THE literature on liquidliquid extraction deals mainly with phase relationships, stage calculations, and discussion of the mechanism of mass transfer between two liquid phases.The published information on commercial extraction equipment, particularly the types used and performance data, is rather limited.Hunter and Nash {24) have written several papers containing brief notes on extraction equipment. Two reviews by Waeser {45,46) written in Germany during the war have become available in this country. Green {19) in England reported on solvent extraction with special reference to fine chemical manufacture.However, the best discussions to date have been those of Elgin in Perry's Handbook {38) and his several annual reviews {10,11) published since that time.This paper is an attempt to summarize all of the information available to date on commercial extraction equipment. The sources have been the general literature, patent literature, and data from manufacturers and operators of extraction equipment. The review of the patent literature is presented because it is a tedious process for an individual engineer and not very informative unless the reviewer goes back to the original patents. The INDUSTRIAL AND ENGINEERING CHEMISTRY Vol. 42, No. 6 Table I. Major Commercial Applications of Liquid-Liquid Extraction Processes I. Petroleum Refining A. Separating high purity products Toluene Butadiene Olefins B. Separating one or more groups of compounds from cuts of wide boiling range 1. Treatment of kerosene, Edeleanu (98) 2. Lubricating oils treated with selected solvents Edeleanu (liquid SO2) Chlorex [bis(2-chloroethyl)etherj Duo-Sol Furfural Nitrobenzene Phenol C. Dewaxing, deasphalting, and decarbonizing operations II. Extraction of Acetic Acid A. Wood distillation B-Recovery of acetic acid from dilute solutions from cellulose acetate, etc. III. Phenol Recovery A. Raschig process, primary phenol production B. Gas works liquids, recovery and by-product phenols C. Recovery of phenol from a wide variety of solutions IV. Chemical Processes with Liquid-Liquid Contacting A. Nitration /Here the value of countercurrent operations may be B. Sulfonation (questioned because of the danger of over-reaction V. Vitamins and Antibiotics VI. Vegetable Oil Refining VII. Fischer-Tropsoh Synthesis of Liquid FuelsA. Separation of water-soluble by-products B. Separation of oil-soluble oxygenated by-products 2. Solvent loss. (This varies considerably.) 3. Capital and labor charges of the distillation equipment.4. Capital, labor, and power for extraction equipment.
The critical constants of propane (C3H8) are: tc = 96.81±0.01°C, pc = 42.01±0.02 normal atmospheres, vc = 0.195 liter per mole (4.43 cc per gram), dc = 5.13 moles per liter (0.226 gram per cc). The uncertainty in the critical volume and density is 1 percent.
The volumetric behavior of gaseous isobutane from 150° to 300°C and from 1.0 to 8.0 moles per liter has been studied. The constants of the Beattie-Bridgeman equation of state for gaseous isobutane are R=0.08206, A0=16.6037, a=0.11171, B0=0.23540, b=0.07697, c=300×104 in units of normal atmospheres, liters per mole, degrees Kelvin.
The compressibility of gaseous ethane (C2H6) has been determined from 0.5 to 5.0 moles per liter and from 25° to 250°C with an estimated accuracy of 0.2 percent or better. Above 250°C ethane decomposes at an appreciable rate when confined in steel. An equation of state is fitted to the data. The average deviation of the calculated from the observed pressure is 0.13 atmosphere or 0.21 percent. The equation of state extrapolates to the critical pressure (at 7 moles/liter and 32.1°C) with an error of 10 percent and calculates the weight of a normal liter to 0.2 percent. The vapor pressures of liquid ethane at 0° and 25°C are given.
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