甲胺生產(chǎn)工藝中的分離塔物料衡算和熱量衡算計(jì)算分離塔MMA226.45kg/hDMA227.50kg/hTMA10.45kg/hNH32.526kg/h分離塔MMA226.45kg/hDMA227.50kg/hTMA10.45kg/hNH32.526kg/hH2O1.393kg/hMMA？DMA？TMA？NH3？CH3OH？MMA？DMA？TMA？NH3？H2O？餾出液進(jìn)料測(cè)線采出釜液MMA？DMA？TMA？NH3？CH3OH？表3?54分離塔進(jìn)料組成Table3?54Feedcompositionoftheseparationtower組分NH3MMADMATMAH2O總和wt(%)0.53948.3548.582.230.297100.000kg/h2.526226.45227.5010.451.393468.319由MMA單程收率95%得出：分離塔塔頂餾出MMA量為：238.234×0.95=226.32kg/h根據(jù)塔頂產(chǎn)品規(guī)格為MMA含量98%，得出：餾出液的量D1=226.32/0.98=230.94kg/h表3?55分離塔餾出液組成Table3?55Distillatecompositionoftheseparationtower組成NH3MMADMATMA總計(jì)wt％0.2098.000.601.20100.00kg/h0.464226.321.3862.77230.94kmol/h0.0277.2870.030700477.3917mol％0.3698.590.410.64100.00根據(jù)產(chǎn)量要求，（182.291kg/h）得出下表：表3?56分離塔MMA產(chǎn)品產(chǎn)出組成Table3?56ProductOutputCompositionofMMAintheSeparationTower組成NH3MMADMATMA總計(jì)wt％0.2098.000.601.20100.00kg/h0.372182.2911.1162.232186.011根據(jù)DMA單程收率為94%，得出側(cè)線產(chǎn)出DMA量為：238.234×0.94=223.94kg/h由產(chǎn)品規(guī)格可以得出側(cè)線產(chǎn)出量得出下表：表3?57分離塔側(cè)線產(chǎn)出組成Table3?57OutputCompositionofSeparationTower放空損失量：G損由上計(jì)算釜液W=F?NH表3?58分離塔放空組成Table3?58Separationtoweremptyingcomposition組分NH3MMADMATMA總和wt(%)6.166.2422.615.05100kg/h0.3873.101.060.2364.683表3?59分離塔釜液組成表Table3?59Compositiontableofseparationtowerkettleliquid組成NH3MMADMAH2O總計(jì)wt％3.53813.7815.7968.81100.00kg/h0.010.991.0264.476.496kmol/h----0.02280.2480.2708mol％----8.4291.58100.00按（182.291kg/h）MMA計(jì)算，其組成如下：表3?60分離塔每小時(shí)采出MMA成品量Table3?60VolumeoffinishedMMAsproductproducedperhoureparationtower組分NH3MMADMATMA總和wt(%)0.2098.000.601.20100.00kg/h0.372182.2911.1162.23186.011表3?61分離塔每小時(shí)返回合成配料的MMA量Table3?61MMAoftheseparationtowerreturnedtothesyntheticingredientperhour組分NH3MMADMATMA總和wt(%)0.2098.000.601.20100.00kg/h0.09244.0290.270.5444.931綜上，得出分離塔物料衡算一覽表：表3?62分離塔物料平衡表Table3?62Materialbalancetableofseparationtower組分進(jìn)塔（kg/h）出塔（kg/h）進(jìn)料量MMA成品量MMA返回合成量DMA側(cè)線采出量釜液放空量NH32.5260.3720.0920.2260.010.387MMA226.45182.29144.0290.67860.993.10DMA227.501.1160.27223.941.0261.06TMA10.452..2320.541.131-0.236H2O1.393--0.2264.47-總計(jì)486.319186.01144.931226.26.4964.683物料守恒486.319486.5081.2熱量衡算（1）塔頂熱量衡算計(jì)算基準(zhǔn)：以0℃，1h時(shí)的NH3(l)、MMA(l)、DMA(l)、TMA(l)、CH3OH(l)、H2O(l)為基準(zhǔn)已知數(shù)據(jù)（1）塔進(jìn)料量、回流、餾出量、釜液量由物料衡算可知。