变换工艺计算

一氧化碳转换率49.56%

预变换炉中CO的转化率为49.56%

预变换气中一氧化碳为体积量1374.352m3/h

预变换后的气体量490682.9122m3/h

预变换气组成体积百分比

H 242.70%209521.6035 CO28.02%1374.352 CO228.32%1361.4007 N20.24%1177.63 Ar0.11%539.7512034 NH30.06%294.4097473 CH40.05%245.3414561 H2S0.49%2404.34627 COS0.01%49.06829122

水解气量（脱硫过程中Ar也不变30%预变换气中Ar）

水解气体积百分含量体积百分比

H 235.39%95508.97545 CO45.91%1239.8887 CO217.87%48226.77003 N20.15%404.8134026 Ar0.06%161.925361NH30.05%134.9378009 CH40.06%161.925361 H2S0.50%1349.378009 COS0.01%26.98756017

水解气中Ar的百分率为0.06%

变换气组成体积百分比

H 252.85%119700.3839 CO 6.00%135.44755 CO240.06%90732.21149 N20.35%792.7177738 Ar0.17%385.0343473 NH30.07%158.5435548 CH40.03%67.94723776 H2S0.47%10.506725 COS0.01%22.907925

调节后的一氧化碳体积量70471.888m3/h

调节变换后的气组成体积百分比

H 246.84%167219.0052 CO19.74%70471.888 CO232.45%115846.22 N20.28%999.6012266 Ar0.13%4.1005695 NH30.06%214.2002628 CH40.04%142.8001752 H2S0.45%1606.501971 COS0.01%35.70004381

一. 进塔新鲜气组成计算:组分

摩尔分率

甲醇年产量1800000000kg

年运行时间8000h

精馏塔出甲醇量7031.25kmol/h 设精馏塔损失3%

设计裕度 4.50%

则进入精馏塔的粗甲醇中甲醇的含量为7362.565445kmol/h 设CO,CO2转化为甲醇的转化率为96%

则进入合成器的新鲜气量为28404.95928kmol/hm3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h

m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h

m3/h m3/h m3/h m3/h m3/hm3/h m3/h m3/h m3/h

m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h

m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h m3/h

636271.0878m3/h