【甲醇生产设计计算案例综述1800字】

甲醇生产设计计算案例综述图1甲醇流程图1.1设计参数年产10万吨甲醇。一年按照330天的操作计算。产品粗甲醇的质量组成：CH3OH：（96.9%）；H2O：（3.1%）（其它杂质忽略不计）。出净醇塔烯醇水为1234.2kg/h，其质量组成为甲醇19%，水81%。醇后气流量：47224Nm3/h，摩尔分率：CH3OH：0.02%，H2：71.27%N2：23.8%，CO：3.82%CO2：0.34%，CH4：0.75%。甲醇合成塔出塔气中含甲醇体积比为4.42%，生产测得CH4的生产在计算中忽略不计。甲醇中间槽气体溶解损失及驰放气中甲醇扩散损失忽略不计。其它数据以工厂实际收集为准。1.2甲醇的生产总量根据粗甲醇的质量组成（CH3OH：96.9%；H2O：3.1%.），算得甲醇中间槽的各组分含量（一年按330计算），年产粗甲醇为10万吨。甲醇年产量：100000吨/年×96.9%=96900吨/年=12234.84kg/h=382.33kmol/h=8565.76Nm3/h水：100000吨/年×3.1%=3100吨/年=391.41kg/h=21.75kmol/h=487.2Nm3/h表6甲醇合成塔产品组成组分甲醇水合计质量分率%96.13.9100摩尔产量kmol/h382.3321.75404.08流量Nm3/h8565.76487.29052.96根据醇后气的流量及各组分的摩尔分率求各组分的流量。CH3OH醇后气=47224Nm3/h×0.02%=9.44Nm3/hH2醇后气=47224Nm3/h×71.27%=33656.54Nm3/hN2醇后气=47224Nm3/h×23.8%=11239.31Nm3/hCO醇后气=47224Nm3/h×3.82%=1803.97Nm3/hCO2醇后气=47224Nm3/h×0.34%=160.56Nm3/hCH4醇后气=47224Nm3/×0.75%=354.18Nm3/h表7醇后气组成组分名称CH3OHH2N2COCO2CH4合计流量（Nm3/h）9.4433656.5411239.311803.97160.56354.182472224摩尔产量kmol/h0.42150.52501.7580.37.1715.81756.2摩尔比率%0.0271.2723.83.820.340.75100根据稀醇水的质量流量以及各组分的质量组成求各组分的流量已知出净醇塔稀醇水为1234.2kg/h。其质量组成：甲醇：19%，水：81%。求得CH3OH稀醇水=1234.2×19%=234.5kg/h=7.33koml/h=164.19Nm3/h水=1234.2×81%=999.7kg/h=55.54kmol/h=1244.07Nm3/h求粗甲醇总产量=8565.76+9.44+164.19=8739.39Nm3/h1.3进净醇塔气体流量及组分摩尔分率图净醇塔气体流向图CH3OH净醇塔=CH3OH醇后气+CH3OH稀醇水=9.44+164.19=173.63Nm3/hH2净醇塔=33656.54Nm3/h;N2净醇塔=11239.31Nm3/h;CO净醇塔=1803.97Nm3/h;CO2净醇塔=160.56Nm3/hCH4净醇塔=354.18Nm3/h表8净醇塔的出塔气量及组成组分名称CH3OHH2N2COCO2CH4合计流量（Nm3/h）173.6333656.5411239.311803.961803.96354.1847388.18摩尔比率%（%）0.3771.0223.723.810.340.741001.4出塔气与循环气图甲醇分离器气体流向图循环中甲醇含量＝（醇后气甲醇含量+烯醇水中甲醇含量）/（醇后气量+烯醇水中甲醇含量）＝（9.4+164.15）/（47224+164.15）＝0.37%设出塔气量为XNm3/h,循环气量为YNm3/h，则4.42%X=47224+164.19+8565.76+Y解 X=210294.59（Nm3/h）Y=154340.64（Nm3/h）求得循环气中各组分流量：CH3OH循环气=154340.64×0.0037=571.06Nm3/hH2循环气=154340.64×0.7102=109612.72Nm3/hN2循环气=154340.64×0.2372=36609.60Nm3/hCO循环气=154340.64×0.0381=5880.38Nm3/hCO2循环气=154340.64×0.0034=524.76Nm3/hCH4循环气=154340.64-571.06-109612.72-36609.60-5880.38-524.76=1142.12Nm3/h表9循环气各组分流量及摩尔分率表组分名称CH3OHH2N2COCO2CH4合计流量（Nm3/h）571.06109612.7236609.605880.38524.761142.12154340.64摩尔比率%0.3771.0223.723.810.340.74100求得出塔气各组分流量：CH3OH出塔气=8565.76+164.19+571.06+9.44=9310.45Nm3/hH2出塔气=109612.72+33656.54=143269.22 Nm3/hN2出塔气=36609.60+11239.31=47848.91Nm3/hCO出塔气=5880.38+1803.97=7684.35Nm3/hCO2出塔气=524.76+160.56=685.32Nm3/hCH4出塔气=1142.12+354.18=1496.3Nm3/h表10出塔气各组分流量及摩尔分率表组分名称CH3OHH2N2COCO2CH4H2O合计流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率%（%）4.4267.9722.703.650.320.710.231001.5新鲜气组成及计算1）新鲜气各组分的摩尔比率CH3OH：0.02%，H2：71.27%N2：23.8%，CO：3.82%CO2：0.34%，CH4：0.75%。