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TERNARY LIQUID-LIQUID EQUILIBRIA for the SYSTEMS of AQUEOUS METHANOL SOLUTIONS and PROPANE OR N-BUTANE

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TERNARY LIQUID-LIQUID EQUILIBRIA for the SYSTEMS of AQUEOUS METHANOL SOLUTIONS and PROPANE OR N-BUTANE w = mass of solid per unit area measured from 3) Carslaw, H. S. and J. C. Jaeger: "Conduction of Heat in medium [g/cm2] Solids", 2nd ed , p. 285, Oxford Univ. Press (1959). Wi, w* = value of w at cake surface and total mass 4) Crank, J. : "The Mathematics of Diffusion", Oxford Univ. of solid per unit area [g/cm2] Press (1956). x = distance from medium [cm] 5) Fujita, H.: /. Chem. Phys., 21, 700 (1953). x% = thickness of cake [cm] 6) Hamill, T. D. and S. G. Bankoff: Ind. Eng. Chem. Funda- mentals, 3, 177 (1964). a = defined by Eq. (30) [-] 7) Lee,E. S. andL. T. Fan: Can. J. Chem. Eng.,46, 200(1968). /3 = 0\b\ [-] 8) Okamura, S. and M. Shirato: Kagaku Kogaku, 19, 104, 111 s = porosity [-] (1955). r] - defined by Eq. (14) [-] 9) Satoh, T. and K. Atsumi: J. Chem. Eng. Japan, 3, 92 (1970). 0 = non-dimensional time, defined by Eq. (14) [-] 10) Shirato, M. and T. Aragaki: Advanced Chemical Engineer- x = b/VT [-] ing (Japan), 8, 121 (1974). li = viscosity of filtrate [g/cm-sec] ll) Shirato, M. and T. Murase: ibid, 8, 153 (1974). P, ps = density of filtrate and of solid [g/cm3] 12) Shirato, M., M. Sambuichi, T. Aragaki and H. Kato: Kagaku Kogaku, 31, 359 (1967). 13) idem: AlChEJ., 15, 405 (1969). Literature Cited 14) Shirato, M. and M. Sambuichi: Kagaku Kogaku, 27, 470 1) Atsumi, K., T. Akiyama and M. Miyagawa: /. Chem. Eng. (1963). Japan, 6, 236 (1973). 15) Smiles, D. E.: Chem. Eng. ScL, 25, 985 (1970). 2) Bankoff, S. G.: Adv. Chem. Eng., 5, 15 (1964). 16) Tiller, F. M. and H. R. Cooper: AIChEJ., 6, 595 (1960). Short Communications TERNARY LIQUID-LIQUID EQUILIBRIA FOR THE SYSTEMS OF AQUEOUS METHANOL SOLUTIONS AND PROPANE OR n-BUTANE Katsuji NODA*, Kuraji SATO1, Koichi NAGATSUKA2 AND KlYOHARU ISHIDA Department of Chemical Engineering, Shizuoka University, Hamamatsu, 432 data for the methanol-n-butane system and the Introduction liquid-liquid equilibrium data for the ternary meth- Liquid-liquid equilibrium data are essential for anol-water-propane and methanol-water-n-butane the selection of solvent and for the design of separa- systems at 0°C and 20°C. liquid-liquidtion processes.equilibriaManyinvestigatorsincluding ternaryhave reportedaqueouson 1. Experimental methanol solutions and /z-paraffin systems. Stephen Mutual solubilities for the methanol-/z-butane and Stephen7) have compiled comprehensive tables system were determined by the cloud point method. of liquid-liquid equilibrium data. Mutual solubili- Ternary liquid-liquid equilibrium data for the meth- ties for methanol-ft-paraffin systems including n- anol-water-propane and methanol-water-^-butane pentane to w-decane have been reported by Kiser3). systems were determined by the samemethodreported As the mutual solubilities for systems of //-paraffin and in the previous paper1} except for the determination water are small and measurementsof the solubilities of compositions by using gas chromatographic analy- for these systems are very difficult, only a few data sis. A column of3 mmdiameter and 3 meter length is have been reported. Kobayashi4) and Mannheimer5) filled with Porapak R as a packing material for gas have reported the mutual solubilities for the propane- chromatograph and hydrogen is used as a carrier gas. water system and Reamer6} for the //-butane-water The sample was injected several