【《甲醇生产设计计算案例综述》1800字】.docx
甲醉生产设计计算案例综述S1甲去程图1.1设计敷(1)年产IO万吨甲醉。一年按照330天的操作计算。产品粗甲醉的质量组成：CHjOH:(96.9%)；HQ：(3.1%)(其它杂质忽略不计)(2)出净醉塔烯N产水为1234.2kg小，其质量组成为甲酹19%,水81%(3)醇后气流量：47224Nm3小，摩尔分率：CH.OH：0.02%,H2:71.27%N2:23.8%,CO：3.82%CO2：0.34%,CHr0.75%o(4)甲醇合成塔出塔气中含甲醇体积比为4.42%,生产测得CH,的生产在计算中忽略不计。(5)甲博中间槽气体溶解损失及驰放气中甲醉扩散损失忽略不计。其它数据以工厂实际收集为准。1.2甲醉的生产总根据粗甲爵的质fit组成(CHAOH：96.9%：11:0：3.1%.),算得甲醉中间槽的各组分含量(一年按330计算),年产粗甲醇为IO万吨。甲静年产星：I(MXXX)盹/年x96.9%=96900吨，年=12234.84kgh=382.33kno1.h=8565.76Nnrh水：100(XX)吨/年x3.1%=3100卿年=391.41kgh=21.75kmo!=487.2Nm3Zh量6甲合成务产品烟成组分甲醉水合计质量分率96.13.9I(X)摩尔产量kmo1./h382.3321.75404.08流殳NnJh8565.76487.29052.96根据醇后气的流址及各组分的摩尔分率求各组分的流址“CHgH=47224Nm3hx().02%=9.44Nm3ZhH:4*47224Nm3hx71.27%=33656.54Nm3N2wir,=47224Nm3h×23.8%=11239.31Nm3ZhCOn,in=47224Nm3×3.82%=1803.97Nm3ZhC2wi=47224Nm3h×0.34%=160.56Nm3ZhCHJm汽=47224Nm3×0.75%=354.18Nm3Zh组分名称CHsOHH:N:COCO2CHi合计流量9.4433656.5411239.311803.97160.56354.182472224摩尔产量0.42150.52501.7580.37.1715.81756.2kno1.h摩尔比率0.0271.2723.83.820.340.75I(X)根据稀醉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醉水为1234.2kg/h。其质量组成：甲醇：19%,水：81%。求得CHOHMI»«=1234.2x19%=234.5kgh=7.33kom1.h=164.19Nm,h水=1234.2x81%=999.7kgh=55.54kmo1.=1244.07NmVh求粗甲醉总产量=8565.76+9.44+164.19=8739.39Nm3ZhIJ进M塔气体流量及蛆分摩尔分率水一净舒塔_稀防水.醒后气去算先BBAN气体流向图CHgHg*=CHQH内：，廿CHgHIH(IA=9.44+164.19=173.63NmVhHz*33656.54Nm3ZhjN2»»»=11239.31Nm;CO“*=1803.97NmYh;CO>i>wtt=160.56NmVhCH=354.1.8Nm«x*塔的出售气或及组成组分名称CH3OH2N2COCO2CH4合计流量173.6333656.5411239.311803.961803.96354.1847388.18(NmVh)摩尔比率0.3771.0223.723.810.340.741.1.4出塔气与循环气图甲,分M1.气体流图循环中甲醉含量=(醉后气甲解含量+烯醇水中甲醉含量)/(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XNmMK循环气量为YNmVh,则8565.76+0.37%V,+9.44+164.19442%=8565.76+Y+47224+164.19X=47224+164.I9+8565.76+Y解X=210294.59(NmVh)Y=154340.64(NnnZIi)求得循环气中各组分流量：CHxOHMnn=154340.64×0.37=571.06NmyIH2M“气=154340.64×0.7102=109612.72NmN:MX=I54340.64x0.2372=36609.60NnCOM11n=154340.64×0.0381=5880.38Nm3ZhCOiM4i=154340.64×0.(X)34=524.76NmVhCHjm>=154340.64-571.06-109612.72-36609.60-5880.38-524.76=1142.12Nm«9环气鲁Ia分薄一及摩尔分率衰流量<NmVh)组分名称CH1.oHHzN>COCO2CHS合计571.06109612.7236609.6()5880.38524.761142.12154340.64摩尔比率0.3771.0223.723.810.340.74I(X)求得出塔气各组分流量：CH3OH,wv=8565.76+IM.19+571.06+9.44=9310.45NmVhH:109612.72+33656.54=143269.22Nma力N2-=36609.60+I1.239.31=47848.91Nm3ZhCO1.tmn=588O.38+1803.97=7684.35Nm5ZhCO>iumn=524.76+160.56=685.32Nm3ZhCH4"MX=I142.I2+354.I8=1496.3NmVh«10出号气各Ia分M2S尔分率衰1）新鲜气各组分的摩尔比率CfbOH:0.02%,F2：71.27%Nu23.8%,CO：3.82%组分名称CHjOHH:N2COCO:CHqH2O合计流量(NmVh)9310.45143269.2247848.91768435685.321496.3487.2210781.75摩尔比率4.4267.9722.703.650.320.710.23I(X)C2:0.34%,CH4：0.75%aCH4忽略不计。