12-附录六能量衡算

川维化工年产12万吨醋酸乙烯酯项目能量衡算 附录六：能量衡算指导老师：任艳群 李文生 罗伟平 夏新年 梁志武团队成员：彭裕 孔昕山 刘永炜 赵孟超 徐志成APEX团队目录1.1能量衡算的意义11.2能量衡算的原则11.3醇解母液回收工段能量衡算11.3.1 T0101醇解母液回收塔11.3.2 T0102乙醛脱除塔21.3.3 T0103乙醛精制塔31.3.4 T0104醋酸脱除塔31.3.5 T0105萃取精馏塔41.3.6 T0106醋酸甲酯粗分塔51.3.7 E0116 EDA一工段冷却器61.3.8 E0108醋酸脱除塔第二再沸器61.3.9 E0110醋酸脱除塔第四再沸器71.4 EDA合成工段81.4.1 E0201醋酸甲酯汽化后加热器81.4.2 R0201 EDA合成反应器81.4.3 V0201不凝汽气液分离器91.4.4 T0201 EDA精制塔101.4.5 T0202醋酸精制低压塔101.4.6 T0203醋酸精制高压塔111.5 EDA裂解制VAC工段121.5.1 E0301 EDA加热器121.5.2 T0301 EDA裂解反应精馏塔131.5.3 T0302 EDA回收精馏塔131.5.4 T0303酸酐回收精馏塔14APEX团队15APEX团队1.1能量衡算的意义在全工艺段中伴随着物料从一个体系或单元进入另一个体系或单元，在发生质量传递的同时也伴随着能量的消耗、释放和转化。其中的能量变换数量关系可以从能量衡算求得，对于新设计的车间，可以由此确定设备的热负荷。再根据设备的热负荷大小、所处理物料的性质及工艺要求选择恰当的设备。总之，通过下述能量衡算，可以为后续设计工作中提高热量的利用率，降低能耗提供主要依据。 1.2能量衡算的原则工程依据化工设计中关于热量衡算的基本思想和要求，遵循基本规范与实际工艺相结合的原则，并进行了该热量衡算书的编制。其中一个主要依据是能量平衡方程：其中，Qin表示输入设备热量的总和；Qout表示输出设备热量的总和；Qi表示损失热量的总和。对于连续系统：其中， Q设备的热负荷；W输入系统的机械能；Hout离开设备的各物料焓之和；Hin进入设备的各物料焓之和。1.3醇解母液回收工段能量衡算1.3.1 T0101醇解母液回收塔表1-1 T0101物流焓变表INOUT流股编号1-11-21-3Temperature C3554.9577629366.17530011Pressure bar4.511.061.06Vapor Frac000Mole Flow kmol/hr1775.566443474.62230181300.944141Mass Flow kg/hr6760026505.9643441094.04142Volume Flow cum/hr81.792682830.6607805255.19732451Enthalpy Gcal/hr-114.2024225-39.68905211-73.2718756表1-2 T0101热负荷表冷凝器再沸器QH Gcal/hr-8.77629596410.017789731.241493768表1-3 T0101热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError1.241493768-114.2024225-112.96092771.08E-061.3.2 T0102乙醛脱除塔表1-4 T0102物流焓变表INOUT流股编号1-21-71-41-5Temperature C54.9577629355.0123566553.3913176955.1444754Pressure bar1.061.061.061.06Vapor Frac0000Mole Flow kmol/hr474.622301854.6300720456.89672196472.3556519Mass Flow kg/hr26505.964343280.6170663380.47912426406.10229Volume Flow cum/hr30.660780523.7551730913.87880615630.53559553Enthalpy Gcal/hr-39.68905211-4.841890632-4.94969631-39.58145382表1-5 T0102热负荷表冷凝器再沸器QH Gcal/hr-2.682710232.6825031-0.00020713表1-6 T0102热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-0.00020713-44.53094274-44.53115013-2.52E-071.3.3 T0103乙醛精制塔表1-7 T0103物流焓变表INOUT流股编号1-41-61-7Temperature C53.3913176922.1589629755.01235665Pressure bar1.061.061.06Vapor Frac000Mole Flow kmol/hr56.896721962.26664962354.63007204Mass Flow kg/hr3380.47912499.862057763280.617066Volume Flow cum/hr3.8788061560.1279397713.755173091Enthalpy Gcal/hr-4.94969631-0.106676966-4.841890632表1-8 T0103热负荷表冷凝器再沸器QH Gcal/hr-0.4339975250.4351262330.001128708表1-9 T0103热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError0.001128708-4.94969631-4.9485675974.95E-091.3.4 T0104醋酸脱除塔表1-10 T0104物流焓变表INOUT流股编号1-51-81-91-10Temperature C55.144475477.259.41041621101.8200919Pressure bar1.063.311Vapor Frac0010Mole Flow kmol/hr472.3556519765.8378471800438.193499Mass Flow kg/hr26406.102292787640580.7279613701.37433Volume Flow cum/hr30.5355955331.6364113421316.2375915.26514457Enthalpy Gcal/hr-39.58145382-60.48593903-58.02925206-35.67350759表1-11 T0104热负荷表冷凝器（无）再沸器QH Gcal/hr06.3646320246.364632024表1-12 T0104热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError6.364632024-100.0673928-93.702759641.18E-061.3.5 