甲胺生產(chǎn)工藝中的脫氨塔設(shè)計(jì)計(jì)算案例圖4-1脫氨塔物料衡算圖Fig.4-1MaterialEquDrawingofDeaminineTower1.1.1物料衡算 ①.已知數(shù)據(jù)表3-5脫氨塔進(jìn)料量及其組成Table3-5InletQuantityandItsCompositionofDeaminationTower組分NH3MMADMATMACH3OHH2O總計(jì)Wt（%）39.7310.0010.0022.820.57216.841100.000Kg/h946.597238.234238.234544.4513.626401.1992382.34Kmol/h55.587.6705.2859.2110.42522.044100.215Mol（%）55.4617.6545.2749.1910.42421.997100.00氨的單程收率為97%；從塔頂蒸出的比例：氨：三甲胺=82：18（質(zhì)量比）；據(jù)餾出液中MMA含量≤2%，釜液中NH3含量≤0.3%。 ②計(jì)算計(jì)算泡點(diǎn)溫度：=0.5799＜1，所以設(shè)泡點(diǎn)溫度為68℃：=0.99744936≈1，所以泡點(diǎn)進(jìn)料溫度為68℃。已知進(jìn)料組分的相對(duì)揮發(fā)度如下表：表3-8進(jìn)料組分的相對(duì)揮發(fā)度Table3-8TheRelativeVolatilityoftheFeedConstituents組分摩爾分?jǐn)?shù)相對(duì)揮發(fā)度NH354.993.15MMA7.651.273DMA9.240.754TMA5.270.700CH3OH0.430.116H2O22.420.029假設(shè)為清晰分割，設(shè)餾出液總量為D、釜液總量為W，則有物料衡算表如下聯(lián)立表中數(shù)據(jù)可算得：D=1238.46kg/h；W=1143.88kg/h。所以物料衡算表如下：芬克斯方程：N計(jì)算餾出液中組分DMA、CH3OH、H2O的摩爾量DDMA=[238.234×(2.48/308.13)×DCHDH則可知組分DMA、CH3OH、H2O的含量均≈0，所以組分DMA、CH3OH、H2O按清晰分割計(jì)算是合理的。③物料衡算表表3-11物料平衡表Table3-11MaterialBalanceTable組分入料（kg/h）出料（kg/h）進(jìn)料量餾出量釜液量NH3946.597912.2834.317MMA238.2342.48235.754DMA238.234-238.234TMA544.45294.632249.818CH3OH13.626-13.626H2O401.199-401.199總計(jì)2382.341209.3921172.948物料守恒2382.342382.234餾出液組成表表3-12脫氨塔餾出液組成Table3-12CompositionofDeamintowerDistillate組分NH3MMATMA總和wt(%)81.320.2226.26100.00kg/h912.282.48294.6321121.796kmol/h53.569007984.98458.6328mol（%）91.360.148.5100.000釜液組成表：1.1.2脫氨塔熱量衡算1.1.2.1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)①塔頂壓力：P=15Kg/cm2（表壓）②回流比：R=4由ASPEN模擬得出混合進(jìn)料即塔頂蒸汽的泡點(diǎn)溫度為33℃，露點(diǎn)溫度為40℃，部分比熱容組分NH3MMATMACP(32.06℃)6.8768.9636.83CP(39.09℃)7.129.1337.75CP(16℃)6.438.6633.21CP(0℃)6.138.3631.65CP(20℃)6.538.7234.15表3-15各組分不同溫度下汽化潛熱（cal/kmol）Table3-15Vaporization(cal/kmol)atDifferentTemperatureofEachcomponent組分NH3MMADMATMACH3OHH2OΔH(32℃)4662.995614.225853.635068