（2）塔操作參數(shù)：①塔頂壓力：（表壓）②回流比：塔頂R塔頂冷凝器放空量即分離塔餾出液組成表3?63塔頂冷凝器放空量組成Table3?63CompositionofTowerTopCondenser上升蒸汽量V：由L=R×D=12×230.94=2771.28kg/hV=L+D=2771.28+230.94=3002.22kg/h表3-64分離塔塔頂蒸汽表Table3-64SteamTableofSeparationTower組分NH3MMADMATMA總和wt(%)0.2098.000.61.20100.000kg/h6.002942.1818.0136.033002.22Kmol/h0.3594.730.401.1296.61Mol(%)0.3698.050.411.16100.00回流液量L：LLMMA=LDMA=LTMA=表3?65分離塔塔頂冷凝器回流液組成表Table3?65compositionofrefluxliquidintopcondenserofammoniatower由Aspen模擬得到泡點(diǎn)溫度為38℃，露點(diǎn)溫度為38℃，查圖表求得，將不同溫度下各組分液體比熱值列與下表中：組分NH3MMADMATMACP（0℃，g）8.33611.96315.93520.580CP（38℃，g）8.58113.02317.44622.676CP（20℃，g）8.45912.51316.70721.648各組分汽化潛熱ΔH如下：組分NH3MMADMATMA△H（38℃）4510.65503.325732.474982.41頂冷凝器的衡算：塔頂冷凝器衡算圖Balancecalculationdiagramofthetowertopcondenser各組分單量熱量：由辛普森公式Q=(b?a)①0-38℃下：q=qqq塔頂蒸汽帶入冷凝器的熱量Q入熱：QQQQQ回流液熱量Q回流：QQQQQ餾出氣體熱量Q餾出：QQQQQ冷凝器帶走Q冷凝：Q熱量平衡表表3?68分離塔塔頂冷凝器熱量平衡表(單位：KJ/h）Table3?68HeatBalanceTableforTopCondenserofExtractionTower(KJ/h)輸入(KJ/h)輸出(KJ/h)塔頂蒸汽進(jìn)料Q入熱46224.46回流液Q回流6665.08餾出Q餾出6850.75冷凝器帶走Q冷凝32708.63共計(jì)46224.46共計(jì)46224.46（2）分離塔總塔熱量衡算圖4?10分離塔總塔熱量衡算圖Fig.4?10CalculationofTotalTowerofSeparationTower表3?69分離塔進(jìn)料組成Table3?69Feedcompositionoftheseparationtower組分NH3MMADMATMAH2O總和wt(%)0.53948.3548.582.230.297100.000kg/h2.526226.45227.5010.451.393468.319kmol/h0.1487.2915.0470.1770.07713.425mol(%)1.10254.3137.591.320.57100.00由Aspen模擬得出泡點(diǎn)溫度52℃，露點(diǎn)溫度為106℃，所以計(jì)算如下P表PP絕壓=P表+組分NH3MMADMATMAH2OCp（0℃）19.3226.5933.2833.82818Cp（18℃）20.1227.2134.7934.2318Cp（52℃）20.3728.3735.8735.118Cp（106℃）27.3731.3140.0539.818.22（1）各組分單量熱量：由辛普森公式Q=(b?a)①0-52℃下：q=qqqq②0-106℃下：q=qqqq（2）進(jìn)料液帶入塔的熱量QQQQQQQ（3）釜液帶走的熱量QQQQQ（4）側(cè)線采出物料帶走的熱量QQQQQQQ（5）放空物料帶走的熱量QQQQQQ（6）餾出液帶走熱量Q餾出：Q（7）回流液熱量Q回流：Q（8）冷凝器帶走熱量Q冷凝：Q（9）加熱蒸汽帶入熱量Q加熱蒸汽：Q（10）熱量平衡表