年产30万吨合成甲醇项目初步设计说明书(6)

年产30万吨合成甲醇分厂设计

图3-3 分离器物料流股图

项目 进料 塔顶出料 40 72.5 1 19756.97 塔底出料 40 72.5 0.096 1677.23 48661.829 119.439 -87.483 40.3 1639.608 301.435 386.149 146.452 44749.2 1171.875 68.657 68.657 89.496 0.001 0.034 0.006 0.008 Temperature C 40 Pressure bar 72.5 Vapor Frac 0.923 Mole Flow kmol/hr 21434.2 Mass Flow kg/hr 270912.18 222250.348 Volume Flow cum/hr 7176.276 7095.157 Enthalpy Gcal/hr -442.992 -356.21 Mass Flow kg/hr CO 4029.98 3989.68 CO2 163960.76 162321.156 H2 30143.493 29842.058 N2 19307.448 18921.299 CH4 7322.606 7176.154 CH3OH 44749.2 0 H2O 1171.875 0 CH3OCH3 68.657 CH3CH2OH 68.657 C2H4O2 89.496 Mass Frac CO 0.015 CO2 0.605 H2 0.111 N2 0.071 0 0 0 0.018 0.73 0.134 0.085 25

年产30万吨合成甲醇分厂设计

CH4 0.027 CH3OH 0.165 H2O 0.004 CH3OCH3 0 CH3CH2OH 0 C2H4O2 0 Mole Flow kmol/hr CO 143.874 0.032 0 0 0 0 0 142.436 0.003 0.92 0.024 0.001 0.001 0.002 1.439 37.256 149.53 13.784 9.129 1396.573 65.049 1.49 1.49 1.49 0.001 0.022 0.089 0.008 0.005 0.833 0.039 0.001 0.001 0.001 CO2 3725.551 3688.296 H2 14953.02 14803.489 N2 689.22 CH4 456.443 675.435 447.314 CH3OH 1396.573 0 H2O 65.049 CH3OCH3 1.49 CH3CH2OH 1.49 C2H4O2 1.49 Mole Frac CO 0.007 CO2 0.174 H2 0.698 N2 0.032 CH4 0.021 CH3OH 0.065 H2O 0.003 CH3OCH3 0 CH3CH2OH 0 C2H4O2 0 0 0 0 0 0.007 0.187 0.749 0.034 0.023 0 0 0 0 0 表3-2 分离器物料流股衡算表

26

年产30万吨合成甲醇分厂设计

第一精馏塔的物料衡算

图3-4 第一精馏塔物料流股图

项目 进料 塔顶出料 37.3 2 1 26.633 1059.158 343.772 -1.997 2.804 767.997 1.596 25.196 22.092 127.657 0.002 33.169 0.011 78.635 0.003 0.725 0.002 0.024 塔底出料 95.6 3 0 1452.956 45668.495 64.675 -80.828 0 0 0 0 0 44423.483 1170.228 0 68.484 6.3 0 0 0 0 Temperature C 65 Pressure bar 10 Vapor Frac 0 Mole Flow kmol/hr 1479.589 Mass Flow kg/hr 46727.652 Volume Flow cum/hr 63.264 Enthalpy Gcal/hr -84.119 Mass Flow kg/hr CO 2.804 CO2 767.997 H2 1.596 N2 25.196 CH4 22.092 CH3OH 44551.14 H2O 1170.23 CH3OCH3 33.169 CH3CH2OH 68.494 C2H4O2 84.935 Mass Frac CO 0 CO2 0.016 H2 0 N2 0.001 27

年产30万吨合成甲醇分厂设计

CH4 0 CH3OH 0.953 H2O 0.025 CH3OCH3 0.001 CH3CH2OH 0.001 C2H4O2 0.002 Mole Flow kmol/hr CO 0.1 CO2 17.451 H2 0.792 N2 0.899 CH4 1.377 CH3OH 1390.391 H2O 64.958 CH3OCH3 0.72 CH3CH2OH 1.487 C2H4O2 1.414 Mole Frac CO 0 CO2 0.012 H2 0.001 N2 0.001 CH4 0.001 CH3OH 0.94 H2O 0.044 CH3OCH3 0 CH3CH2OH 0.001 C2H4O2 0.001 0.021 0.121 0 0.031 0 0.074 0.1 17.451 0.792 0.899 1.377 3.984 0 0.72 0 1.309 0.004 0.655 0.03 0.034 0.052 0.15 0 0.027 0 0.049 0 0.973 0.026 0 0.001 0 0 0 0 0 0 1386.407 64.958 0 1.487 0.105 0 0 0 0 0 0.954 0.045 0 0.001 0 表3-3 第一精馏塔物料流股衡算表

28

年产30万吨合成甲醇分厂设计

（4）第二精馏塔的物料衡算

图3-5 第二精馏塔物料流股图

项目 进料 塔顶出料 68.9 1.2 0 1322.19 42369.082 57.379 -73.839 0 0 0 0 0 42356.201 1.559 0 5.021 6.3 0 塔底出料 78 1.22 0 130.766 3299.412 4.194 -8.059 0 0 0 0 0 2067.282 1168.669 0 63.462 0 0 Temperature C 95.6 Pressure bar 3 Vapor Frac 0 Mole Flow kmol/hr 1452.956 Mass Flow kg/hr 45668.495 Volume Flow cum/hr 64.675 Enthalpy Gcal/hr -80.828 Mass Flow kg/hr CO 0 CO2 0 H2 0 N2 0 CH4 0 CH3OH 44423.483 H2O 1170.228 CH3OCH3 0 CH3CH2OH 68.484 C2H4O2 6.3 Mass Frac CO 0 29

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