赛区-32共价键队-321设计5附录

第一章物料CO羰化偶联工段物料..................................................................酯再生工 碳酸二甲酯提纯工 乙二醇提纯工 甲醇水双效精馏工 1.5总 第二章能量总 能量的主要依 能量任 能量..........................................................................................................CO羰化偶联工段能量..................................................................酯再生工段能量............................................................................碳酸二甲酯提纯工段能量...........................................................乙二醇提纯工段能量....................................................................甲醇水双效精馏工段能量............................................................附录三设备一览 附录四配管一览 第一章物料CO羰化偶联工段物料物流Temperature-物流Temperature-PressureVpaor111Enthalpy---TotalTotalFlowTotalFlowMassFlow00000000000000000000000000000000000000000表 CO羰化偶联反应器（R0201）物料物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlowMassFlow00000000000000表 CO羰化偶联反应器（R0202）物料物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlowMassFlow0000000000酯再生工1.51.6酯再生工段总物料TemperaturePressureVpaor1100110-------TotalTotalTotalMass00000000000000000000000000000000000000000000000000000000000000000000000000000000000000000000001.7反应精馏塔（T0101）物料物流TemperaturePressureVpaor1010Enthalpy-TotalFlowTotalFlowTotalFlowMassFlow0000000000000000000000000000000000000碳酸二甲酯提纯工1.9碳酸二甲酯提纯工段总物料物流TemperaturePressureVpaor001101Enthalpy-4-4--3-1-3-6Total3TotalFlow2Total7MassFlow00000000000000000000000000000001000600000000000000000001.10预分离塔（T0301）物料物流Temperature0PressureVpaor0010EnthalpyTotalFlowTotalFlowTotalFlowMassFlow0000000000003.58e-9.0519e-000000001.11吸收塔（T0302）物料物流TemperaturePressureVpaor1010EnthalpyTotalFlowTotalFlowTotalFlowMassFlow00000000000000001.4162e-01.0026e-0000000000001.12高压共沸精馏塔（T0303）物料物流TemperaturePressureVpaor0001EnthalpyTotalFlowTotalFlowTotalFlowMassFlow00003.4331e-1.2967e-000000002.5784e-5.5072e-00002.2834e-00001.13碳酸酯精制塔（T0304）物料物流TemperaturePressureVpaor000EnthalpyTotalFlowTotalFlowTotalFlowMassFlow000000000000000000000乙二醇提纯工1.15乙二醇提纯工段总物料物流TemperaturePressureVpaor15.6566e-0100Enthalpy-----TotalFlowTotalFlowTotalFlowMassFlow006.2041e-000001.1426e-000000000000000001.6181e-000001.4855e-9.2882e-0002.2202e-1.2235e-00001.0836e-6.6389e-08.6416e-9.4494e-001.16乙二醇精制塔（T0401）物料物流TemperaturePressureVpaor0100EnthalpyTotalFlowTotalFlowTotalFlowMassFlow7.3759e-000000000000000000001.6807e-1.9846e-1.4308e-1.17甲醇精制回收塔（T0402）物料物流TemperaturePressureVpaor000EnthalpyTotalFlowTotalFlowTotalFlowMassFlow0000000000000001.18草酸酯加氢反应器（R0401）物料物流TemperaturePressure22Vpaor11EnthalpyTotalFlowTotalFlowTotalFlowMassFlow6.2041e-1.1426e-00001.6181e-1.4855e-2.2202e-01.0836e-8.6416e-0甲醇水双效精馏工1.20双效精馏工段总物料物流TemperaturePressureVpaor00EnthalpyTotalFlowTotalFlowTotalFlowMassFlow000000000000000000000000000001.21高压塔（T0501）物料物流TemperaturePressureVpaor0010EnthalpyTotalFlowTotalFlowTotalFlowMassFlow00001.0948e-00000006.2207e-0000000000000000000000001.22常压塔（T0502）物料物流TemperaturePressureVpaor000EnthalpyTotalFlowTotalFlowTotalFlowMassFlow00000000000000000000000001.1941e-000000000000000000001.5总1.23123.6万吨/23.34万吨/36.9万吨/46.9万吨/1.24/质量指标1.25/第二章能量总拟建一套年产25万吨的乙二醇装置，在全工艺段中伴随着物料从一系或单元进入另一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求得，对于新设计的车间，可以由此确定的设备。