.2211382.8993.322质量分率%丙烷000丙烯000苯000异丙苯97.23.9100二异丙苯2.896.10总质量流量kg/hr49714.75949714.7591.2.5 异构化反应器（R0302）项目INOUT温度/60.9239.3180.0压力/bar2.12.135.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr18.4328.98727.420质量流量kg/hr1724.6621438.8143163.476体积流量cum/hr2.1412.1364.514密度kg/m805.504673.602700.814焓Gcal/hr0.017-0.112-0.044质量流量kg/hr丙烷64.458064.458丙烯000苯704.614039.598异丙苯955.58655.9153058.038二异丙苯0.0031382.8991.383质量分率%丙烷3.702.0丙烯000苯40.901.3异丙苯55.43.996.7二异丙苯096.10总质量流量kg/hr3163.4763163.4761.3 过氧化氢异丙苯制作工段1.3.1鼓泡式反应器（R0401）项目INOUT温度/130.1244.0110.0110.0压力/bar4.54.54.54.5气相分率0.0001.0001.0000.000液相分率1.0000.0000.0001.000摩尔流量kmol/hr438.1552043.9701618.901498.617总质量流量kg/hr52508.89559002.68945418.69166092.893体积流量cum/hr68.73119554.80011465.69468.958密度kg/m763.9773.0173.961958.451焓Gcal/hr-1.7263.1510.916-14.654质量流量kg/hr丙烷64.458064.4580水000750.134苯39.5980039.598异丙苯52378.225001047.564氧气014002.675354.2190过氧化氢异丙苯00058659.069氮气045000.01445000.0140氨水0000甲醛000609.099六次甲基四氨0000丙酮21.9100021.910-甲基苯乙烯0002523.488苯乙酮0002437.327二异丙苯4.704004.704质量分率%丙烷0.100.10水0001.1苯0000异丙苯99.8001.6氧气00.80.80过氧化氢异丙苯00088.8氮气099.199.10氨水0000甲醛0000.9六次甲基四氨0000丙酮0.1000-甲基苯乙烯0003.8苯乙酮0003.7二异丙苯0000总质量流量kg/hr111511.584111511.5841.3.2去甲醇反应器（R0402）项目INOUT温度/25.0110.0100.0100.0压力/bar1.01.01.01.0气相分率1.0000.0000.0000.940液相分率0.0001.0001.0000.060摩尔流量kmol/hr13.200498.617435.78066.137总质量流量kg/hr224.80366092.89364667.4481650.249体积流量cum/hr324.49968.95867.7841912.315密度kg/m0.693958.451954.0630.863焓Gcal/hr-0.145-14.654-11.710-3.413质量流量kg/hr丙烷0000水0750.13401106.836苯039.598039.598异丙苯01047.5641047.5640氧气0000过氧化氢异丙苯058659.06958659.0690氮气0000氨水224.803000甲醛0609.099014.579六次甲基四氨000462.621丙酮021.910021.910-甲基苯乙烯02523.4882523.4880苯乙酮02437.3272437.3270二异丙苯04.70404.704质量分率%丙烷0000水01.1067.1苯0002.4异丙苯01.61.60氧气0000过氧化氢异丙苯088.890.70氮气0000氨水100000甲醛00.900.9六次甲基四氨00028.0丙酮0001.3-甲基苯乙烯03.83.90苯乙酮03.73.80二异丙苯0000.3总质量流量kg/hr66317.69666317.6961.4 苯酚、丙酮制作工段1.4.1反应精馏塔（T0501）项目INOUT温度/140140140压力/bar1.01.01.0气相分率0.0001.0000.000液相分率1.0000.0001.000摩尔流量kmol/hr435.780394.141427.064质量流量kg/hr64667.44823433.08341234.364体积流量cum/hr71.27713327.31843.346密度kg/m907.2691.758951.284焓Gcal/hr-10.343-18.926-12.116质量流量kg/hr异丙苯1047.5641047.5640过氧化氢异丙苯58659.06900苯酚0036273.550丙酮022385.5190-甲基苯乙烯2523.48802523.488苯乙酮2437.32702437.327质量分率%异丙苯1.64.50过氧化氢异丙苯90.700苯酚0088.0丙酮095.50-甲基苯乙烯3.906.1苯乙酮3.805.9总质量流量kg/hr64667.44864667.4481.4.2精馏塔（T0502）项目INOUT温度/5056.6138.5压力/bar1.01.01.0气相分率1.0000.0000.000液相分率0.0001.0001.000摩尔流量kmol/hr394.141385.0489.093质量流量kg/hr23433.08322363.6091069.474体积流量cum/hr30.68529.8121.474密度kg/m763.666750.155725.559焓Gcal/hr-22.571-22.403-0.050质量流量kg/hr异丙苯1047.56401047.564过氧化氢异丙苯000苯酚000丙酮22385.51922363.60921.910-甲基苯乙烯000苯乙酮000质量分率%异丙苯4.5098.0过氧化氢异丙苯000苯酚000丙酮95.51002.0-甲基苯乙烯000苯乙酮000总质量流量kg/hr1.4.3精馏塔（T0503）项目INOUT温度/140165.6182.1压力/bar1.01.01.