Vapor-Liquid Equilibrium Coefficients Determined by Gas-Liquid Partition Chromatography: Systems Methane-Propane-n-Decane and Methane - Propane-n-Heptane.

Abstract

The results of the experimental solubility data are tabulated in Table II. In Figure 3 the methane K-values are presented. Figure 4 shows the extrapolation of the solubility data to the vapor pressure of re-decane. A temperature crossplot of the K-values for methane obtained from the solubility data in this work along with those obtained by Sage and Lacey (6) at higher temperatures is presented in Figure 5. The agreement of results from the experiments outlined herein with those of more complex static equilibrium studies is quite favorable. ADVANTAGE OF THE SOLUBILITY TECHNIQUEThe validity of the volumetric, static experiments described herein for determining the solubility of a highly volatile material in another which is quite nonvolatile is established by the consistency of the results with those of other investigators. The technique has the distinct advantage of furnishing vapor-liquid equilibria information from P-V-T measurements, with no need for sampling or analysis of either phase when the assumption that the vapor contains essentially none of the nonvolatile components is valid.

Phase equilibriums in hydrocarbon systems. Phase behavior in the methane-propane-n-decane system

“…Comparison of phase behavior from two sources equilibrium ratios for propane calculated from radioactive retention data yielded an average deviation of -0.0005, and from thermal conductivity retention data of 0.0015. In the case of methane, Koonce's data (9) at the lower values of composition parameter C, corresponding to higher mole fractions of n-decane, were consistently lower than the current measurements at 400 p.s.i.a. They (9) were somewhat higher than the current measurements at the higher values of the composition parameter.…”

“…(25), the methane-re-butanedecane system (13,16,17), the methane-ethane-re-pentane system (3), and the methane-propane-re-decane system at temperatures below 70°F. (9). Some studies of the quaternary system, methane-ethane-propane-re-butane, were made by Benedict et al (2), and limited investigations of other hydrocarbon systems have been reported.…”

Integrated solvent and process design using a SAFT-VR thermodynamic description: High-pressure separation of carbon dioxide and methane

“…Properties of the relevant single component and binary mixture uids have been intensively studied, both from experimental (Fredenslund & Mollerup, 1974;Hamam & Lu, 1974;Davalos, Anderson, Phelps & Kidnay, 1976;Brown, Kidnay & Sloan, 1988;Nagahama, Konishi, Hoshino & Hirata, 1974;Ohgaki & Katayama, 1977;Wei, Brown, Kidnay & Sloan, 1995;Somait & Kidnay, 1978;Kaminishi & Toriumi, 1968;Xu, Dong, Wang & Shi, 1992b;Bian, 1992;Xu, Dong, Wang & Shi, 1992a;Bian, Wang & Shi, 1993;Koonce & Kobayashi, 1964;Reamer, Olds, Sage & Lacey, 1942;Lavender, Sage & Lacey, 1940;Bett, Juren & Reynolds, 1968;Lin, Sebastian, Simnick & Chao, 1979;Reamer & Sage, 1963;Iwai, Hosotani, Morotomi, Koga & Arai, 1994;Inomata, Tuchiya, Arai & Saito, 1986;Jennings & Schucker, 1996;Chou, Forbert & Prausnitz, 1990;Nagarajan & Robinson, 1986;Sebastian, Simnick, Lin & Chao, 1980) and theoretical perspectives (McCabe, Galindo, GilVillegas & Jackson, 1998a;McCabe, Gil-Villegas & Jackson, 1998;Nguyen-Huynh, Tran, Tamouza, Passarello, Tobaly et al, 2008), but experimental data for ternary mixtures (Dunyushkin, Skripka & Nenartovich, 1977) are scarce for the systems of interest here. Thus, we rst present the SAFT-VR molecular models developed for this work; we obtain transferable binary interaction parameters where necessary and compare the result of the SAFT-VR calculations for the phase equilibria of pure components and binary mixtures to experimental data.…”

“…For CO 2 + C 10 and CH 4 + C 10 , we selected experimental data for pressures below 10 MPa and temperatures below 477 K. This corresponds to the operating range of the separation process that is being considered in our work. All of the experimental data available in the Detherm database (Fletcher, F., McMeeking & Parkin, 1996) are used for CH 4 + C 10 (111 points) (Koonce & Kobayashi, 1964;Reamer, Olds, Sage & Lacey, 1942;Lavender, Sage & Lacey, 1940;Bett, Juren & Reynolds, 1968;Lin, Sebastian, Simnick & Chao, 1979) and for CO 2 + C 10 (85 points) (Reamer & Sage, 1963;Iwai, Hosotani, Morotomi, Koga & Arai, 1994;Inomata, Tuchiya, Arai & Saito, 1986;Jennings & Schucker, 1996;Chou, Forbert & Prausnitz, 1990;Nagarajan & Robinson, 1986;Sebastian, Simnick, Lin & Chao, 1980), both over 15 temperature values (see table 2).…”

General friction theory viscosity model for the PC‐SAFT equation of state

“…The reason is that the k ij value of 0.056 reported in Gross and Sadowski23 was correlated against VLE data in the range 423 to 583 K, which is outside the temperature range of the considered viscosity data. The temperature dependency of the estimated K ij values obtained by fitting the PC‐SAFT EoS to experimental VLE data58–63 is shown in Figure 9, revealing a linear dependency as a function of the temperature, which can be expressed as with T given in K.…”