馏段:Р Р提镏段操作线方程:Р相平衡方程为:Р板效率及实际塔板数的确定Р(1)求Р平均温度= = 87.15 (C)下РμA= 0.449mpas μB=0.3281 mpasР则μL=+(1-)Р=0.17×0.449+(1-0.17)×0.3281Р =0.3487mpasР = 2.35×0.3487=0.8194Р(2)求板效率ETР由=0.8194,由《化工原理(下)》118页图10-20查得 ET=51%,Р(3)求实际板数Р由乙醇—水X—Y相平衡图,精馏段,提馏段操作线方程,q线方程作出Р附图1,并求出塔板数,可知精馏段理论板数:=13 块Р 提馏段理论板数:=5 块Р由,有Р精馏段实际板数: N精= 13/0.51 26 (块)Р提馏段实际板数: N提= 5/0.51 10 (块)Р全塔板数: N= 36 块Р2.2 精馏段物性衡算Р2.2.1物料衡算Р操作压强 P = 101.325Р温度 t t=78.30C t=90C t=96.00CР t=CР定性组成Р(1)塔顶 y= X= 0.826 查平衡曲线得到 x=0.810Р(2)进料 y=0.355 x=0.0639Р平均分子量查附表知:Р(1)塔顶:=0.82646.07+(1-0.826)18.02=41.20()Р=0.81046.07+(1-0.810)18.02=40.73()Р(2)进料: =0.35546.07+(1-0.355)18.02=27.98()=0.063946.07+(1-0.0639)18.02=19.81()Р平均分子量===34.59()===30.27()Р平均密度由和:1/=a/+a/ A为乙醇 B为水Р塔顶:在78.30℃下:=744.289() =972.870()Р=0.9241/744.289+(1-0.9241)/972.870 则=758.716(