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr427.06429.040398.024质量流量kg/hr41234.3643246.94937987.416体积流量cum/hr43.3464.07241.070密度kg/m951.284797.384924.943焓Gcal/hr-12.1160.306-11.595质量流量kg/hr异丙苯000过氧化氢异丙苯000苯酚36273.550723.46235550.088丙酮000-甲基苯乙烯2523.4882523.4870.001苯乙酮2437.32702437.327质量分率%异丙苯000过氧化氢异丙苯000苯酚88.022.393.6丙酮000-甲基苯乙烯6.177.70苯乙酮5.906.4总质量流量kg/hr41234.36441234.3641.4.4精馏塔（T0504）项目INOUT温度/150.0181.7200.7压力/bar1.01.01.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr398.024377.38120.643质量流量kg/hr37987.41635521.6912465.725体积流量cum/hr39.66538.0982.862密度kg/m957.706932.377861.539焓Gcal/hr-12.220-11.074-0.523质量流量kg/hr异丙苯000过氧化氢异丙苯000苯酚35550.08835497.49752.591丙酮000-甲基苯乙烯0.0010.0010苯乙酮2437.32724.1932413.134质量分率%异丙苯000过氧化氢异丙苯000苯酚93.699.92.1丙酮000-甲基苯乙烯000苯乙酮6.40.197.9总质量流量kg/hr37987.41637987.416附录二 能量衡算一览表2.1 反应器能量衡算2.1.1移动床反应器表2-1 移动床反应器焓变计算表项目INOUT温度/600600.0压力/bar2.02.0气相分率1.0001.000液相分率0.0000.000摩尔流量kmol/hr979.3581408.846质量流量kg/hr22292.08222292.082体积流量cum/hr35570.28951169.704密度kg/m0.6260.436焓Gcal/hr-1.62211.635总焓Gcal/hr-1.62211.635表2-2 移动床反应器热负荷计算表热负荷热负荷Gcal/hr13.2569925Q=13.2569925 Gcal/hr表2-3 移动床反应器能量平衡表Q总W总HinHoutError13.25699250-1.62216311.634829502.1.2烷烃化反应器（R0301）表2-4 烷烃化反应器焓变计算表项目INOUT温度/120.027.6120.0压力/bar2.12.12.1气相分率1.0001.0000.075液相分率0.0000.0000.925摩尔流量kmol/hr427.600471.019471.496质量流量kg/hr33401.39319909.25053310.642体积流量cum/hr6347.2345435.947604.011密度kg/m5.2623.6688.261焓Gcal/hr9.3640.962-2.890总焓Gcal/hr10.326-2.890表2-5 烷烃化反应器热负荷计算表热负荷热负荷Gcal/hr-13.215421Q=-13.215421 Gcal/hr表2-6 烷烃化反应器能量平衡表Q总W总HinHoutError-13.215421010.3254081-2.8900131E-072.1.3 异构化反应器（R0302）表2-7 异构化反应器焓变计算表项目INOUT温度/60.9239.3180.0压力/bar2.12.135.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr18.4328.98727.420质量流量kg/hr1724.6621438.8143163.476体积流量cum/hr2.1412.1364.514密度kg/m805.504673.602700.814焓Gcal/hr0.017-0.112-0.044总焓Gcal/hr-0.095-0.044表2-8 异构化反应器热负荷计算表热负荷热负荷Gcal/hr0.05188286Q=0.05188286 Gcal/hr表2-9 异构化反应器能量平衡表Q总W总HinHoutError0.051882860-0.0958295-0.04394676E-082.1.4鼓泡式反应器（R0401）表2-10鼓泡式反应器焓变计算表项目INOUT温度/130.1244.0110.0110.0压力/bar4.54.54.54.5气相分率0.0001.0001.0000.000液相分率1.0000.0000.0001.000摩尔流量kmol/hr438.1552043.9701618.901498.617总质量流量kg/hr52508.89559002.68945418.69166092.893体积流量cum/hr68.73119554.80011465.69468.958密度kg/m763.9773.0173.961958.451焓Gcal/hr-1.7263.1510.916-14.654总焓Gcal/hr1.425-13.738表2-11 鼓泡式反应器热负荷计算表热负荷热负荷Gcal/hr-14.422029Q=-14.422029 Gcal/hr表2-12 鼓泡式反应器能量平衡表Q总W总HinHoutError-14.42202901.4250184-12.9970114E-072.1.5去甲醇反应器（R0402）表2-13 去甲醇反应器焓变计算表项目INOUT温度/25.0110.0100.0100.0压力/bar1.01.01.01.0气相分率1.0000.0000.0000.940液相分率0.0001.0001.0000.060摩尔流量kmol/hr13.200498.617435.78066.137总质量流量kg/hr224.80366092.89364667.4481650.249体积流量cum/hr324.49968.95867.7841912.315密度kg/m0.693958.451954.0630.863焓Gcal/hr-0.145-14.654-11.710-3.413总焓Gcal/hr-14.799-15.123表2-14 去甲醇反应器热负荷计算表热负荷热负荷Gcal/hr-0.7600096Q=-0.7600096 Gcal/hr表2-15 去甲醇反应器能量平衡表Q总W总HinHoutError-0.76000960-14.799298-15.5593076E-072.2 塔设备能量衡算2.2.1脱乙烷塔（T0202）表2-16 脱乙烷塔焓变计算表项目INOUT温度/-109.0-85.9-31.0压力/bar2.02.02.