醉后气流5147224NmVh。CO+2H>C1.hOH+102.5KJZmo1.在反应中,已知出塔气中甲醇的生成量为9310.45Nh,则CO的消耗量为9310.45Nm5Zh.112的消耗I=18620.9Nm1Z1.uCOz+Hj>>CO+H>0-42.9kJ/mo1.己知甲醉中间槽中H2O的流量为487.2Nm3小，则CO的生成量为487.2NmVh,CO2的消耗域为487.2Nm,Hi的消耗量为487.2Nmvh。反应所消耗与去成气体衣如卜表所示:*11反应献3生成气体巾灌我反应消耗量（Nmvh）反应生成量Nm,h）COCO:H:CEbOHCO主反应9310.4518620.99310.45副反应487.2487.2487.2合计9310.45487.219108.19310.45487.2Fh,”33656.54+19108.1=52764.64Nm3Zh,N2.»«<=11239.31NmVh,C?O.,4,r=1803.96+9310.45-487.2=1()627.21Nn,CO?,w,1.=160.56+487.2=647.76Nm½,CH4.wn=354.18NmVh«12*气各M分海及摩尔分率衰组分名称H2N2COC02CH4合计潦量52764.6411239.3110627.21647.76354.1875633.1(Nm3Zh)摩尔比率69.7614.8614.050.860.47I(X)(%)1.6混合气的各组分流混合气=新鲜气+循环气CHxOH-=571.06Nm3Zh.Hi,wa-<52764.64+10%12.72=162377.36Nm,N2.wfr<=I1.239.31+36609.60=47848.91NmVh.CO4n=10627.21+5880.38=16507.59Nin3XibCO：,aft1=647.76+524.76=1.172.52Nm.CH4,H*.=354.18+1142.12=1496.3Nm,h.«13震合气各蛆分震及摩尔分率赛组分名称CH30HH2N2COCO2CH4合计潦量(Nm3Zh)571.06162377.3647848.9116507.591172.521496.3229973.74摩尔比率(%)0.2370.6120.817.18().520.65I(X)«141。万励年里甲碘物料*声总表CH1.oHH;N2COCOiCH4H>O合计新鲜气流量(NmVh52764.6411239.3110627.21647.76354.1875633.1摩尔比率(%)69.7614.8614.050.860.47100循环气流S.(NmVh571.06109612.7236609.605880.38524.761142.12154340.64摩尔比率)0.3771.0223.723.810.340.7410()进泄油流ft器混合(NmVh571.06162377.3647848.9116507.591172.521496.3229973.74气体摩尔比率()0.2370.6120.827.180.520.65100进合成流量<NmVh571.06162377.3647848.9116507.591172.521496.3229973.74塔气体摩尔比率（）0.2370.6120.817.180.52().65I(X)出合成流量9310.4514326947848.7684.35685.3214963487.2塔气体<NmVh.2291210781.75摩尔比4.4267.9722.703.650.320.710.23100率（）进废流S1.9310.4514326947848.7684.35685.3214963487.2210781.75热锅(NmVh.2291炉气摩尔比4.4267.9722.703.650.320.710.23I(X)体率（）流量（Nm½）9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.2310()潦量(NnrZh)9310.45143269.2247848.917684.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.23100潦量（Nm3Zh）9310.45143269.2247848.9176R4.35685.321496.3487.2210781.75摩尔比率（%）4.4267.9722.703.650.320.710.23I(X)流量（NnMh）8565.76487.29052.96摩尔比率（%）94.625.38I(X)潦量(Nnr,h)173.6333656.5411239.311803.961803.96354.1847388.18摩尔比率%）0.3771.0223.723.810.340.74I(X)潦量（Nn"h）164.19/I/1244.07140.26摩尔比率11.66/88.34100CHjOHHjN2COCO:CH合计（%）预冷体水器料分器料进热气进冷物进离物甲中槽料进醉间物净塔体酹物进醇气稀水料CHg比N2COCO2CH4Hq合计醇流量：9.443365611231803.9160.56354.1847224后气Nm3Zh).549.316摩尔比率0.0271.2723.83.820.340.75I(X)(%)
