【甲醇生產(chǎn)設(shè)計(jì)計(jì)算案例綜述1800字】

甲醇生產(chǎn)設(shè)計(jì)計(jì)算案例綜述圖1甲醇流程圖1.1設(shè)計(jì)參數(shù)年產(chǎn)10萬(wàn)噸甲醇。一年按照330天的操作計(jì)算。產(chǎn)品粗甲醇的質(zhì)量組成：CH3OH：（96.9%）；H2O：（3.1%）（其它雜質(zhì)忽略不計(jì)）。出凈醇塔烯醇水為1234.2kg/h，其質(zhì)量組成為甲醇19%，水81%。醇后氣流量：47224Nm3/h，摩爾分率：CH3OH：0.02%，H2：71.27%N2：23.8%，CO：3.82%CO2：0.34%，CH4：0.75%。甲醇合成塔出塔氣中含甲醇體積比為4.42%，生產(chǎn)測(cè)得CH4的生產(chǎn)在計(jì)算中忽略不計(jì)。甲醇中間槽氣體溶解損失及馳放氣中甲醇擴(kuò)散損失忽略不計(jì)。其它數(shù)據(jù)以工廠實(shí)際收集為準(zhǔn)。1.2甲醇的生產(chǎn)總量根據(jù)粗甲醇的質(zhì)量組成（CH3OH：96.9%；H2O：3.1%.），算得甲醇中間槽的各組分含量（一年按330計(jì)算），年產(chǎn)粗甲醇為10萬(wàn)噸。甲醇年產(chǎn)量：100000噸/年×96.9%=96900噸/年=12234.84kg/h=382.33kmol/h=8565.76Nm3/h水：100000噸/年×3.1%=3100噸/年=391.41kg/h=21.75kmol/h=487.2Nm3/h表6甲醇合成塔產(chǎn)品組成組分甲醇水合計(jì)質(zhì)量分率%96.13.9100摩爾產(chǎn)量kmol/h382.3321.75404.08流量Nm3/h8565.76487.29052.96根據(jù)醇后氣的流量及各組分的摩爾分率求各組分的流量。CH3OH醇后氣=47224Nm3/h×0.02%=9.44Nm3/hH2醇后氣=47224Nm3/h×71.27%=33656.54Nm3/hN2醇后氣=47224Nm3/h×23.8%=11239.31Nm3/hCO醇后氣=47224Nm3/h×3.82%=1803.97Nm3/hCO2醇后氣=47224Nm3/h×0.34%=160.56Nm3/hCH4醇后氣=47224Nm3/×0.75%=354.18Nm3/h表7醇后氣組成組分名稱CH3OHH2N2COCO2CH4合計(jì)流量（Nm3/h）9.4433656.5411239.311803.97160.56354.182472224摩爾產(chǎn)量kmol/h0.42150.52501.7580.37.1715.81756.2摩爾比率%0.0271.2723.83.820.340.75100根據(jù)稀醇水的質(zhì)量流量以及各組分的質(zhì)量組成求各組分的流量已知出凈醇塔稀醇水為1234.2kg/h。其質(zhì)量組成：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求粗甲醇總產(chǎn)量=8565.76+9.44+164.19=8739.39Nm3/h1.3進(jìn)凈醇塔氣體流量及組分摩爾分率圖凈醇塔氣體流向圖CH3OH凈醇塔=CH3OH醇后氣+CH3OH稀醇水=9.44+164.19=173.63Nm3/hH2凈醇塔=33656.54Nm3/h;N2凈醇塔=11239.31Nm3/h;CO凈醇塔=1803.97Nm3/h;CO2凈醇塔=160.56Nm3/hCH4凈醇塔=354.18Nm3/h表8凈醇塔的出塔氣量及組成組分名稱CH3OHH2N2COCO2CH4合計(jì)流量（Nm3/h）173.6333656.5411239.311803.961803.96354.1847388.18摩爾比率%（%）0.3771.0223.723.810.340.741001.4出塔氣與循環(huán)氣圖甲醇分離器氣體流向圖循環(huán)中甲醇含量＝（醇后氣甲醇含量+烯醇水中甲醇含量）/（醇后氣量+烯醇水中甲醇含量）＝（9.4+164.15）/（47224+164.15）＝0.37%設(shè)出塔氣量為XNm3/h,循環(huán)氣量為YNm3/h，則4.42%X=47224+164.19+8565.76+Y解 X=210294.59（Nm3/h）Y=154340.64（Nm3/h）求得循環(huán)氣中各組分流量：CH3OH循環(huán)氣=154340.64×0.0037=571.06Nm3/hH2循環(huán)氣=154340.64×0.7102=109612.72Nm3/hN2循環(huán)氣=154340.64×0.2372=36609.60Nm3/hCO循環(huán)氣=154340.64×0.0381=5880.38Nm3/hCO2循環(huán)氣=154340.64×0.0034=524.76Nm3/hCH4循環(huán)氣=154340.64-571.06-109612.72-36609.60-5880.38-524.76=1142.12Nm3/h表9循環(huán)氣各組分流量及摩爾分率表組分名稱CH3OHH2N2COCO2CH4合計(jì)流量（Nm3/h）571.06109612.7236609.605880.38524.761142.12154340.64摩爾比率%0.3771.0223.723.810.340.74100求得出塔氣各組分流量：CH3OH出塔氣=8565.76+164.19+571.06+9.44=9310.45Nm3/hH2出塔氣=109612.72+33656.54=143269.22 