Treybal

R. E. Treybal, Mass Transfer Operations, 3rd ed. McGraw Hill, New York, 1980. 

Taylor and Krishna, Multicomponent Mass Transfer, Wiley, 1993. Toumie, Laguerie, and Couderc, Chem. Engr. Sd., 34, 1247 (1979). Treybal, Mass Transfer Operations, 3d ed., McGraw-Hill, 1980. 

Heating, Refrigerating and Air-Conditioning Engineers, New York, 1967. Quinn, Humidity The Neglected Parameter, Test Eng. (July 1968). Treybal, Mass-Ttansfet- Operations, 3d ed. McGraw-Hill, New York, 1980. Wexler, Humidity and Moisture, vol. I, Reinhold, New York, 1965. Zimmerman and Lavine, Psychrometric Charts and Tables, Industrial Research Service, 2d ed., Dover, N.H., 1964. 

In concentrated wstems the change in gas aud liquid flow rates within the tower and the heat effects accompanying the absorption of all the components must be considered. A trial-aud-error calculation from one theoretical stage to the next usually is required if accurate results are to be obtained, aud in such cases calculation procedures similar to those described in Sec. 13 normally are employed. A computer procedure for multicomponent adiabatic absorber design has been described by Feiutnch aud Treybal [Jnd. Eng. Chem. Process Des. Dev., 17, 505 (1978)]. Also see Holland, Fundamentals and Modeling of Separation Processes, Prentice Hall, Englewood Cliffs, N.J., 1975. 

When the equihbrium line is not straight, Treybal Liquid Extraction, 2d ed., McGraw-Hill, New York, 1963) recommends that the geometric mean value of m be used. The geometric mean of the slope of the equilibrium hue at the concentration leaving the feed state and at the raffinate concentration leaving the raffinate stage is... 

See also Treybal [Am. ln.st. Chem. Eng. J., 4, 202 (1958) 6, 5M (I960)] and Olander [Chem. Eng. Sci, 18, 47 (1963) 19, 275 (1964)]. The remaining discussion is confined to measured values of stage efficiency or volumetric overall coefficients. These are largely of value only for the particiilar systems studied. For this reason, one fairly complete study will be described, and the others will only be mentioned. 

Flynn and Treybal [Am. Inst. Chem. Eng. J., I,. 324 (1955)]. Continuous extraction of benzoic acid from toluene and kerosine into water baffled vessels, turbine agitators. Stage efficiency is correlated with agitator energy per unit of liquid treated. 

The power for agitation of two-phase mixtures in vessels such as these is given by the cuiwes in Fig. 15-23. At low levels of power input, the dispersed phase holdup in the vessel ((j)/ ) can be less than the value in the feed (( )df) it will approach the value in the feed as the agitation is increased. Treybal Mass Transfer Operations, 3d ed., McGraw-HiU, New York, 1980) gives the following correlations for estimation of the dispersed phase holdup based on power and physical properties for disc flat-blade turbines ... 

Mass Transfer Extraction rates for packed towers are usually excellently correlated for a given situation on the coordinate system of Fig. 15-35. Treybal [Chem. Eng. Prog., 62(9), 67 (1966)] nas suggested means whereby overall Hto s may be resolved into constituent... 

For the same liquids axial mixing is described by (Bibaud and Treybal, loc. cit.)... 

See also Miyauchi et al. (loc. cit.), who express the axial mixing in terms of interstage flow. For the continuous phase with no dispersed-phase flow, see Bibaud and Treybal, and Cutoff (loc. cit.). 

Treybal Tower Treybal [U.S. Patent 3,325,255, 1967) Chem. Eng. Prog., 60(5), 77 (1964)] adapted a mixer-settler cascade in tower form in which the liquids are setued between stages. 

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