Vapor−Liquid Equilibrium, Coexistence Curve, and Critical Locus for Pentafluoroethane + 1,1,1-Trifluoroethane (R125/R143a)

Higashi, Yukihiro

doi:10.1021/je980266+

Cited by 21 publications

(4 citation statements)

References 7 publications

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“…Experimental data[29]: VLE prediction for R-125 (1) + R-143a (2). Experimental data[30]: VLE prediction for R-143a (1) + R-1234yf (2). Experimental data[33]: VLE prediction for CO 2 (1) + R-32 (2).…”

mentioning

confidence: 99%

Prediction of thermodynamic properties of refrigerant fluids with a new three-parameter cubic equation of state

Coquelet

Abbadi

Houriez

2016

International Journal of Refrigeration

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To describe the thermodynamic properties of refrigerant fluids, it is important to use a reliable thermodynamic model able to predict accurate results for both pure compounds and mixtures. In this study, a new three-parameter cubic equation of state is presented, based on the modification of the well-known Patel-Teja equation of state. The new equation of state is associated with the Mathias-Copeman alpha function. By only knowing the acentric factor ω and the experimental critical compressibility factor Z c of pure compounds, it is possible to predict thermodynamic properties for both pure compounds and mixtures by means of the new equation of state. No binary interaction parameter k ij is needed for the prediction of mixture properties. The results obtained with the new equation of state show a good agreement with experimental data for vapor-liquid equilibrium and density properties. The obtained results are particularly satisfying for liquid density, and in the vicinity of the critical point, by comparison with the results obtained using the Peng-Robinson and the Patel-Teja equations of state.

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confidence: 99%

Prediction of thermodynamic properties of refrigerant fluids with a new three-parameter cubic equation of state

Coquelet

Abbadi

Houriez

2016

International Journal of Refrigeration

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“…Other authors measured the critical point of the mixture (50 wt % R143a + 50 wt % R125) by observation of the vanishing meniscus between the liquid and vapor phases. 26,28 Fro ¨ba et al 26 reported a critical temperature for R507 (50 wt % R143a + 50 wt % R125), the refrigerant mixture commercially available from Solvay, of 344.06 K. Kishizawa et al 28 and Higashi 27 determined slightly lower critical temperatures for the same mixture of (343.783 and 343.76) K, respectively. These data deviate less than 0.1 % in temperature from the gas-liquid critical values obtained by our acoustic method.…”

Section: Speed Of Sound Of Liquid (51 Wt % R143a + 49 Wt % R125)mentioning

confidence: 99%

“…Higashi 27 measured the critical parameters of the R143a + R125 mixture for different compositions. To represent the composition dependence of the critical parameters of the system, the author formulated a correlation of the critical locus, having his correlation given at 343.82 K for the critical locus of (51 wt % R143a + 49 wt % R125).…”

Section: Speed Of Sound Of Liquid (51 Wt % R143a + 49 Wt % R125)mentioning

confidence: 99%

Acoustic Determination of Thermophysical Properties and Critical Parameters for the Mixture (51 wt % R143a + 49 wt % R125) and Critical Line of xCO₂ + (1 − x)(51 wt % R143a + 49 wt % R125)

et al. 2006

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The thermophysical properties and critical parameters for the alternative refrigerant (51 wt % of 1,1,1-trifluoroethane (R143a) + 49 wt % of pentafluoroethane (R125))svery close to the composition of R507 (50 wt % of each mixture component)swere investigated using two different acoustic techniques. The critical behavior of the system xCO 2 + (1x)(51 wt % R143a + 49 wt % R125) was also investigated. Experimental data of speed of sound in liquid (51 wt % R143a + 49 wt % R125) from T ) (253 to 338) K and pressures up to 65 MPa were measured using a pulse-echo method. Derived thermodynamic properties were calculated, combining our experimental data with density and isobaric heat capacity values published by other authors. Measurements of the critical temperature T c and pressure p c on (51 wt % R143a + 49 wt % R125) and mixtures of xCO 2 + (1x)(51 wt % R143a + 49 wt % R125) were performed using another simple ultrasonic time-delay technique. The binary critical line was determined over the whole composition range showing that this system deviates only slightly from ideality since the critical line is a continuous line. The Peng-Robinson equation of state with conventional mixing and combining parameters was used to correlate the binary experimental data.

