常压白煤气化制氢流程图---wgb

11、计算条件1.1制氢总体工艺流程蒸汽2空气3二氧化碳9无烟煤15678渣4解吸气10燃料气产品氢气111.2计算基准1.3原料煤成分成分水份固定碳挥发份灰份硫ΣG%6.8725.6150.6100热值Q=33285-360.0648X0.068-385.1856X0.18-100.4832X0.03=33188KJ/KG1.4.假定水煤气组成%H2COCO2N2CH4ArO2总硫Σ45.7236.5810.46.000.700.300.301.0G/NM3100238371907254223128365.156156521362、工艺计算2.1、物料平衡计算气化栲胶拖硫压缩机1~3段变换碳丙脱碳变压吸附压缩机4段图1.1供H2及CO、生产工艺流程示意图2计算结果汇总表位号123物流原料煤工艺蒸汽工艺空气序号组分分子量%Gt/H%VNM3/tNH3%WKg/tNH31CO28.012H22.023CO244.014CH416.045AR39.950.915026N228.0175.79418377H2S34.088COS60.079O23220.341122810NH317.0311水1002.96163512煤23.2513渣干基流量NM3/h41853水量Kg/h1027总流量NM3/h42880总流量Kg/h29222压力MpaG0.30.02温度℃14028重度Kg/M3粘度3计算结果汇总表（续）位号456物流煤气炉渣水煤气脱硫气序号组分分子量%Gt/h%VNM3/h%WNM3/h1CO28.0134.041490234.06149012H22.0242.541862542.56186243CO244.019.6842369.6842364CH416.040.652850.652855AR39.950.281221226N228.015.59244424447H2S34.080.0419.531.0948COS60.079O232121.9121.910NH317.0311水6.930193.68301912煤13渣4075干基流量NM3/h4075540736水量Kg/h24262426总流量NM3/h4374443754总流量Kg/h395024262426压力MpaG0.020.02温度℃4040重度Kg/M3粘度4计算结果汇总表（续）位号789物流变换气脱碳净化气CO2解吸气序号组分分子量%GNM3/h%VNM3/h%WNM3/h1CO28.013.3317884.8717830.0442H22.0258.653149485.92314500.37443CO244.0132.30173491.3348699.46116734CH416.040.522850.772820.0335AR39.950.23121.90.33119.50.022.46N228.014.5524446.6524350.079.07H2S34.081.0948COS60.079O23210NH317.0311水180.42223.50.1349.012煤13渣干基流量NM3/h534833655611736水量Kg/h179.639.4总流量NM3/h5370636605总流量Kg/h压力MpaG1.60.02温度℃2020重度Kg/M3粘度5计算结果汇总表（续）位号101112物流PSA解吸气产品氢气造气吹风气序号组分分子量%GNM3/h%VNM3/h%WNM3/h1CO28.0127.01783.510PPM0.306.7029392H22.0223.81157299.5298780.482153CO244.017.35485.715.3168984CH416.044.25280.650PPM1.50.86388.35AR39.950.138.60.37110.90.28125.86N228.0136.742426.30.038.772.06324617H2S34.088COS60.079O23210NH317.0311水180.7247.34.31193912煤13渣干基流量NM3/h6556.73000043109水量Kg/h总流量NM3/h6604.145048总流量Kg/h压力MpaG0.023.60.002温度℃3030320重度Kg/M3粘度