.16——ΔH(40℃)4494.715488.585716.374971.758787.610374.47ΔH(66℃)3919.24941.565158.294574.988407.9310098.92ΔH(144℃)-3688.032288.431570.566546.341009033.41H(0℃)5138.846138.656459.065505.169195.6710725.14塔頂冷凝器放空量即脫氨塔餾出液組成：3-16脫氨塔塔頂冷凝器放空量及其組成3-16Deamintowertopcondenserventinganditscomposition組分NH3MMATMA總和wt(%)81.320.2226.26100.00kg/h912.282.48294.6321121.796kmol/h53.569007984.98458.6328mol（%）91.360.148.5100.000上升蒸汽量V：由R=LL=R×D=4×1121.796=4487.184kg/hV=L+D=4487.184+1121.796=5608.98kg/h表3-17脫氨塔塔頂上升蒸汽表Table3-17RisingSteamattheTowerTopoftheDeaminationTower組分NH3MMATMA總和wt(%)81.840.217.96100kg/h4590.3911.221007.375608.98kmol/h269.550.3617.04286.95mol（%）93.9350.12655.94100回流液量L：LLLTMA=表3-18脫氨塔塔頂冷凝器回流液組成表Table3-18CompositionofRefluxofDeaminotowerTopCondenser組分NH3MMATMA總和wt(%)81.840.217.96100kg/h3678.118.74712.7384399.588kmol/h215.9780.28112.058228.314mol（%）94.5970.0125.28100塔頂冷凝器的衡算：4?2脫氨塔塔頂冷凝器熱量衡算圖4?2Heatbalancecalculationdiagramofdeamintowertopcondenser（4）各組分單量熱量：由辛普森公式Q=(b?a)①0-33℃下：q=qq②0-40℃下：q=q=q=（5）塔頂蒸汽帶入冷凝器的熱量Q(入熱)QQQQ（6）回流液熱量Q(回流)NH333℃(l)NH333℃(NH333℃(l)NH333℃(g)NH30℃(g)MMA33℃(l)MMA33℃(g)MMA33℃(l)MMA33℃(g)MMA0℃(g)TMA33℃(l)TMA33℃(TMA33℃(l)TMA33℃(g)TMA0℃(g)QNHQMMAQTMAQ回流（7）餾出氣體熱量Q餾出：NH340℃(g)NHNH340℃(g)NH30℃(g)MMA40℃(g)MMA0℃(gMMA40℃(g)MMA0℃(g)TMA40℃(g)TTMA40℃(g)TMA0℃(g)QQQQ餾出（8）冷凝器帶走Q冷凝Q（9）熱量平衡表圖4-3脫氨塔總塔熱量衡算圖Fig.4-3HeatBalanceCalculationofTotalDeaminizedTower1.1.1.2脫氨塔總塔熱量衡算計(jì)算基準(zhǔn)：以0℃，1h的NHCH（2）P表PP絕壓=由aspen軟件計(jì)算得：混合物進(jìn)料的泡點(diǎn)溫度為：33℃，露點(diǎn)溫度為：144℃。所以使塔釜tW=144℃，進(jìn)料tF=33℃，（3）各組分單量熱量：由辛普森公式Q=(b?a)①0-33℃下：q=qqqqq②0-144℃下：q=q==q=q=（4）進(jìn)料液帶入塔的熱量Q進(jìn)料：NH333℃(l)NHNH333℃(l)NH30℃(l)MMA33℃(l)MMA0℃(lMMA33℃(l)MMA0℃(l)TMA33℃(l)TTMA33℃(l)TMA0℃(l)DMA33℃(l)DMA0℃(lDMA33℃(l)DMA0℃(l)CH3OH33℃(l)CHCH3OH33℃(l)CH3OH0℃(l)H2O33℃(l)HH2O33℃(l)H2O0℃(l)QQQQQQQ（5）釜液帶走的熱量熱量Q釜液：NH3144℃(l)NHNH3144℃(l)NH30℃(l)MMA144℃(l)MMA0℃(lMMA144℃(l)MMA0℃(l)TMA144℃