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr502.16910.616491.553总质量流量kg/hr20629.216333.31620295.900体积流量cum/hr30.1240.57834.044密度kg/m684.809576.671596.167焓Gcal/hr-3.3490.060-2.650总焓Gcal/hr-3.349-2.590表2-17 脱乙烷塔热负荷计算表冷凝器再沸器热负荷Gcal/hr-0.05634340.81575469Q=0.75941129 Gcal/hr表2-18 脱乙烷塔能量平衡表Q总W总HinHoutError0.759411290-3.3488092-2.58940254.59E-062.2.2 精馏塔（T0301）项目INOUT温度/-50.0174.7-24.2压力/bar2.12.12.1气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr471.496429.06242.435质量流量kg/hr53310.64251439.4211871.222体积流量cum/hr59.45271.5593.339密度kg/m896.701718.839560.414焓Gcal/hr-6.749-0.481-1.280总焓Gcal/hr-6.749-1.761表2-19 精馏塔焓变计算表表2-20 精馏塔热负荷计算表冷凝器再沸器热负荷Gcal/hr-0.20501915.19250828Q=4.98748918 Gcal/hr表2-21 精馏塔能量平衡表Q总W总HinHoutError4.987489180-6.7490344-1.76154574.8E-072.2.3 精馏塔（T0302）表2-22 精馏塔焓变计算表项目INOUT温度/25.0183.960.9压力/bar2.12.12.1气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr429.062410.62918.432质量流量kg/hr51439.42149714.7591724.662体积流量cum/hr60.05969.9802.141密度kg/m856.481710.414805.504焓Gcal/hr-4.056-0.3420.017总焓Gcal/hr-4.0560.325表2-23 精馏塔热负荷计算表冷凝器再沸器热负荷Gcal/hr-0.24880543.98015074Q=3.73134534 Gcal/hr表2-24 精馏塔能量平衡表Q总W总HinHoutError3.731345340-4.0563758-0.32506983.934E-052.2.4 精馏塔（T0303）表2-25 精馏塔焓变计算表项目INOUT温度/80.0239.3183.2压力/bar2.12.12.1气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr410.6298.987401.642质量流量kg/hr49714.7591438.81448275.944体积流量cum/hr61.3182.13667.910密度kg/m810.769673.602710.881焓Gcal/hr-2.913-0.112-0.203总焓Gcal/hr-2.913-0.315表2-26 精馏塔热负荷计算表冷凝器再沸器热负荷Gcal/hr-5.21770627.81532637Q=2.59762017 Gcal/hr表2-27 精馏塔能量平衡表Q总W总HinHoutError2.597620170-2.9132914-0.31567152.7E-072.2.5 精馏塔（T0502）表2-28 精馏塔焓变计算表项目INOUT温度/140140140压力/bar1.01.01.0气相分率0.0001.0000.000液相分率1.0000.0001.000摩尔流量kmol/hr435.780394.141427.064质量流量kg/hr64667.44823433.08341234.364体积流量cum/hr71.27713327.31843.346密度kg/m907.2691.758951.284焓Gcal/hr-10.343-18.926-12.116总焓Gcal/hr-10.343-31.042表2-29 精馏塔热负荷计算表冷凝器再沸器热负荷Gcal/hr-2.99648363.11488859Q=0.11840499 Gcal/hr表2-30 精馏塔能量平衡表Q总W总HinHoutError0.118404990-22.571143-22.4527381E-082.2.6 精馏塔（T0503）表2-31 精馏塔焓变计算表项目INOUT温度/140165.6182.1压力/bar1.01.01.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr427.06429.040398.024质量流量kg/hr41234.3643246.94937987.416体积流量cum/hr43.3464.07241.070密度kg/m951.284797.384924.943焓Gcal/hr-12.1160.306-11.595总焓Gcal/hr-12.116-11.289表2-32 精馏塔热负荷计算表冷凝器再沸器热负荷Gcal/hr-3.02402173.85108169Q=0.82705999 Gcal/hr表2-33 精馏塔能量平衡表Q总W总HinHoutError0.827059990-12.116117-11.2890571E-082.2.7 精馏塔（T0504）表2-34 精馏塔焓变计算表项目INOUT温度/150.0181.7200.7压力/bar1.01.01.0气相分率0.0000.0000.000液相分率1.0001.0001.000摩尔流量kmol/hr398.024