CH4忽略不计。醇后气流量47224Nm3/h。CO+2H2→CH3OH+102.5KJ/mol在反应中，已知出塔气中甲醇的生成量为9310.45Nm3/h，则CO的消耗量为9310.45Nm3/h，H2的消耗量=18620.9Nm3/h。CO2+H2→CO+H20-42.9kJ/mol已知甲醇中间槽中H2O的流量为487.2Nm3/h，则CO的生成量为487.2Nm3/h，CO2的消耗量为487.2Nm3/h，H2的消耗量为487.2Nm3/h。反应所消耗与生成气体量如下表所示：表11反应所消耗及生成气体中流量表反应消耗量（Nm3/h）反应生成量（Nm3/h）COCO2H2CH3OHCO主反应9310.45\18620.99310.45\副反应\487.2487.2\487.2合计9310.45487.219108.19310.45487.2H2=33656.54+19108.1=52764.64Nm3/h，N2=11239.31Nm3/h，CO=1803.96+9310.45-487.2=10627.21Nm3/h，CO2=160.56+487.2=647.76Nm3/h，CH4=Nm3/h组分名称H2N2COCO2CH4合计流量（Nm3/h）52764.6411239.3110627.21647.76354.1875633.1摩尔比率（%）69.7614.8614.050.860.47100表12新鲜气各组分流量及摩尔分率表1.6混合气的各组分流量混合气=新鲜气+循环气CH3OH混合气=571.06Nm3/h，H2混合气52764.64+109612.72=162377.36Nm3/h，N2混合气=11239.31+36609.60=47848.91Nm3/h，CO混合气=10627.21+5880.38=16507.59Nm3/h，CO2混合气=647.76+524.76=1172.52Nm3/h，CH4混合气=1142.12=1496.3Nm3/h，表13混合气各组分流量及摩尔分率表组分名称CH3OHH2N2COCO2CH4合计流量（Nm3/h）571.06162377.3647848.9116507.591172.521496.3229973.74摩尔比率（%）0.2370.6120.817.180.520.651001.7物料衡算总表表1410万吨/年粗甲醇的物料衡算总表CH3OHH2N2COCO2CH4H2O合计新鲜气流量（Nm3/h）\52764.6411239.3110627.21647.76354.18\75633.1摩尔比率(%)\69.7614.8614.050.860.47\100循环气流量（Nm3/h）571.06109612.7236609.605880.38524.761142.12\154340.64摩尔比率%）0.3771.0223.723.810.340.74\100进滤油器混合气体流量（Nm3/h）571.06162377.3647848.9116507.591172.521496.3\229973.74摩尔比率（%）0.2370.6120.827.180.520.65\100进合成塔气体流量（Nm3/h）571.06162377.3647848.9116507.591172.521496.3\229973.74摩尔比率（%）0.2370.6120.817.180.520.65\100出合成塔气体流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.23100进废热锅炉气体流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.23100CH3OHH2N2COCO2CH4H2O合计进预热器气体流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率(%)4.4267.9722.703.650.320.710.23100进水冷器物料流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.23100进分离器物料流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.23100进甲醇中间槽物料流量（Nm3/h）8565.76\\\\\487.29052.96摩尔比率（%）94.62\\\\\5.38100进净醇塔气体流量（Nm3/h）173.6333656.5411