T0105萃取精馏塔表1-13 T0105物流焓变表INOUT流股编号1-91-111-121-13Temperature C59.410416212575.0406820986.50535563Pressure bar11.013250.980.98Vapor Frac1010Mole Flow kmol/hr8002941.9470586403101.947058Mass Flow kg/hr40580.727965300033066.1380760514.58989Volume Flow cum/hr21316.2375953.3222262118905.9411268.43157219Enthalpy Gcal/hr-58.02925206-200.8237674-51.81289559-204.5068923表1-14 T0105热负荷表冷凝器（无）再沸器QH Gcal/hr02.5332843462.533284346表1-15 T0105热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError2.533284346-258.8530195-256.3197879-5.28E-051.3.6 T0106醋酸甲酯粗分塔表1-16 T0106物流焓变表INOUT流股编号1-121-141-15Temperature C75.0406820955.5498480492.31012676Pressure bar0.980.980.98Vapor Frac100Mole Flow kmol/hr640420220Mass Flow kg/hr33066.1380729050.53344015.604667Volume Flow cum/hr18905.9411232.550432484.347948998Enthalpy Gcal/hr-51.81289559-42.44150018-14.75950106表1-17 T0106热负荷表冷凝器再沸器QH Gcal/hr-9.2892244323.90117132-5.388053112表1-18 T0106热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-5.388053112-51.81289559-57.20100124-5.25E-051.3.7 E0116 EDA一工段冷却器表1-19 E0116物流焓变表INOUT流股编号2-62-10Temperature C17063Pressure bar360.92Vapor Frac10.06148756Mole Flow kmol/hr448.8507259448.8507259Mass Flow kg/hr40114.6675740114.66757Volume Flow cum/hr363.9880078874.7188478Enthalpy Gcal/hr-57.3074383-61.73182673表1-20 E0116热负荷表H Gcal/hr-4.424388444表1-21 E0116热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-4.424388444-57.3074383-61.731826731.03E-081.3.8 E0108醋酸脱除塔第二再沸器表1-22 E0108物流焓变表INOUT流股编号3-163-18Temperature C168.581267480Pressure bar1.013251.01325Vapor Frac00Mole Flow kmol/hr100.213175100.2087454Mass Flow kg/hr14638.3894714637.74243Volume Flow cum/hr16.2458762814.49917118Enthalpy Gcal/hr-19.80059291-20.39850156表1-23 E0108热负荷表H Gcal/hr-0.598810331表1-24 E0108热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-0.598810331-19.80059291-20.398501569.02E-041.3.9 E0110醋酸脱除塔第四再沸器表1-25 E0110物流焓变表INOUT流股编号3-203-22Temperature C139.597699680Pressure bar1.013251.01325Vapor Frac00Mole Flow kmol/hr1128.037711128.034423Mass Flow kg/hr115160.7343115160.3987Volume Flow cum/hr123.9040622114.1933451Enthalpy Gcal/hr-162.1045028-165.1863886表1-26 E0110热负荷表H Gcal/hr-3.082367059表1-27 E0110热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-3.082367059-162.1045028-165.18638864.81E-041.4 EDA合成工段1.4.1 E0201醋酸甲酯汽化后加热器表1-28 E0201物流焓变表INOUT流股编号2-22-4Temperature C8.830817395170Pressure bar0.981.01325Vapor Frac0.6693338421Mole Flow kmol/hr997.0899997.0899Mass Flow kg/hr40114.6675740114.66757Volume Flow cum/hr15963.9361636184.29332Enthalpy Gcal/hr-52.49705784-47.7227733表1-29 E0201热负荷表H Gcal/hr4.77428454表1-30 E0201热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError4.77428454-52.49705784-47.7227733-4.45E-091.4.2 R0201 EDA合成反应器表1-31 R0201物流焓变表INOUT流股编号2-52-6Temperature C170170Pressure bar3636Vapor Frac11Mole Flow kmol/hr997.0899448.8507259Mass Flow kg/hr40114.6675740114.66757Volume Flow cum/hr949.9404307363.9880078Enthalpy Gcal/hr-47.93639647-57.3074383表1-32 R0201热负荷表H Gcal/hr-9.371041848表1-33 