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“…A summary for the binary VLE regression results ( k ij (1) and k ij (2) ) is shown in Table , − where column “ x i ” represents the overall AAD in composition of both x i and y i . The AAD for each variable ( T , P , x i , y i ) for all binary systems can be found in the SI (see Table S6).…”

Section: Regressionmentioning

confidence: 99%

Multicomponent Refrigerant Separation Using Extractive Distillation with Ionic Liquids

Finberg

May

Shiflett

2022

Ind. Eng. Chem. Res.

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Hydrofluorocarbon refrigerants are being phased out over the next two decades due to concerns about high global warming potential. In order to separate refrigerant mixtures that form azeotropes, new technologies will be required. Currently, fractional distillation is unable to efficiently separate azeotropic refrigerant mixtures. Extractive distillation using an ionic liquid as the entrainer offers a solution. Vapor–liquid equilibria data for refrigerants difluoromethane (HFC-32), pentafluoroethane (HFC-125), 1,1,1,2-tetrafluoroethane (HFC-134a), 1,1,1-trifluoroethane (HFC-143a), chlorodifluoromethane (HCFC-22), propane (HC-290), and isobutane (HC-600a) and ionic liquid 1-butyl-3-methylimidazolium hexafluorophosphate ([C4C1im][PF6]) was regressed using the Peng–Robinson equation of state with the van der Waals 1-parameter mixing rule and Boston–Mathias nonideal correction. Process flow diagrams using ASPEN simulations were prepared for demonstrating how multicomponent mixtures of these refrigerants can be separated. Opportunities for measuring and modeling the solubility of new refrigerants in ionic liquids are discussed, and challenges remain for effectively separating some azeotropic refrigerant mixtures containing hydrofluorocarbons and hydrocarbons.

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Vapor−Liquid Equilibrium, Coexistence Curve, and Critical Locus for Pentafluoroethane + 1,1,1-Trifluoroethane (R125/R143a)

Cited by 21 publications

References 7 publications

Prediction of thermodynamic properties of refrigerant fluids with a new three-parameter cubic equation of state

Prediction of thermodynamic properties of refrigerant fluids with a new three-parameter cubic equation of state

Acoustic Determination of Thermophysical Properties and Critical Parameters for the Mixture (51 wt % R143a + 49 wt % R125) and Critical Line of xCO₂ + (1 − x)(51 wt % R143a + 49 wt % R125)

Multicomponent Refrigerant Separation Using Extractive Distillation with Ionic Liquids

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Vapor−Liquid Equilibrium, Coexistence Curve, and Critical Locus for Pentafluoroethane + 1,1,1-Trifluoroethane (R125/R143a)

Cited by 21 publications

References 7 publications

Prediction of thermodynamic properties of refrigerant fluids with a new three-parameter cubic equation of state

Prediction of thermodynamic properties of refrigerant fluids with a new three-parameter cubic equation of state

Acoustic Determination of Thermophysical Properties and Critical Parameters for the Mixture (51 wt % R143a + 49 wt % R125) and Critical Line of xCO2 + (1 − x)(51 wt % R143a + 49 wt % R125)

Multicomponent Refrigerant Separation Using Extractive Distillation with Ionic Liquids

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Product

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Acoustic Determination of Thermophysical Properties and Critical Parameters for the Mixture (51 wt % R143a + 49 wt % R125) and Critical Line of xCO₂ + (1 − x)(51 wt % R143a + 49 wt % R125)