附录2-能量衡算书VIP

2019“东华科技恒逸石化杯”第十三届全国大学生化工设计竞赛2019年“东华科技-恒逸杯”第十三届全国大学生化工设计竞赛南京扬子石化分公司能量衡算书年产20万吨醋酸乙烯酯的项目 Hots团队任珈萱 杨钰芬 王凯 吴培丽 孙旺指导老师：常西亮 邵圣娟 李晓红 张云凤I目 录1.1概述11.2 热量衡算原理11.3 热量衡算任务21.4 热量衡算21.4.1 醋酸乙烯合成工段21.4.2 气体吸收工段81.4.3 醋酸乙烯精制工段201.5 总结381.1概述本项目拟建一套年产20万吨醋酸乙烯酯的装置，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热量的消耗、释放和转化。其中的热量变换数量关系可以从热量衡算求得，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。总而言之，通过下述热量衡算，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 热量衡算原理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，进行热量衡算书的编制。其中一个主要依据是热量平衡方程：其中，表示输入设备热量的总和；表示输出设备热量的总和；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；离开设备的各物料焓之和；进入设备的各物料焓之和。在进行全厂热量衡算时，是以单元设备为基本单位，考虑由机械能转换、化学反应释放和单纯的物理变化带来的热量变化。最终对全工艺段进行系统级的热量平衡计算，进而用于指导节能降耗设计工作。1.3 热量衡算任务在进行脱硫并资源化利用装置的热量衡算中，主要通过定量计算完成下述基本任务：确定工艺单元中物料输送机械（如泵）所需要的功率，以便于进行设备的设计和选型； 确定精馏等单元操作中所需要的热量或冷量以及传递速率，计算换热设备的尺寸，确定加热剂和冷却剂的消耗量，为后续设计中比如供汽、供冷、供水等专业提供设备条件；确定为保持一定反应温度所需移除或者加入的热传递速率，指导反应器的设计和选型；提高热量内部集成度，充分利用余热，提高能量利用率，降低能耗；最终计算出总需求能量和能量的费用，并由此确定工艺过程在经济上的可行性。1.4 热量衡算注：以下流股编号和设备位号与源文件中“3-全流程模拟（含热泵、含公用工程、含换热网络、含塔优化参数代入）”对应。1.4.1 醋酸乙烯合成工段1.4.1.1 泵热量衡算（1）醋酸进料泵(P0101)表1-1 热负荷表P0101WQHeat Duty（Gcal/hr）0.00760表1-2 流股焓变计算表P0101进口出口流股编号CH3COOHP0101OUTTemperature C93.44 94.11 Pressure bar1 8 Vapor Frac0 0 Mole Flow kmol/hr414.200 414.200 Mass Flow kg/hr23764.687 23764.687 Volume Flow cum/hr25.061 25.085 Enthalpy Gcal/hr-43.908 -43.900 表1-3 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00760-43.908 -43.900 -1.74E-04（2）乙烯预热泵(P0103)表1-4 热负荷表P0103WQHeat Duty（Gcal/hr）00表1-5 流股焓变计算表P0103进口出口流股编号T0302DP0103OUTTemperature C99.64 99.64 Pressure bar1.0 1.2 Vapor Frac0 0 Mole Flow kmol/hr414.200 414.200 Mass Flow kg/hr23764.687 23764.687 Volume Flow cum/hr14.009 14.009 Enthalpy Gcal/hr-47.693 -47.693 表1-6 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-47.693 -47.693 5.76E-151.4.1.2 反应器热量衡算反应器(R0101、R0102)表1-7 热负荷表R0101WQHeat Duty（Gcal/hr）0.00 -10.64 表1-8 流股焓变计算表R0101进口出口流股编号M0102OUTR0101OUTTemperature C197.58 180.00 Pressure bar8.0 7.8 Vapor Frac1 1 Mole Flow kmol/hr1941.660 1819.609 Mass Flow kg/hr67210.705 67210.705 Volume Flow l/min158317.191 146487.822 Enthalpy Gcal/hr-26.594 -37.235 表1-9 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-10.64-26.594 -37.235 0表1-10 热负荷表R0102WQHeat Duty（Gcal/hr）0.00 1.79 表1-11 流股焓变计算表R0102进口出口流股编号R0101OUTR0102OUTTemperature C180.00 180.00 Pressure bar7.8 8.0 Vapor Frac1 1 Mole Flow kmol/hr1819.609 1807.010 Mass Flow kg/hr67210.705 67210.705 Volume Flow l/min146487.822 141836.643 Enthalpy Gcal/hr-37.235 -39.022 表1-12 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error01.79-37.235 -39.022 01.4.1.3 换热器热量衡算（1）醋酸蒸发器（E0101）表1-13 热负荷表E0101WQHeat Duty（Gcal/hr）0.00 -3.40 表1-14 流股焓变计算表E0101进口出口流股编号P0101OUTE0101OUTTemperature C94.11 200.00 Pressure bar8.0 8.0 Vapor Frac0 1 Mole Flow kmol/hr414.200 414.200 Mass Flow