乙醇精馏塔设计

1、基础数据摩尔质量MA=46.07MB=18.02进料含量Wq=0.25塔顶含量WD=0.94塔底含量WW=0.001处理量F=2.36t/h摩尔分率Xq=0.115XD=0.86XW=0.0004进料MF=21.26kg/kmol塔顶出料MD=42.13kg/kmol塔底出料MW=18.03kg/kmol2、进料FF=111.08kmol/h塔顶出料FD=14.86kmol/h塔底出料FW=96.22kmol/h3、塔板数气相液相气相液相99.90.0040.0538227.356.4499.80.040.5181.333.2458.7899.70.050.7780.642.0962.2299.50.121.5780.148.9264.799.20.232.979.8552.6866.28990.313.72579.561.0270.2998.750.394.5179.265.6472.7197.650.798.7678.9568.9274.6995.81.6116.3478.7572.3676.9391.34.1629.9278.675.9979.2687.97.4139.1678.479.8281.8385.212.6447.4978.2783.8784.9183.7517.4151.6778.285.9786.482.325.7555.7478.1589.4189.41在上图对角线上，自点c（0.115,0.115）作垂线ec即为q线，该线与相平衡线的由a点引出的切线的交点坐标为Yd=0.354Xq=0.1152.123.17L=R*FD=47.16kmol/h62.02kmol/h62.14kmol/hV'=V=62.02kmol/h15精馏段=123塔板效率TD=78.5℃TF=85.5℃TD=99.5℃Yd=0.864Yf=0.461Yw=0.002αd=1.04αf=6.56αw=5.12α=3.27查手册：塔顶μA=0.501mPa·sμB=0.36mPa·sμD=0.479mPa·s进料板μA=0.45mPa·sμB=0.32mPa·sμF=0.3745mPa·s塔底μA=0.34mPa·sμB=0.29mPa·sμW=0.290mPa·s平均粘度μDW=0.381mPa·sα*μDW=1.24mPa·sEO=0.47提馏段（不包括再沸器）=R=1.55Rmin=精馏段操作线方程为对应气液平衡可查得提馏段操作线方程为图解法求理论板层数由乙醇—水的气液两相平衡图【1】可查得L′=L+XF=平均摩尔质量物料摩尔流量最小回流比Rmin=精馏塔的气、液相负荷表1乙醇—水系统t—x—y数据乙醇摩尔数/%乙醇摩尔数/%沸点t/℃沸点t/℃V=(R+1)*FD=采用图解法求理论板层数，结果见上图，得理论塔板数N=全塔液体平均粘度的计算：查oconnell关联图206.0761.0860.091.6181.1491.6110.47xxxVDxVLyD001.0555.20004.091.6130.9691.6121.158′''''''xxxVWxVLyW0.52N精馏=12/0.52=23N提馏=3/0.52=6N=29操作压力PD=105.3KpaΔP=0.7KpaPF=121.5KpaP精平均=113.4Kpa操作温度TD=78.5℃TF=85.5℃T精平均=82℃摩尔流量X1=0.848kg/kmolMDMV=42.13kg/kmolMDML=41.81kg/kmolXq=0.115Yq=0.461进料板YF=0.415kg/kmolXF=0.085kg/kmolMFMV=28.83kg/kmolMFML=19.86kg/kmolMMV=35.48kg/kmolMML=30.83kg/kmol密度1.36kg/M3624.93kg/M3ρDA=611.00kg/M3ρDB=972kg/M3WF=0.192ρFA=505.00kg/M3ρFB=867kg/M3762.15kg/M3693.54kg/M3σDA=17.3mN/mσDB=62.9mN/mσDML=23.70mN/mσDA=15.9mN/mσDB=60.4mN/mσDML=56.62mN/mσDML=40.16mN/mμL精馏=0.427mPa·s塔径计算精馏段V精馏=0.45M3/SL精馏=0.0006M3/S0.400.06HT-hL=0.34m查图得C20=0.073C=0.084νmax=1.89m/s1.32m/sD提=0.52m0.8m塔截面积A=0.50㎡实际空塔气速ν=0.89m/s史密斯关联图横坐标=塔顶温度78.5℃精馏段密度ρML=液体平均表面张力提馏段塔径计算，所需数据可从相关手册查得，方法同精馏段。计算结果为比较精馏段与提馏段计算结果，两段的塔径相差不大，圆整塔径，取D=取安全系数为0.7，则空塔气速ν=0.66m0.033取板间距HT=液层高度hl=精馏塔的塔体工艺尺寸计算由XD=Y1=0.860，查平衡曲线（x-y图），得实际塔板数工艺条件及有关物性数据从乙醇-水溶液的气液相平衡图查得泡点温度为：筛板塔全塔效率相对值为1.1，故E=1.1*EO=由图解理论板（x-y图），得精馏段平均摩尔质量气相平均密度ρMDV=PMMMV/RTM=液相平均密度ρMDL=精馏段液相平均粘度进料板温度87.3℃精馏段平均表面张力液相平均表面张力依下式计算，即塔顶温度78.5℃进料板温度87.3℃进料板密度ρMFL=iiLmxVVLCumax2.02020LCC21VLssVLν4精馏VD塔高计算人孔数=N/6=50.5m0.6m塔顶间距=1.7HD=0.681.2m封头H10.375m裙座H21m进料板间距HF=设置人孔板间距Hm=塔底空间高度HB=21mm2）1（HHHHHNHNHNNNHBDmFFTF