Showing papers in "Journal of Chemical & Engineering Data in 1981"

Density and surface tension of 83 organic liquids

Abstract: 1920 where subscript 2 stands for the solute and 1 for the solvent: x2 is the mole fraction of the solute in the solvent; f2 is the fugacity of the solute in the gas phase. Henry’s constants for hydrogen in the three aromatic compounds were evaluated by extrapolating a plot of fH,lxHl to xH = 0. The fugacity of hydrogen in the gas phase, fw was calculated from the Soave-Redlich-Kwong equation of state (4). Figure 2 shows the plot of Henry’s constants vs. temperature. The values of

Vapor-liquid phase equilibrium for carbon dioxide-n-hexane at 40, 80, and 120 .degree.C

Abstract: Vapor and liquid equilibrium phase compositions have been measured for carbon dioxide-n-hexane at temperatures of 40, 80, and 120/sup 0/C. At each temperature, the pressure range from approximately 6.8 atm (100 psia) to near the system critical pressure was covered. Equilibrium K values for carbon dioxide and n-hexane were calculated from these data. The data from this work are well represented by the Soave Equation of State. When one uses an optimum interaction parameter, C12 = 0.131, in the Soave equation, average errors in the predicted phase compositions (at fixed T and P) are 0.012 and 0.009 for the liquid and vapor phases, respectively.

Three-phase liquid-liquid-vapor equilibriums behavior of certain binary carbon dioxide-n-paraffin systems

Abstract: The 3-phase liquid-liquid-vapor loci of 4 binary CO/sub 2/-n-paraffin systems (n-dodecane, n-tridecane, n-tetradecane, n-pentadecane) are studied, and temperature, pressure, and molar volumes and composition of both liquid phases are reported. It is within this group of n-paraffins that the nature of the upper critical end point for the CO/sub 2/-containing binary systems changes with increasing carbon number from an upper critical solution (temperature) point where L/sub 1/ and L/sub 2/ phases become critical in presence of vapor phase to a K point, where L/sub 2/ and vapor phases become critical in the presence of L/sub 1/ phase. These 4 loci are compared with earlier obtained loci on CO/sub 2/-n-decane and CO/sub 2/-n-elcosane.

Three-phase solid-liquid-vapor equilibriums in the binary hydrocarbon systems methane-n-hexane and methane-benzene

Abstract: Pressure, temperature, liquid-phase compositions, and liquid-phase molar volumes are presented along the solid-liquid-vapor (SLV) loci of the binary systems methane-n-hexane and methane-benzene. The data were taken by using cryoscopic techniques and are compared to the solid-liquid (SL) data at elevated pressures of Kuebler and McKinley. The standard deviations of the smoothed SLV data for liquid-phase solute composition presented herein from the raw SLV data are 3.7% for the methane-n-hexane system and 8.6% for the low-temperature branch of the methane-benzene system. The corresponding standard deviation for the high-temperature (high solute composition) branch for the system methane-benzene is less than 0.7%. 8 refs.

Adsorption of a gaseous mixture of ethane and propane on a carbon molecular sieve

Abstract: Using temperatures of 40/sup 0/, 86/sup 0/, and 120/sup 0/F at 100-mm Hg pressure and 86/sup 0/F at 300-mm Hg, researchers measured the adsorption of a binary gaseous mixture of ethane and propane on the carbon molecular sieve MSC-5A. The system's preference for propane - which was higher than predicted by the Myers-Prausnitz method - was greater at lower temperatures but did not change with pressure. Activity coefficients of the adsorbed phase calculated by the Myers-Prausnitz method show that at very high concentrations of propane, the ethane dissolves in the adsorbed propane in the micropores rather than being adsorbed on the surface of the adsorbent.