times into a gas system. This paper presents the mutual solubility chromatograph and was analyzed by the total amounts Received December 2, 1974. of the sample. The composition of each component 1 Niigata Tekkosho Co., Ltd. was determined by the total areas of the gas chro- 2 Dainichiseika Co., Ltd. matogram. As the amount of water in the hydro- 492 JOURNAL OF CHEMICAL ENGINEERING OF JAPAN Table 1 Solubility data for the methanol-w-butane system, METHANOL weight fraction M e t h a n o l C l o u d p o i n t M e th a n o l C l o u d p o i n t [- C ] [- C ] 0 . 5 5 4 - 1 9 . 2 0 . 2 1 5 - 7 . S 0 . 5 1 6 - 1 5 . 0 0 . 1 6 7 - 9 . 1 0 . 4 4 7 - 1 0 . 8 0 . 1 4 9 - 9 . 5 0 . 3 4 2 - 8 . 1 0 . 0 8 4 - 1 8 . 6 0 . 3 3 1 - 7 . 9 0 . 0 7 4 - 2 3 . 4 Table 2 Equilibrium data for the methanol-water-propane T esystem,m p . weightH y d rfractiono ca r b o n la y er W a te r la y e r [ - C ] P r o p a n e W a t e r M e t h a n o l P r o p a n e W a t e r M e t h a n o l WATER PROPANE 0 0 . 9 9 7 0 . 0 0 0 2 0 . 0 0 3 0 . 0 0 9 0 . 4 5 4 0 . 5 3 7 Fig. 1 Liquid-liquid equilibria for the methanol-water- 0 . 9 9 5 0 . 0 0 0 3 0 . 0 0 5 0 . 0 1 7 0 . 3 4 0 0 . 6 4 3 0 . 9 8 5 0 . 0 0 0 8 0 . 0 14 0 . 0 3 6 0 . 1 9 2 0 . 7 7 2 propane system at 0°C (O) and 20°C ((à")), weight fraction 0 . 9 7 1 0 . 0 0 1 0 . 0 2 8 0 . 0 5 4 0 . 1 2 8 0 . 8 1 8 0 . 8 8 6 0 . 0 0 2 0 . 1 1 2 0 . 1 3 4 0 . 0 2 8 0 . 8 3 8 METHANOL 2 0 0 . 9 94 0 . 0 0 0 6 0 . 0 0 5 0 . 0 0 7 0 . 5 9 1 0 . 4 0 2 0 . 9 8 8 0 . 0 0 0 8 0 . 0 1 1 0 . 0 1 8 0 . 3 8 8 0 . 5 9 4 0 . 9 8 5 0 . 0 0 1 0 . 0 14 0 . 0 2 5 0 . 3 5 1 0 . 6 2 4 0 . 9 7 2 0 . 0 0 15 0 . 0 2 6 0 . 0 6 4 0 . 2 0 6 0 . 7 3 0 0 . 9 4 9 0 . 0 0 2 0 . 0 4 9 0 . 1 6 3 0 . 0 9 7 0 . 7 4 0 Table 3 Equilibrium data for the methanol-water-«-butane system,T e m p . weightH y d r ofractionc a r b o n l a y e r W a t e r l a y e r [ - C ] ^ - B u t a n e W a t e r M e t h a n o l # - B u t a n e W a t e r M e t h a n o l 0 0 . 9 9 4 0 . 0 0 0 3 0 . 0 0 6 0 . 0 1 5 0 . 2 7 8 0 . 7 0 7 0 . 9 8 9 0 . 0 0 0 4 0 . 0 1 1 0 . 0 3 9 0 . 1 5 6 0 . 8 0 5 WATER n-BUTANE 0 . 9 7 8 0 . 0 0 0 6 0 . 0 2 1 0 . 0 8 2 0 . 0 8 4 0. 8 3 4 0 . 9 6 3 0 . 0 0 0 7 0 . 0 3 6 0 . 1 3 0 0 . 0 4 6 0 . 8 2 4 Fig. 2 Liquid-liquid equilibria for the methanol-water-/*- 0 . 9 4 1 0 . 0 0 0 8 0 . 0 5 8 0 . 2 0 6 0 . 0 2 2 0 . 7 7 2 butane system at 0°C (O) and 20°C ((à")), weight fraction 0 . 9 3 8 0 . 0 0 0 8 0 . 0 6 1 0 . 2 18 0 . 0 18 0 . 7 6 4 2 0 0 . 9 9 6 0 . 0 0 0 4 0 . 0 0 4 0 . 0 0 3 0 . 6 0 1 0 . 3 9 6 0 . 9 9 1 0 .0 0 0 6 0 . 0 0 8 0 . 0 1 1 0 . 3 4 5 0 . 6 4 4 anol-water-propane and methanol-water-^-butane 0 . 9 8 8 0 . 0 0 0 7 0 . 0 1 1 0 . 0 2 2 0 . 2 4 1 0 . 7 3 7 systems at 0°C and 20°C are given in Tables 2 and 3 0 . 9 8 6 0 . 0 0 0 8 0 . 0 13 0 . 0 2 7 0. 2 2 0 0 . 7 5 3 and are shown in Figs. 1 and 2. Tieline data for 0 . 9 7 6 0 .0 0 1 0. 0 2 3 0 . 0 4 6 0 . 1 5 7 0 . 7 9 7 0 . 9 6 5 0 . 0 0 1 0 . 0 34 0 . 10 5 0 . 1 0 8 0 . 7 8 7 these systems are fairly well correlated by Ishida2) 0 . 9 5 1 0 . 0 0 1 5 0 . 0 4 7 0 . 16 3 0 . 0 69 0. 7 6 8 coordinates. 0. 9 2 7 0 . 0 0 2 0 . 0 7 1 0 . 2 8 9 0 . 0 3 6 0. 6 7 5 Conclusion carbon-rich phase is very small, care was taken in Mutual solubility data for the w-butane-methanol analyzing the sample to avoid contamination by the system and ternary liquid-liquid equilibrium data for surroundings, especially water vapor. the methanol-water-propane and methanol-water- Standard reagent propane and ^-butane purchased rc-butane systems at 0°C and 20°C have been presented.
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