6 747 1803 4092 819 4383 899 1828 1853 4691 985 1857

Info iconThis preview shows page 1. Sign up to view the full content.

View Full Document Right Arrow Icon
This is the end of the preview. Sign up to access the rest of the document.

Unformatted text preview: 474.2 99.9 KA 1.000 1.043 1.092 1.191 1.297 1.411 1.534 1.665 1.805 2.115 2.286 2.468 2.661 2.867 3.085 3.317 3.563 3.824 4.100 4.392 4.701 4.751 KB 0.131 0.138 0.147 0.164 0.183 0.203 0.226 0.251 0.279 0.343 0.379 0.419 0.463 0.510 0.562 0.619 0.681 0.748 0.821 0.901 0.987 1.001 xA 1.000 0.953 0.903 0.814 0.733 0.659 0.592 0.530 0.472 0.371 0.326 0.284 0.244 0.208 0.173 0.141 0.111 0.082 0.055 0.028 0.004 0.000 yA 1.000 0.993 0.986 0.970 0.951 0.931 0.908 0.882 0.853 0.784 0.744 0.700 0.650 0.596 0.535 0.468 0.395 0.313 0.224 0.125 0.017 0.000 Analysis: (continued) Exercise 7.21 (continued) Exercise 7.21 (continued) Analysis: (continued) Now determine the tray requirements for actual operation. Using Eq. (7-7), with the operating reflux ratio of 0.464, L/V = R/(1 + R) = 0.464/(1 + 0.464) = 0.317. Because such high purity distillate and bottoms products are to obtained, use 3 McCabe-Thiele diagrams. The first diagram is for the high purity region of component A from y and x = 0.9 to 1.0. The operating line for the rectifying section begins at {0.99...
View Full Document

This note was uploaded on 09/08/2008 for the course CHE 244 taught by Professor Selebi during the Spring '06 term at Lehigh University .

Ask a homework question - tutors are online