Nm3/hN2出塔氣=36609.60+11239.31=47848.91Nm3/hCO出塔氣=5880.38+1803.97=7684.35Nm3/hCO2出塔氣=524.76+160.56=685.32Nm3/hCH4出塔氣=1142.12+354.18=1496.3Nm3/h表10出塔氣各組分流量及摩爾分率表組分名稱CH3OHH2N2COCO2CH4H2O合計(jì)流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩爾比率%（%）4.4267.9722.703.650.320.710.231001.5新鮮氣組成及計(jì)算1）新鮮氣各組分的摩爾比率CH3OH：0.02%，H2：71.27%N2：23.8%，CO：3.82%CO2：0.34%，CH4：0.75%。CH4忽略不計(jì)。醇后氣流量47224Nm3/h。CO+2H2→CH3OH+102.5KJ/mol在反應(yīng)中，已知出塔氣中甲醇的生成量為9310.45Nm3/h，則CO的消耗量為9310.45Nm3/h，H2的消耗量=18620.9Nm3/h。CO2+H2→CO+H20-42.9kJ/mol已知甲醇中間槽中H2O的流量為487.2Nm3/h，則CO的生成量為487.2Nm3/h，CO2的消耗量為487.2Nm3/h，H2的消耗量為487.2Nm3/h。反應(yīng)所消耗與生成氣體量如下表所示：表11反應(yīng)所消耗及生成氣體中流量表反應(yīng)消耗量（Nm3/h）反應(yīng)生成量（Nm3/h）COCO2H2CH3OHCO主反應(yīng)9310.45\18620.99310.45\副反應(yīng)\487.2487.2\487.2合計(jì)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組分名稱H2N2COCO2CH4合計(jì)流量（Nm3/h）52764.6411239.3110627.21647.76354.1875633.1摩爾比率（%）69.7614.8614.050.860.47100表12新鮮氣各組分流量及摩爾分率表1.6混合氣的各組分流量混合氣=新鮮氣+循環(huán)氣CH3OH混合氣=571.06Nm3/h，H2混合氣52764.64+109612.72=162377.36Nm3/h，N2混合氣=11239.31+36609.60=47848.91Nm3/h，CO混合氣=10627.21+5880.38=16507.59Nm3/h，CO2混合氣=647.76+524.76=1172.52Nm3/h，CH4混合氣=1142.12=1496.3Nm3/h，表13混合氣各組分流量及摩爾分率表組分名稱CH3OHH2N2COCO2CH4合計(jì)流量（Nm3/h）571.06162377.3647848.9116507.591172.521496.3229973.74摩爾比率（%）0.2370.6120.817.180.520.651001.7物料衡算總表表1410萬(wàn)噸/年粗甲醇的物料衡算總表CH3OHH2N2COCO2CH4H2O合計(jì)新鮮氣流量（Nm3/h）\52764.6411239.3110627.21647.76354.18\75633.1摩爾比率(%)\69.7614.8614.050.860.47\100循環(huán)氣流量（Nm3/h）571.06109612.7236609.605880.38524.761142.12\154340.64摩爾比率%）0.3771.0223.723.810.340.74\100進(jìn)濾油器混合氣體流量（Nm3/h）571.06162377.3647848.9116507.591172.521496.3\229973.74摩爾比率（%）0.2370.6120.827.180.520.65\100進(jìn)合成塔氣體流量（Nm3/h）571.06162377.3647848.9116507.591172.521496.3\229973.74摩爾比率（%）0.2370.6120.817.180.520.65\100出合成塔氣體流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩爾比率（%）4.4267.9722.703.650.320.710.23100進(jìn)廢熱鍋爐氣體流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩爾比率（%）4.4267.9722.703.650.320.710.23100CH3OHH2N2COCO2CH4H2O合計(jì)進(jìn)預(yù)熱器氣體流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩爾比率(%)4.4267.9722.703.650.320.710.23100進(jìn)水冷器物料流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩爾比率（%）4.4267.9722.703.650.320.710.23100進(jìn)分離器物料流量（Nm3/h）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩爾比率（%）4.4267.9722.703.650.320.710.23100進(jìn)甲醇中間槽物料流量（Nm3/h）8565.76\\\\\487.29052.96摩爾比率（%）94.62\\\\\5.38100進(jìn)凈醇塔氣體流量（Nm3/h）173.6333656.5411