kg/hr23764.687 23764.687 Volume Flow cum/hr25.085 2036.788 Enthalpy Gcal/hr-43.900 -40.503 表1-15 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-3.40-43.900 -40.503 0（2）乙烯预热器（E0102）表1-16 热负荷表E0102WQHeat Duty（Gcal/hr）0.00 -0.19 表1-17 流股焓变计算表E0102进口出口流股编号CH2CH2P0103OUTE0102OUTFH2OTemperature C25.00 99.64 80.00 85.91 Pressure bar8181Vapor Frac1010Mole Flow kmol/hr303.44 712.38 303.44 712.38 Mass Flow kg/hr8512.69 12855.73 8512.69 12855.73 Volume Flow cum/hr940.26 14.01 1113.71 13.79 Enthalpy Gcal/hr-43.90 -43.71 表1-18 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-0.19-43.899 -43.714 0（2）原料冷却器（E0103）表1-19 热负荷表E0103WQHeat Duty（Gcal/hr）0.00 0.46 表1-20 流股焓变计算表E0103进口出口流股编号M0102OUTE0103OUTTemperature C197.58 180.00 Pressure bar8.0 8.0 Vapor Frac1 1 Mole Flow kmol/hr1941.660 1941.660 Mass Flow kg/hr67210.705 67210.705 Volume Flow cum/hr9499.031 9144.341 Enthalpy Gcal/hr-26.134 -26.594 表1-21 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00.46-26.134 -26.594 01.4.1.4 风机热量衡算循环乙烯风机（P0102）表1-22 热负荷表P0102WQHeat Duty（Gcal/hr）0.00 -2.39 表1-23 流股焓变计算表P0102进口出口流股编号GCH2CH2XCH2CH2Temperature C40.00 247.29 Pressure bar1.0 8.0 Vapor Frac1 1 Mole Flow kmol/hr1079.752 1079.702 Mass Flow kg/hr30323.010 30323.010 Volume Flow cum/hr27745.142 5840.006 Enthalpy Gcal/hr8.004 10.390 表1-24 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-2.398.00410.39001.4.2 气体吸收工段1.4.2.1 塔热量衡算（1）酸洗塔（T0201）表1-25 热负荷表T0201WQHeat Duty（Gcal/hr）0.00 0.00 表1-26 流股焓变计算表T0201进口出口流股编号C2H4O2E0202OUTT0201DT0201WTemperature C20.00 21.06 20.08 36.62 Pressure bar3.53.53.53.5Vapor Frac0.0 1.0 1.0 0.0 Mole Flow kmol/hr961.20 1173.75 1100.34 1034.61 Mass Flow kg/hr55149.84 35194.50 31138.60 59205.74 Volume Flow cum/hr52.97 8191.04 7664.59 59.32 Enthalpy Gcal/hr-99.69 -99.69 表1-27 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-99.686 -99.686 0（2）水洗塔（T0202）表1-28 热负荷表T0202WQHeat Duty（Gcal/hr）0.00 0.00 表1-29 流股焓变计算表T0202进口出口流股编号GCH2CH2XCH2CH2Temperature C40.00 247.29 Pressure bar1.0 8.0 Vapor Frac1 1 Mole Flow kmol/hr1079.752 1079.702 Mass Flow kg/hr30323.010 30323.010 Volume Flow cum/hr27745.142 5840.006 Enthalpy Gcal/hr8.004 10.390 表1-30 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-27.316 -27.316 0（3）CO2吸收塔（T0203）表1-31 热负荷表T0203WQHeat Duty（Gcal/hr）0.00 0.00 表1-32 流股焓变计算表T0203进口出口流股编号E0203OUTLEANINT0203DT0203WTemperature C25.0025.0025.1825.17Pressure bar3.541.011.011.29Vapor Frac1.00.01.00.0Mole Flow kmol/hr1109.37295.271099.81298.13Mass Flow kg/hr31064.156792.2330684.367172.02Volume Flow cum/hr26838.805.637682.465.00Enthalpy Gcal/hr-15.23-15.23表1-33 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00-15.231 -15.231 0（4）CO2解吸塔（T0204）表1-34 热负荷表T0204WQHeat Duty（Gcal/hr）0.00 -1.55 表1-35 流股焓变计算表T0204进出流股编号T0203WT0204DT0204WTemperature C25.17 106.45 127.94 Pressure bar1.3 1.0 1.3 Vapor Frac0.0 1.0 0.0 Mole Flow kmol/hr298.133 