总之，通过下述能量，可以为后续设计工作中提高热量的利用率，降能量的主要依工程依据化工设计中关于热量的基本思想和要求遵循基与实际工艺相结合的原则，进行热量书的编制。其中一个主要依据是能量平衡方程：Q+W=ΣHout–能量任在进行乙二醇装置的热量中，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）提高热量集成度，充分利用余热，提高能量利用率，降低能耗能量CO羰化偶联工段能量CO羰化偶联反应器2.1QHeat 2.2物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlow2.3Q-0CO羰化偶联反应器2.4QHeat 2.5物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlow2.6Q酯再生工段能量反应精馏塔2.7QHeat 2.8物流TemperaturePressureVpaor1010EnthalpyTotalFlowTotalFlowTotalFlow2.9Q单级压缩机2.10WHeat 2.11物流Temperature-PressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlow2.12W碳酸二甲酯提纯工段能量预分离塔2.13QHeat 2.14物流TemperaturePressureVpaor0010EnthalpyTotalFlowTotalFlowTotalFlow2.15Q吸收塔2.16QHeat 0002.17物流TemperaturePressureVpaor1010EnthalpyTotalFlowTotalFlowTotalFlow2.18Q0高压共沸精馏塔2.19QHeat 2.20物流TemperaturePressureVpaor0001EnthalpyTotalFlowTotalFlowTotalFlow2.21Q碳酸酯精制塔2.22QHeat 2.23物流TemperaturePressureVpaor000EnthalpyTotalFlowTotalFlowTotalFlow2.24Q气液分离器2.25QHeat 02.26物流TemperaturePressureVpaor01EnthalpyTotalFlowTotalFlowTotalFlow2.27Q0乙二醇提纯工段能量乙二醇精制塔2.28QHeat 2.29物流TemperaturePressureVpaor0100EnthalpyTotalFlowTotalFlowTotalFlow2.30Q甲醇回收精制塔2.31QHeat 2.32物流TemperaturePressureVpaor000EnthalpyTotalFlowTotalFlowTotalFlow2.33Q草酸酯加氢反应器2.34QHeat 2.35物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlow2.36Q0单级压缩机2.37WHeat 2.38物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlow2.39W单级压缩机2.40WHeat 2.41物流TemperaturePressureVpaor11EnthalpyTotalFlowTotalFlowTotalFlow2.42W气液分离器2.43QHeat 2.44物流TemperaturePressureVpaor10EnthalpyTotalFlowTotalFlowTotalFlow2.45Q甲醇水双效精馏工段能量高压塔2.46QHeat 02.47物流TemperaturePressureVpaor0010EnthalpyTotalFlowTotalFlowTotalFlow2.48Q常压塔2.49QHeat 02.50物流TemperaturePressureVpaor000EnthalpyTotalFlowTotalFlowTotalFlow2.51Q附录备一览泵泵 扬轴功总轴功率电机总功率231DMC预分醇1DMC预分111DMC精制塔1DMO加氢泵2223215设计温度MNF1Z-4AF1Z-3AF1Z-3AF1Z-3ADMCF1Z-4AF1Z-4AF1Z-4AF1Z-4AF1Z-4A封头内径 列管壁反应温腐蚀余质量反应标准62 火反应标准62 火反应标准62 火尺寸度内管列管规格管数根管程数换热面积重量/BEM600-0.35/0.7-48.8-1.5/19-11BEM1000-2.2/0.7-219.3-3.0/19-11BEM400-0.7/0.35-19.7-2.0/19-11BEM400-1.7/0.7-30.1-3.0/19-11BEM800-2.2/1.1-138.0-3.0/19-11BEM400-0.35/0.7-14.5-1.5/19-11BEM500-0.35-47.5-3.0/19-11BEM1400-0.35-900.5-6.0/19-11BEM450-0.35-28.4-3.0/19-22BEM1600-0.35-1175.9-9.0/19-11BEM219-0.35-2.8-1.5/19-66BEM219-0.35-2.8-1.5/19-11BEM273-0.35-5.4-1.5/19-11BEM273-0.35/9.0-4.7-1.5/19-66BEM450-0.35/9.0-61.3-6.0/19-11BEM219-0.35/9.0-2.8-1.5/19-14BEM1000-0.35/9.0-219.3-3.0/19-11BEM325-2.2/9.0-8