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qα13.650tF(℃）82.35RminR是Rmin的几倍1.5392.60精馏段截距0.166082104理论板数NT板效率ET11.6170.5001精馏段LSVS0.003242.20652TcmT1538.38298.15检验：AT1.54弓形单流降液管lw是D的几倍0.65塔板布置孔径d00.0045弓形降液管宽度Wd0.168筛孔个数n8157.73性能校核板压降溢流液泛精馏塔的工艺设计塔及塔板结构计算气泡夹带液沫夹带严重漏液提馏段LSVS0.001660.00000TcmT1645.95298.15检验：AT0.79弓形单流降液管lw是D的几倍0.6塔板布置孔径d00.005弓形降液管宽度Wd0.100筛孔个数n3441.36性能校核板压降溢流液泛气泡夹带液沫夹带严重漏液精馏段严重漏液线负荷性能图液体流量下限线液体流量上限线过量雾沫夹带线0.057445705溢流液泛线提馏段严重漏液线液体流量下限线液体流量上限线过量雾沫夹带线0.05155907溢流液泛线塔高的计算精馏段板数23H19.9液体停留时间（min)10H61.264833271总高h19.28983327管道尺寸塔顶蒸汽Vs2.206517514塔顶回流Ls0.003243366进料Ls0.000728993塔釜蒸汽Vs0釜液Ls0.001655663原料罐的设计每罐排空时间8V26.24374708原料泵的选型原料温度（℃）25体积流量2.614592745P2/ρg1.807806545体积流量2.624374708换热器的选型与设计热量衡算进料带入的热量QF(kw)回流带入的热量QR(kw）塔顶蒸汽带出的热量Qv（kw）残液带出热量QW（kw）加热蒸汽带入的的热量QB（kw）选用120℃水蒸气加热换热器换热器核算33.5u0.667792021设壁温tw50乙醇水混合物进料（质量分数)0.46αDαWXF（摩尔分数）1.1112.000.2500tD(℃）tW(℃）D（kmol/h）78.2897.1555.09D（kg/h）2364.229RL（kmol/h）V（kmol/h）4220.378275.472L（kg/h）V（kg/h）9456.91711821.146L（m3/h）V（m3/h）11.6767943.463L（m3/s）V（m3/s）0.003242.20652实际板数NP（选用再沸器）实际进料位置理论精馏板数21.229420.161840399.5832.9190295450.000810842ρmD液（kg/m3）ρmD气（kg/m3）FLV809.936731.488160.03429T2σ1(达因/厘米）σ2(达因/厘米）351.4322.6416.76An允许气速uu/uF1.431.540.82lw板上层清液高度hL(0.05-0.1m)溢流堰高度hw(0.025-0.05mm)0.910.06000.0440塔板厚度ζ开孔率φt/d00.00350.11572.8Wc（0.05-0.06）鼓泡区半径r出口安定区Ws（0.05-0.07）0.050.650.05A0/Anζ/d0C00.07810.780.77降液管底隙阻力损失hr降液管清液层高度Hd0.0013480.1399小于τAf4.65应该大于3~5s0.1078泡沫层高度hfev0.150.0640应该小于0.1kg液/kg气hσu0M稳定系数K0.0018778.481.996038792ρmD液（kg/m3）ρmD气（kg/m3）FLV955.630960.60222#DIV/0!T2σ1(达因/厘米）σ2(达因/厘米）370.363.8448.30An允许气速uu/uF0.740.000.00lw板上层清液高度hL(0.05-0.1m)溢流堰高度hw(0.025-0.05mm)0.60.05000.0362塔板厚度ζ开孔率φt/d00.00350.10083Wc（0.05-0.06）鼓泡区半径r出口安定区Ws（0.05-0.07）0.050.450.06A0/Anζ/d0C0#DIV/0!0.700.758降液管底隙阻力损失hr降液管清液层高度Hd0.0012760.0998小于τAf2.46应该大于3~5s0.0408泡沫层高度hfev0.1250.0000应该小于0.1kg液/kg气hσu0M稳定系数K0.00412611.860hwlwE0.04400.911.03LhhowhL20.0049450.048970.0113990.055490.0134780.0574180.0213950.0654howElw0.00610.91AfHd0.1080.1399τLsLh30.0050318.096Lhhowhf20.00490.122370.01140.138490.01350.1436180.02140.1634βLhhow0.753140.01800.748150.01880.738170.02050.733180.0212hwlwE0.03620.61.05LhhowhL10.0041920.040470.0153390.051690.0181370.0544110.0207330.05700.0002000.0004000.0006000.0008000.00010000.00012000.00014000.00016000.00005101520howElw0.00610.6AfHd0.0410.2681τLsLh40.002749.855Lhhowhf10.00420.101070.01530.128990.01810.1359110.02070.1424βLhhow0.85370.01490.84480.01630.824100.01900.815110.0202提馏段板数31.2~1.5mH2H3H410.3751.355~15min2~3mH7H8Δ30.750.45假设流速u内径d圆整d12483.98435速度核算u实际内径d14.72437假设流速u内径d圆整d245.4545速度核算u实际内径d2.2343假设流速u内径d圆整d221.5528速度核算u实际内径d1.1828假设流速u内径d圆整d130.00430速度核算u实际内径d0.00#DIV/0!