Separation Process Principles- 2n - Seader & Henley - Solutions Manual

9987 y 3 02707 02653 02582 02489 02370 02221 02000

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Unformatted text preview: of nodes are determined using Fig. 11.6: Component or Azeotrope Normal boiling pt., oC Type node n-Hexane 69.0 stable Methanol 64.7 stable Methyl acetate 57.0 stable 50.6 saddle n-Hexane/Methanol n-Hexane/Methyl acetate 51.8 saddle Methanol/Methyl acetate 53.5 saddle n-Hexane/Methanol/Methyl acetate 47.4 unstable A computed residue curve map is given by van Dongen and Doherty, IEC Fundamentals, Vol. 24, 454 (1985). Analysis: (continued) Exercise 11.1 (continued) Subject: acetate. Exercise 11.2 Calculation of a residue curve for the system n-hexane - methanol - methyl Given:. Ternary system n-hexane - methanol - methyl acetate at 1 atm. Assumptions: UNIFAC method for computing K-values. Find: Portion of a residue curve starting from a bubble-point liquid of 20 mol% n-Hexane (1), 60 mol% methanol (2), and 20 mol% methyl acetate (3), at 1 atm. Analysis: The residue curve is computed numerically, in the same manner as in Example 11.1, except that the bubble-point calculations at each step are made with the Chemcad FLASH model. To begin, a bubble point is run with Chemcad on the above initial liquid composition, xi(0), at 1 atm. The computed vapor composition, yi(0), is then used with the Euler form of Eqs. (11-5) and (11-6) to compute xi(1): xi(1) = xi( 0) + xi( 0) − yi( 0) ∆ξ , i = 1 to C -1 The procedure is repeated in steps of ∆ξ = 0.1 in the forward direction from ξ = 0 to ξ = 1, and ∆ξ = -0.1in the backward direction from ξ = 0 to ξ = -1. The results are as follows, with a plot on the following page. ξ -1.0 -0.9 -0.8 -0.7 -0.6 -0.5 -0.4 -0.3 -0.2 -0.1 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 x (1) 0.3277 0.3203 0.3120 0.3027 0.2923 0.2806 0.2676 0.2531 0.2371 0.2194 0.2000 0.1806 0.1597 0.1373 0.1137 0.0894 0.0652 0.0426 0.0233 0.0097 0.0028 x (2) 0.4560 0.4647 0.4744 0.4852 0.4970 0.5102 0.5248 0.5409 0.5587 0.5784 0.6000 0.6216 0.6451 0.6704 0.6974 0.7260 0.7556 0.7853 0.8137 0.8389 0.8598 x (3) 0.2163 0.2150 0.2136 0.2121 0.2107 0.2092 0.2076 0.2060 0.2042 0.2022 0.2000 0.1978 0.1952 0.1923 0.1889 0.1846 0.1792 0.1721 0.1630 0.1514 0.1374 y (1) 0.3933 0.3942 0.3950 0.3959 0.3966 0.3973 0.3978 0.3979 0.3975 0.3964 0.3940 0.3900 0.3835 0.3730 0.3566 0.3311 0.2920 0.2350 0.1591 0.0797 0.0260 y (2) 0.3770 0.3773 0.3776 0.3779 0.3782 0.3786 0.3790 0.3796 0.3804 0.3818 0.3840 0.3871 0.3920 0.3995 0.4114 0.4300 0.4588 0.5019 0.5617 0.6300 0.6866 y (3) 0.2297 0.2285 0.2274 0.2262 0.2252 0.2241 0.2232 0.2225 0.2221 0.2218 0.2220 0.2229 0.2245 0.2275 0.2320 0.2389 0.2492 0.2631 0.2792 0.2903 0.2874 T, o C 47.88 47.88 47.88 47.88 47.88 47.88 47.88 47.89 47.90 47.93 47.99 48.08 48.24 48.51 48.96 49.68 50.80 52.44 54.59 56.83 58.46 Analysis: (continued) Exercise 11.2 (continued) Exercise 11.3 Subject: : Calculation of a portion of a distillation curve for the system n-hexane - methanol methyl acetate. Given:. Ternary system n-hexane - methanol - methyl acetate at 1 atm. Assumptions: UNIFAC method for computing K-values. Find: Portion of a distilla...
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This document was uploaded on 02/24/2014 for the course CBE 2124 at NYU Poly.

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