Applied process design for chemical and petrochemical plants by Ernest E. Ludwig (Eds.)

By Ernest E. Ludwig (Eds.)

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Continue until feed plate composition is reached, then switch to equation of stripping section and continue as before until desired bottoms composition is reached. 01455 Use this equation as described above following down from the feed plate cross-overfrom the rectifylng equation to the stripping equation. B. Fmq= 0 This represents feed as all vapor (not superheated). Slope of “q” line: -q =-=-- 1-q -0 - 0 1-0 This represents no change in overflow from the feed plate, and the increase in vapor flow is equal to the mols of feed.

063 ~ ~~ *Used by permission of McFarland et al. [86]. 2%, which is about as accurate, or perhaps more so, than other efficiency equations. 6%. See Example 8-13 for identification of dimensionless groups. Vapor densities are calculated from the ideal gas relation: pv = MPt/555(T + 460) where total pressure P, is given in millimeters of mercury. Distillation Mixture densities of the binary mixtures require a knowledge of volume fraction for each component. 609 lb/hr-ft Liquid surface tension is calculated using the Sugden Parachor method [242].

A. Calculate the minimum reflux ratio if the feed is liquid at its boiling point. 5 times the minimum is employed. *Used by permidon, SfcCmmick,J. ~ 95 g , no. 13 (1988). all rights Ipserved. 90 = 50 mols overhead product D = overhead product, mols B = bottoms, mols The following is a short approximation method for minimum reflux ratios for multicomponent mixtures [98]: - Step-wise Troys for Operating (8 63) where(xFLK)eff = x m / ( x m + xFHK) n = number of components h i n = minimum reflux ratio x = liquid mol fraction q = relative volatility of component i based on heavy key a L K = relative volatility of component, i,based on light key.

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