“…Densities and vapor pressures of pure R 13 have been measured by several workers (2-6), and several reports exist for the measurement of the densities and vapor-liquid equilibrium properties for R 13 in mixed refrigerant systems, generally with R 12, R 14, and R 23 (7)(8)(9)(10)(11)(12). As far as we are aware, however, the present measurements are the first that have been reported on mixtures of R 13 with hydrocarbons at elevated temperatures and pressures.…”
Vapor and liquid equilibrium phase compositions were determined at 310.93, 350.00, and 400.00 K for the binary systems of chlorotrifluoromethane (R 13) with -butane and with Isobutane. The data were fit with the Peng-Robinson equation of state. Henry's constants were derived, and their temperature behavior Is compared with a new model calculation.
“…Densities and vapor pressures of pure R 13 have been measured by several workers (2-6), and several reports exist for the measurement of the densities and vapor-liquid equilibrium properties for R 13 in mixed refrigerant systems, generally with R 12, R 14, and R 23 (7)(8)(9)(10)(11)(12). As far as we are aware, however, the present measurements are the first that have been reported on mixtures of R 13 with hydrocarbons at elevated temperatures and pressures.…”
Vapor and liquid equilibrium phase compositions were determined at 310.93, 350.00, and 400.00 K for the binary systems of chlorotrifluoromethane (R 13) with -butane and with Isobutane. The data were fit with the Peng-Robinson equation of state. Henry's constants were derived, and their temperature behavior Is compared with a new model calculation.
“… 2 Mixture phase behavior of R23/R13. The empty circles are the experimental data, the dashed line is for k ij = 1.0, and the solid line is the correlation using SAFT-VR with k ij = 0.930. The filled circle denotes the experimental azeotrope.…”
Section: Resultsmentioning
confidence: 99%
“…Figure 2 shows the VLE for the R23/R13 system at 273.09, 255.32, 224.79, and 199.05 K for which experimental data 15 are available in the literature. The dashed line shown only for 273.09 K provides the predictions using k ij ) 1, and it shows that there is no azeotrope predicted.…”
An ever increasing concern on the stratospheric ozone depletion has led to a worldwide ban on fully halogenated chlorofluorocarbons (CFCs) and prompted a rigorous search for alternative refrigerants with a zero ozone-depletion potential (ODP) and a low global warming potential (GWP). Accurate thermodynamic information is required to develop an optimum alternative to replace an existing CFC pure fluid or mixture. In this work, statistical associating fluid theory with variable range (SAFT-VR) is used to correlate the vapor liquid equilibria (VLE) and the vapor-liquid-liquid equilibria (VLLE) for various refrigerant mixtures. An analysis on the pure component parameters for pentane was performed due to the existence of multiple parameter sets using SAFT-VR. The effects of the pure component parameters in mixture phase predictions were investigated. An optimized binary interaction parameter (k ij ) value was used to correlate the experimental data. It was found that the mixture phase predictions were sensitive to the adjusted k ij value in such a way that fundamental changes in the phase diagram can occur with a small change in the k ij value. Hence, an attempt was made to model new refrigerant mixture blends by transferring the k ij value to similar mixtures. The good agreement of the predictions made using the transferred k ij value and the experimental data aids in suggesting new alternative refrigerant blends.
“…The apparatus used was of the vapor-recirculation type; its description, construction, and mode of operation have been reported elsewhere. 1,2 The temperature was measured to within ±0.01 K with a three-junction copper-constantan thermopile, the emf of which was determined by using a Leeds and Northrup type K-3 potentiometer. Calibration of the thermopile, which was referenced to melting ice, was effected against a platinum resistance thermometer, which, in turn, had been calibrated and certified by the U.S. National Bureau of Standards.…”
Section: Methodsmentioning
confidence: 99%
“…The usual equation for vapor-liquid equilibrium was applied /iP = 7 /;•01 (1) The vapor-phase fugacity coefficient , was calculated from the experimental temperature, pressure, and vapor composition through the use of a modified Redlich-Kwong equation of state.4 (2) where…”
Section: Correlation Of Experimental Datamentioning
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