R0201热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-9.371041848-47.93639647-57.30743831.67E-081.4.3 V0201不凝汽气液分离器表1-34 V0201物流焓变表INOUT流股编号2-102-112-12Temperature C636363Pressure bar0.920.920.92Vapor Frac0.0614875610Mole Flow kmol/hr448.850725927.59873605421.2519899Mass Flow kg/hr40114.66757711.187944239403.47962Volume Flow cum/hr874.7188478837.157586137.56126171Enthalpy Gcal/hr-61.73182673-0.811620989-60.92020574表1-35 V0201热负荷表H Gcal/hr-2.10E-15表1-36 V0201热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-2.10E-15-61.73182673-61.731826732.22E-131.4.4 T0201 EDA精制塔表1-37 T0201物流焓变表INOUT流股编号2-122-132-142-15Temperature C6390.14299221909121294Pressure bar0.920.90.90.9Vapor Frac0100Mole Flow kmol/hr421.25198997.207559697233.0444302181Mass Flow kg/hr39403.47962352.329461612676.5396126374.61055Volume Flow cum/hr37.56126171238.668204913.3709657229.05947122Enthalpy Gcal/hr-60.92020574-0.534481472-23.23621831-35.75810195表1-38 T0201热负荷表冷凝器再沸器QH Gcal/hr-2.2884199743.679824061.391404086表1-39 T0201热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError1.391404086-60.92020574-59.52880173-7.13E-081.4.5 T0202醋酸精制低压塔表1-40 T0202物流焓变表INOUT流股编号2-142-162-21Temperature C85.0961285226.838029118.6516405Pressure bar1.013251.013251.01325Vapor Frac000Mole Flow kmol/hr238.077913750.46834605187.6095676Mass Flow kg/hr13270.8919169475582Volume Flow cum/hr13.815905891.83367969512.22439455Enthalpy Gcal/hr-25.22164492-3.736201359-21.35403179表1-41 T0202热负荷表冷凝器再沸器QH Gcal/hr-2.7538402932.885256140.131415847表1-42 T0202热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError0.131415847-25.22164492-25.09023315-4.07E-061.4.6 T0203醋酸精制高压塔表1-43 T0203物流焓变表INOUT流股编号2-212-232-25Temperature C118.6516405132.6104327117.9237986Pressure bar1.013251.013251.01325Vapor Frac000Mole Flow kmol/hr187.60956769.999978349177.6095893Mass Flow kg/hr11576.75582922.384054310654.37176Volume Flow cum/hr12.224394550.97757093811.27123787Enthalpy Gcal/hr-21.35403179-1.365088237-19.98964875表1-44 T0203热负荷表冷凝器再沸器QH Gcal/hr-8.9389792448.938274076-0.000705168表1-45 T0203热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError-0.000705168-21.35403179-21.35473699-3.18E-081.5 EDA裂解制VAC工段1.5.1 E0301 EDA加热器表1-46 E0302物流焓变表INOUT流股编号3-13-2Temperature C95.04874057140Pressure bar0.91.01325Vapor Frac00Mole Flow kmol/hr1400.290971400.29097Mass Flow kg/hr155233.6041155233.6041Volume Flow cum/hr156.1036145166.0106588Enthalpy Gcal/hr-220.0013372-216.7676928表1-47 E0302热负荷表H Gcal/hr3.233644333表1-48 E0302热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError3.233644333-220.0013372-216.7676928-1.31E-091.5.2 T0301 EDA裂解反应精馏塔表1-49 T0301物流焓变表INOUT流股编号3-23-33-4Temperature C14072.70776819132.2211454Pressure bar1.013251.013251.01325Vapor Frac000Mole Flow kmol/hr1400.29097180.20344491400.190829Mass Flow kg/hr155233.604115511.1805139722.4236Volume Flow cum/hr166.010658817.98619409147.7475011Enthalpy Gcal/hr-216.7676928-14.72684444-200.5287314表1-50 T0301热负荷表冷凝器再沸器QH Gcal/hr-20.1052617821.6173791.512117216表1-51 T0301热量平衡计算表Q Gcal/hrHin Gcal/hrHout Gcal/hrError1.512117216-216.7676928-215.2555758-1.67E-071.5.3 T0302 EDA回收精馏