甲胺生產(chǎn)工藝中的回收塔物料衡算和熱量衡算計(jì)算案例1.1物料衡算進(jìn)料量及其組成與脫水塔釜液一樣，如下所示：表3?72甲醇回收塔進(jìn)料量及其組成Table3?72InletQuantityandItsCompositionofMethanolRecoveryTower甲醇的收率為80%。餾出液的組成如下：表3?73甲醇回收塔餾出液的組Table3?73GroupofDistillateofMethanolRecoveryTower組分NH3MMADMACH3OHH2OΣwt/(%)0.503.504.0090.002.00100.00設(shè)塔頂?shù)姆趴論p失為進(jìn)料量（除水外）的31%，其組成如下：表3?74甲醇回收塔放空組成Table3?74Emptycompositionofmethanolrecoverytower組分NH3MMADMACH3OHΣwt%3.7026.3033.0037.00100.00餾出液組成：餾出液量為表3?75甲醇回收塔餾出液組成Table3?75Compositionofmethanolrecoverytower組分NH3MMADMACH3OHH2OΣwt/(%)0.503.504.0090.002.00100.00kg/h0.060.420.5410.810.2412.0112kmol/h0.0040.0140.0120.3370.0130.38mol/(%)0.913.642.7389.093.64100.00放空損失量：其組成為：表3?76甲醇回收塔放空組成Table3?76Emptycompositionofmethanolrecoverytower釜液組成：釜液量：其組成為表3?77甲醇回收塔釜液組成Table3?77CompositionofMethanolRecoveryTower物料平衡表表3?78甲醇回收塔物料平衡表Table3?78MaterialBalanceTableofMethanolRecoveryTower組分進(jìn)塔（kg/h）出塔（kg/h）進(jìn)料液餾出液釜液放空量NH30.6040.060.2970.24MMA2.420.420.7971.72DMA3.01940.540.322.16CH3OH15.09710.810.572.52H2O1186.620.241186.38-總計(jì)1207.761207.761.2熱量衡算（1）塔頂熱量衡算塔頂冷凝器放空量即甲醇回收塔餾出液組成：表3?79甲醇回收塔餾出液組成Table3?79DistillateCompositionofMethanolRecoveryTower取回流比R=60；塔頂操作壓力為6Kg/cm2。上升蒸汽量V：由R=LL=R×D=60×12.01=720.6kg/hV=L+D=720.6+12.01=732.61kg/h表3-80脫氨塔塔頂上升蒸汽表Table3-80RisingSteamattheTowerTopoftheDeaminationTower組分NH3MMADMACH3OHH2O總和wt(%)0.53.54902100kg/h3.6625.6429.3659.3514.65732.61回流液量L：L依次推得：表3-81脫氨塔塔頂冷凝器回流液組成表Table3-81compositionofrefluxliquidintopcondenserofammoniatower組分NH3MMADMACH3OHH2O總和wt(%)0.53.54902100kg/h3.625.2228.76648.5414.411048.26塔頂蒸汽塔頂蒸汽：60℃NH30.21kmol/hMMA0.83kmol/hDMA0.65kmol/hCH3OH20.58kmol/hH2O0.81kmol/h餾出：60℃NH30.005kmol/hMMA0.020kmol/hDMA0.016kmol/hTMA0.491kmol/hH2O0.019kmol/h塔頂回流：55℃NH30.21kmol/hMMA0.81kmol/hDMA0.64kmol/hCH3OH20.24kmol/hH2O0.7997kmol/h圖4-12塔頂冷凝器熱量衡算圖Figure4-12HeatBalanceDrawingofTowerTopCondenser由aspen模擬計(jì)算得出的圖形可知，泡點(diǎn)溫度為15℃；露點(diǎn)溫度為30℃。則取餾出液溫度t各組分在15℃時(shí)的汽化潛熱△H表3?82各組分在15℃時(shí)的汽化潛熱△H（單位：cal/kmol)Table3?82Vaporizationlatentheat△Hofeachcomponentat55℃(unit:cal/kmol)組分NH3MMADMATMAH2O△H（15℃）4167.525173.455387.024738.8810206.2表3?83不同溫度下部分組分汽、液體比熱值表（單位：cal/kmol·℃)Table3?83Specificcalorificvalueofsomecomponentsatdifferenttemperatures(unit:cal/kmol·℃)組分NH3MMADMACH3OHH2OCP（0℃，g）8.1110.326514.3219.4537.998CP（7.5℃，g）8.23611.986815.69820.56828.00416CP（15℃，g）8.324712.373516.508721.3738.0105CP（30℃，g）8.5258213.795317.113722.21298.02516由辛普森公式Q=(b?a)①0-15℃下：q=qqqq=②0-30℃下：q=q=q=q=q=塔頂蒸汽帶入冷凝器的熱量Q入熱：NH330℃(g)NHNH330℃(g)NH30℃(g)MMA30℃(g)MMA0℃(gMMA30℃(g)MMA0℃(g)CH3OH30℃(g)CHCH3OH30℃(g)CH3OH0℃(g)DMA30℃(g)DMA0℃(g)（）（）DMA30℃(g)DMA0℃(g)（）（） H2O30℃(g)HH2O30℃(g)H2O0℃(g)QQQQQQ回流液熱量Q回流：QQQQQQ餾出氣體熱量Q餾出：QQQQQQ冷凝器帶走Q冷凝：Q熱量平衡表表3?88甲醇回收塔塔頂冷凝器熱量平衡表(單位：KJ/h）Table3?88HeatBalanceTableforTopCondenserofMethanolRecoveryTower(KJ/h)輸入(KJ/h)輸出(KJ/h)塔頂蒸汽進(jìn)料Q入熱13953.986回流液Q回流-28539.514餾出Q餾出355.808冷凝器帶走Q冷凝42137.629共計(jì)13953.986共計(jì)13953.986（2）甲醇回收塔總塔熱量衡算計(jì)算基準(zhǔn)：以0℃，1h的NH由Aspen模擬計(jì)算得出泡點(diǎn)溫度為119表Table3?76Specificheatvalueofeachcomponentliquidatdifferenttemperatures(unit:cal/kmol?K)組分NH3MMADMATMACH3OHH2OCp（55℃）22.1220.8117.9829.6635.4622.12Cp（79℃）22.8821.4618.0030.4736.422.88Cp（115℃）26.3424.2118.1235.0139.1126.34Cp（119℃）28.8225.5518.2436.2342.928.82Cp（0℃)19.5318.2616.1127.3832.4520.11（1）各組分單量熱量：由辛普森公式Q=(b?a)①0-119℃下：q=qqqq②0-60℃下：q=qqqq（2）進(jìn)料液帶入塔的熱量Q進(jìn)料：QQQQQQ（3）釜液帶走的熱量Q釜液：QQQQQQ（4）放空物料帶走的熱量Q放空：QQQQQ（5）餾出液帶走熱量Q餾出：Q（6）回流液熱量Q回流：Q（7）冷凝器帶走熱量Q冷凝：Q（8）加熱蒸汽帶入熱量Q加熱蒸汽：Q(9)熱量平衡表表3?92甲醇回收塔全塔熱量平衡表(單位：KJ/h）Table3?92He