By Ernest E. Ludwig (Eds.)
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475, Note: This is not too accurate due to switched operating line equations before the feed compositionswere reached, yet, one more calculation on the stripping line would have placed us below the feed plate composition. Hence a change in reflux ratio is necessary in order to split right at the feed composition. 5 Referring to calculations of Example 8-10, for an equimolal mixture of benzene and toluene in feed: Total theoretical trays: rectifylng section = 4 feed tray =1 stripping section = 7 total = 12 Trays overhead product, D = 50 mols/100 mols feed ($) =-, YC XD calculate min Example: 8 1 1 Thermal Condition of Feed Using the same operating reflux (same fraction times the minimum) as was used in Example 8-10, calculate the theoretical plates required for feed of the following thermal conditions: Use Figure 8-27.
8. 3 stages or 16%. For ideal systems following Raoult’s Law;relative volatility alh = pI/ph, ratio of partial pressures. For a binary distillation, a is calculated at top and bottom conditions and a geometric mean used where the differences are relatively small. .... 37;No. 5 (1958), p. 216, Gulf Pub. Co. 9 By assuming values of xl, the corresponding y1 may be calculated. 4 9 Using the vapor pressure data for benzene and toluene : 1. Construct a boiling point diagram at a total pressure of 760 mm Hg, Figure 8-18.
Thermal Condition of Feed The condition of the feed as it enters the column has an effect on the number of trays, reflux requirements and heat duties for a given separation. , sub-cooled liquid feed, feed at the boiling point of the column feed tray, part vapor and part liquid, all vapor but not superheated, and superheated vapor. 0 2. 0 P a r t i a l Condensation of Overhead Vapors Minimum Reflux Abnormal Equilibrium Figure 8-15. Operating characteristics of distillation columns. is approximately the amount of heat required to vaporize one mol of feed at the feed tray conditions, divided by the latent heat of vaporization of the feed.