假设流速u内径d圆整d232.4734速度核算u实际内径d1.8833.5装料系数高/径（1.2~1.8）体积流量0.81.52.624374708H罐DH液体4.2205867312.8137244883.376469385原料密度原料质量分数乙醇密度886.63208550.46785.0452563Z1Z2ΔZ3.3764693857.2148332713.838363886ε(无缝钢管)ε/dλ0.150.0053571430.033ξ1标准截止阀ξ2两个弯头ξ3突然扩大6.41.51选泵IS150-32-125转速nr/min流量m3/h扬程Hm29007.522tF质量分数Cp水82.350.464.1985tr质量分数Cp水78.280.926td质量分数Cp水78.280.9264.1941tw质量分数Cp水97.150.0254.2163QBQL3684.815548368.4815548rWCB2258.46781.631555494加热蒸汽热量(kw)3684.815548kg/h5873.59978Qc冷却水进口温度t1冷却水出口温度t23094.8913432245Δt1Δt256.2833.28设K(700~800)计算A取A80088.3696799572.2外径d10.019tTμ33.5306.650.000762566uRePr0.66779202113040.837955.158045914设壁温twλdm500.2415017930.016921277温度密度ρ乙醇50749.1653266水337.29984.3043873混合物64.14761.9060719进入系统的热量塔顶（质量分数)塔釜（质量分数)1250.9260.025425.554.966887417XD（摩尔分数）XW（摩尔分数）MDMF0.83040.009942.91225.500F（kmol/h）W（kmol/h）ρmD液（kg/m3）ρmF液（kg/m3）90.91124.34809.94883.33F（kg/h）W（kg/h）μmD液（cP）μmF液（cP）2318.1822275.1980.470.37L'（kmol/h）V'（kmol/h）ρmD气（kg/m3）μmF液（cP）311.287275.4721.4881602860.37L'（kg/h）V'（kg/h）c2h5oh5695.9300.000798.8539548799.2150875L'（m3/h）V'（m3/h）h2o5.9600.000970.7720216973.3313252L'（m3/s）V'（m3/s）0.001660.000000.0011320830.001234664883.3272973809.936731790.9090909155.094422492.6243747082.3808329040.0007289930.000661342HT(m)C20C液泛气速uF0.450.0840.08111.8898塔有效截面积An单流型塔板溢流堰Af/ATAT1.67lw=0.65D0.071.79应该在0.65-0.85间Lh收缩系数ELh/(lw^2.5）how11.681.0314.780.0160t0.0126x鼓泡区面积AaA0u00.48201.1260.13016.94干板压降hd气体动能因子Fa充气系数β泡沫层压降he0.04532.390.550.03330.5（HT+hw）0.2470应该大于1.5~2.0HT(m)C20C液泛气速uF0.50.080.09543.8001塔有效截面积An单流型塔板溢流堰Af/ATAT0.00lw=0.6D0.0520.00应该在0.65-0.85间Lh收缩系数ELh/(lw^2.5）how5.961.0521.370.0138t0.015x鼓泡区面积AaA0u00.34000.6730.0680.00干板压降hd气体动能因子Fa充气系数β泡沫层压降he0.00000.000.970.04860.5（HT+hw）0.2681应该大于1.5~2.0hσC0ρmD液（kg/m3）ρmD气（kg/m3）0.001880.77809.93673171.488160286u0MVh7.9363722.4152.794414068.2603874.2082.794414068.3623921.8568.7384098.2250Lh11.676118182.79418.096458218.0964582unVh1.93589976.60741.84059485.41361.80989327.18051.69288724.6493hrhphehd0.001940.18310.04660.13650.002230.18200.04700.13500.002860.17970.04750.13220.003200.17860.04780.1308hσC0ρmD液（kg/m3）ρmD气（kg/m3）0.004130.758955.63095790.602222279u0MVh10.89742661.9931.84247080912.01392934.7191.84247080912.27822999.27812.51843057.96600.0002000.0004000.0006000.0008000.00010000.00012000.00014000.00016000.000024681012Lh5.9603862681.8429.8548167929.854816792unVh3.28068793.42