123.612 180.042 Mass Flow kg/hr7172.024 2403.850 4768.174 Volume Flow cum/hr5.629 3825.410 3.219 Enthalpy Gcal/hr-21.924 -20.377 表1-36 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0-1.55 -21.924 -20.377 01.4.2.2 换热器热量衡算（1）生成气冷却器（E0201）表1-37 热负荷表E0201WQHeat Duty（Gcal/hr）0.00 8.76 表1-38 流股焓变计算表E0201进口出口流股编号J0101OUTE0201OUTTemperature C180.00 30.00 Pressure bar3.5 3.5 Vapor Frac1 1 Mole Flow kmol/hr1807.010 1807.009 Mass Flow kg/hr67210.705 67210.705 Volume Flow cum/hr19451.883 8436.949 Enthalpy Gcal/hr-39.022 -47.781 表1-39 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error08.76 -39.022 -47.781 0（2）气体冷却器（E0202）表1-40 热负荷表E0202WQHeat Duty（Gcal/hr）0.00 2.99 表1-41 流股焓变计算表E0202进口出口流股编号P0201OUTE0202OUTTemperature C249.08 21.06 Pressure bar3.5 3.5 Vapor Frac1 1 Mole Flow kmol/hr1173.753 1173.753 Mass Flow kg/hr35194.496 35194.496 Volume Flow cum/hr14561.141 8191.044 Enthalpy Gcal/hr6.993 4.000 表1-42 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error02.99 6.993 4.000 0 （3）乙烯冷却器（E0203）表1-43 热负荷表E0203WQHeat Duty（Gcal/hr）0.00 1.29 表1-44 流股焓变计算表E0203进口出口流股编号P0202OUTE0203OUTTemperature C134.14 25.00 Pressure bar3.5 3.5 Vapor Frac1 1 Mole Flow kmol/hr1109.368 1109.368 Mass Flow kg/hr31064.150 31064.150 Volume Flow cum/hr10593.004 7682.459 Enthalpy Gcal/hr7.316 6.030 表1-45 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error01.29 7.316 6.030 0 （4）循环吸收剂冷却器（E0204）表1-46 热负荷表E0204WQHeat Duty（Gcal/hr）0.00 3.80 表1-47 流股焓变计算表E0204进口出口流股编号M0202OUTLEANINTemperature C300.14 25.00 Pressure bar1.0 1.0 Vapor Frac1 0 Mole Flow kmol/hr295.273 295.273 Mass Flow kg/hr6792.226 6792.226 Volume Flow cum/hr11379.378 5.000 Enthalpy Gcal/hr-17.463 -21.261 表1-48 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error03.80 -17.463 -21.261 0 （4）循环乙烯预热器（E0205）表1-49 热负荷表E0205WQHeat Duty（Gcal/hr）0.00 0.15 表1-50 流股焓变计算表E0205进口出口流股编号T0203DE0205OTTemperature C25.18 40.00 Pressure bar1.0 1.0 Vapor Frac1 1 Mole Flow kmol/hr1099.810 1099.810 Mass Flow kg/hr30684.358 30684.358 Volume Flow cum/hr26838.796 28260.547 Enthalpy Gcal/hr6.693 6.847 表1-51 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error00.15 6.693 6.847 0 1.4.2.3 风机热量衡算（1）气体输送风机（P0201）表1-52 热负荷表P0201WQHeat Duty（Gcal/hr）-2.99 0.00 表1-53 流股焓变计算表P0201进口出口流股编号M0201OUTP0201OUTTemperature C20.00 249.08 Pressure bar0.3 3.5 Vapor Frac1 1 Mole Flow kmol/hr1173.753 1173.753 Mass Flow kg/hr35194.496 35194.496 Volume Flow cum/hr95361.398 14561.141 Enthalpy Gcal/hr4.003 6.993 表1-54 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error-2.99 0.00 4.003 6.993 0 （2）气体输送风机（P0202）表1-55 热负荷表P0202WQHeat Duty（Gcal/hr）-1.27 0.00 表1-56 流股焓变计算表P0202进口出口流股编号T0202DP0202OUTTemperature C15.83 134.14 Pressure bar1.0 3.5 Vapor Frac1 1 Mole Flow kmol/hr1109.368 1109.368 Mass Flow kg/hr31064.150 31064.150 Volume Flow cum/hr26305.541 10593.004 Enthalpy Gcal/hr6.044 