得 y yx 47 .1 47 .2??用精馏段操作线和相平衡方程进行逐板计算 1D y x ?=0.983 , 1 1 1 1 1 1 1 (1 ) 2.475(1 ) y y x y y y y ? ???? ??=0.959 苯-甲苯连续精馏筛板塔的设计 10 970 .0 426 .0 567 .0 12???xy , 959 .0 47 .1 47 .2 2???y yx 953 .0 426 .0 567 .0 23???xy ,891 .047 .147 .2 3 3???y yx931 .0426 .0567 .0 34???xy ,845 .047 .147 .2 4 4???y yx 905 .0 426 .0 567 .0 45???xy , 795 .0 47 .1 47 .2 5 5???y yx 877 .0 426 .0 567 .0 56???xy , 742 .0 47 .1 47 .2 6 6???y yx 因为,780 .0742 .0 6??? Fxx 故精馏段理论板 n=5 ,用提留段操作线和相平衡方程继续逐板计算 811 .0 426 .0 567 .0 67???xy , 635 .0 47 .1 47 .2 7 7???y yx 693 .0 426 .0 567 .0 78???xy , 478 .0 47 .1 47 .2 8 8???y yx 519 .0 426 .0 567 .0 89???xy , 304 .0 47 .1 47 .2 9 9???y yx326 .0426 .0567 .0 910???xy , 164 .0 47 .1 47 .2 10 10???y yx
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