7.316 表1-57 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error-1.27 0.00 6.044 7.316 0 1.4.2.4 气液分离罐热量衡算（1）F0201表1-58 热负荷表F0201WQHeat Duty（Gcal/hr）0.00 0.48 表1-59 流股焓变计算表F0201进出流股编号E0201OUTF0201DF0201WTemperature C30.00 20.00 20.00 Pressure bar3.5 3.5 3.5 Vapor Frac0.6 1.0 0.0 Mole Flow kmol/hr1807.009 1170.176 636.832 Mass Flow kg/hr67210.705 35019.651 32191.054 Volume Flow cum/hr8436.949 8148.923 32.794 Enthalpy Gcal/hr-47.781 -48.264 表1-60 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.48 -47.781 -48.264 0 （2）F0202表1-61 热负荷表F0202WQHeat Duty（Gcal/hr）0.00 0.02 表1-62 流股焓变计算表F0202进出流股编号F0201WF0202DF0202WTemperature C20.00 20.00 20.00 Pressure bar3.5 0.3 0.3 Vapor Frac0.0 1.0 0.0 Mole Flow kmol/hr636.832 3.577 633.256 Mass Flow kg/hr32191.054 174.845 32016.209 Volume Flow cum/hr32.794 290.627 32.569 Enthalpy Gcal/hr-52.393 -52.376 表1-63 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.02 -52.393 -52.376 0 （3）脱气槽（F0203）表1-64 热负荷表F0203WQHeat Duty（Gcal/hr）0.00 -0.14 表1-65 流股焓变计算表T0203进口出口流股编号T0201WT0202WF0203DF0203WTemperature C36.62 9.48 25.00 25.00 Pressure bar3.50 1.01 1.00 1.00 Vapor Frac0.00 0.00 1.00 0.00 Mole Flow kmol/hr1034.61 490.97 32.60 1492.98 Mass Flow kg/hr59205.74 9082.09 953.66 67334.17 Volume Flow cum/hr59.32 9.14 808.13 67.36 Enthalpy Gcal/hr-139.87 -140.01 表1-66 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 -0.14 -139.868 -140.012 0 1.4.2.5 泵热量衡算醋酸循环泵（PX01）表1-67 热负荷表PX01WQHeat Duty（Gcal/hr）0.01 0.00 表1-68 流股焓变计算表PX01进口出口流股编号MX02OUTPX01OUTTemperature C100.56 100.76 Pressure bar1.0 3.5 Vapor Frac0 0 Mole Flow kmol/hr961.200 961.200 Mass Flow kg/hr55149.841 55149.841 Volume Flow cum/hr58.752 58.770 Enthalpy Gcal/hr-101.705 -101.700 表1-69 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.01 0.00 -101.705 -101.700 0 1.4.3 醋酸乙烯精制工段1.4.3.1 塔热量衡算（1）醋酸粗分塔（T0301）表1-70 热负荷表T0301WQHeat Duty（Gcal/hr）0.00Condenser：-4.57 Reboiler：11.19表1-71 流股焓变计算表T0301进出流股编号P0302OUTT0301DT0301WTemperature C23.6865.85108.70Pressure bar2.01.01.01Vapor Frac0.00.00.0Mole Flow kmol/hr2126.240330.6341795.607Mass Flow kg/hr99350.37923337.62176012.757Volume Flow cum/hr99.9239197.23684.884Enthalpy Gcal/hr-192.508-185.896表1-72 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 -6.61 -192.508 -185.896 0 （2）醋酸精制塔（T0302）表1-73 热负荷表T0302WQHeat Duty（Gcal/hr）0.00Condenser：-34.89Reboiler：35.01表1-74 流股焓变计算表T0302进出流股编号T0301WT0302DT0302WTemperature C108.70 99.64 116.45 Pressure bar1.0 1.0 1.0 Vapor Frac0.0 0.0 0.0 Mole Flow kmol/hr1795.607 712.382 1083.225 Mass Flow kg/hr76012.757 12855.729 63157.028 Volume Flow cum/hr84.884 14.009 68.718 Enthalpy Gcal/hr-162.929 -162.812 表1-75 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.12 -162.929 -162.812 0 （3）醋酸乙烯精制塔（T0303）表1-76 热负荷表T0303WQHeat Duty（Gcal/hr）0.00Condenser：-4.76Reboiler：5.80表1-77 流股焓变计算表T0303进出流股编号P0303OUTT0303DT0303WTemperature C20.02 54.84 74.93 Pressure bar1.2 1.0 1.1 Vapor Frac0.0 1.0 0.0 Mole Flow kmol/hr282.900 64.672 218.228 Mass Flow kg/hr22441.927 3657.409 18784.518 Volume Flow cum/hr24.046 1763.640 21.801 Enthalpy Gcal/hr-22.912 -21.867 表1-78 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 -1.05 -22.912 -21.867 0 （4）乙醛精制塔（T0304）表1-79 热负荷表T0304WQHeat Duty（Gcal/hr）0.00Condenser：-1.23Reboiler：0.86表1-80 流股焓变计算表T0304进出流股编号T0303DT0304DT0304WTemperature C54.84 19.97 61.84 Pressure bar1.0 1.0 1.0 Vapor Frac1.0 1.0 0.0 Mole Flow kmol/hr64.672 19.819 44.853 Mass Flow kg/hr3657.409 869.205 2788.204 Volume Flow cum/hr1763.640 483.005 3.071 Enthalpy Gcal/hr-3.968 -4.343 表1-81 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.38 -3.968 -4.343 0 （5）醋酸甲酯粗分塔（T0305）表1-82 热负荷表T0305WQHeat Duty（Gcal/hr）0.00Condenser：-0.54Reboiler：0.60表1-83 流股焓变计算表T0305进出流股编号P0302OUTT0305DT0305WTemperature C23.68 60.39 75.61 Pressure bar2.0 1.0 1.1 Vapor Frac0.0 0.0 0.0 Mole Flow kmol/hr2126.240 9.524 22.226 Mass Flow kg/hr99350.379 631.813 1913.156 Volume Flow cum/hr99.923 0.705 2.223 Enthalpy Gcal/hr-2.727 -2.669 表1-84 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.06 -2.727 -2.669 0 （6）醋酸甲酯精制塔（T0306）表1-85 热负荷表T0306WQHeat Duty（Gcal/hr）0.00 0.00 表1-86 流股焓变计算表T0306进口出口流股编号P0305OUTT0306FT0306LT0306DT0306WTemperature C25.0376.0458.5459.1276.03777Pressure bar1.201.131.001.001.125Vapor Frac0.001.000.001.000Mole Flow kmol/hr8.4623.1415.5621.7725.39398Mass Flow kg/hr610.971992.271045.641462.742186.135Volume Flow cum/hr0.65597.231.17601.522.541748Enthalpy Gcal/hr-3.98-3.98表1-87 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.00 -3.981 -3.981 0 1.4.3.2 换热器热量衡算（1）气体冷却器（E0301）表1-88 热负荷表E0301WQHeat Duty（Gcal/hr）0.00 2.96 表1-89 流股焓变计算表E0301进口出口流股编号T0301DE0301OUTTemperature C65.85 38.33 Pressure bar1.0 1.0 Vapor Frac1 0 Mole Flow kmol/hr330.634 330.632 Mass Flow kg/hr23337.621 23337.621 Volume Flow cum/hr9197.236 25.316 Enthalpy Gcal/hr-22.967 -25.928 表1-90 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 2.96 -22.967 -25.928 0 （2）粗醋酸甲酯冷却器（E0302）表1-91 热负荷表E0302WQHeat Duty（Gcal/hr）0.00 0.06 表1-92 流股焓变计算表E0302进口出口流股编号T0304WE0302OUTTemperature C61.84 25.00 Pressure bar1.0 1.0 Vapor Frac0 0 Mole Flow kmol/hr44.853 44.853 Mass Flow kg/hr2788.204 2788.204 Volume Flow cum/hr3.071 2.913 Enthalpy Gcal/hr-3.562 -3.617 表1-93 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.06 -3.562 -3.617 0 （3）粗醋酸甲酯冷却器（E0303）表1-94 热负荷表E0303WQHeat Duty（Gcal/hr）0.00 0.01 表1-95 流股焓变计算表E0303进口出口流股编号P0306OUTT0305DE0303OUTFH2O2Temperature C36.62 9.48 25.00 25.00 Pressure bar3.50 1.01 1.00 1.00 Vapor Frac0.00 0.00 1.00 0.00 Mole Flow kmol/hr1034.61 490.97 32.60 1492.98 Mass Flow kg/hr59205.74 9082.09 953.66 67334.17 Volume Flow cum/hr59.32 9.14 808.13 67.36 Enthalpy Gcal/hr-4.10 -4.10 表1-96 热量平衡计算一览表W（Gcal/hr）Q（Gcal/hr）Hin（Gcal/hr）Hout（Gcal/hr）Error0.00 0.01 -4.0