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Kim, C.-N.; Park, Y.-M.

doi:10.1023/a:1022605104490

Cited by 15 publications

(2 citation statements)

References 6 publications

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“…All of the datasets appear to be of similar quality. Average differences are 0.38%, 0.41%, 0.50%, and 0.57% for the datasets of Takagi et al (1999), Piao et al (1996), Kim and Park (1999), and Chung and Kim (1997), respectively. For those datasets which reported both liquid and vapor composition, differences in the dew point composition are generally around 0.006 mole fraction.…”

Section: The R-32/125 Systemmentioning

confidence: 89%

Appendix B, Equations of States for Mixtures of R-32, R-125, R-134a, R-143a, and R-152a

Lemmon¹,

Jaconsen²

2002

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Mixture models explicit in Helmholtz energy have been developed to calculate the thermodynamic properties of refrigerant mixtures containing R-32, R-125, R-134a, R143a, and R-152a. The Helmholtz energy of the mixture is the sum of the ideal gas contribution, the compressibility (or real gas) contribution, and the contribution from mixing. The independent variables are the density, temperature, and composition. The model may be used to calculate thermodynamic properties of mixtures, including dew and bubble point properties and critical points, within the experimental uncertainties of the available measured properties. It incorporates the most accurate equations of state available for each pure fluid. The estimated uncertainties of calculated properties are 0.1% in density and 0.5% in heat capacities and the speed of sound. Calculated bubble point pressures are generally accurate to within 0.5%.

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Section: The R-32/125 Systemmentioning

confidence: 89%

Appendix B, Equations of States for Mixtures of R-32, R-125, R-134a, R-143a, and R-152a

Lemmon¹,

Jaconsen²

2002

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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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Study on the Interaction Coefficients in PR Equation with vdW Mixing Rules for HFC and HC Binary Mixtures

Chen

2008

Int J Thermophys

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The Peng-Robinson equation of state with the van der Waals mixing rules was used to correlate vapor-liquid equilibrium (VLE) data for HFC/HC, HFC/HFC, and HC/HC binary mixtures. The interaction parameter k i j was obtained for every binary mixture. It was assumed that k i j has contributions from the two components, and each component has its own constant contribution factor k i for the mixture, and the values of k i j indicate the degree in difference of properties between the two components. Therefore, the interaction parameters k i j is proposed as: k i j = k i − k j . The values of the mixing factor k i for Hydrofluorocarbons (HFCs) and Hydrocarbons (HCs), including propane, isobutane, n-butane, R23, R32, R125, R143a, R134a, R152a, R227ea R236fa, R236ea, and R245fa, were obtained by least-square fitting. In total, 39 refrigerant binary mixtures were analyzed on the basis of this method, and the results showed good agreement with experimental data. The overall average absolute deviations of pressure and vapor mole fraction are 1.3 % and 0.0089, respectively.

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Untitled

Cited by 15 publications

References 6 publications

Appendix B, Equations of States for Mixtures of R-32, R-125, R-134a, R-143a, and R-152a

Appendix B, Equations of States for Mixtures of R-32, R-125, R-134a, R-143a, and R-152a

Multicomponent Refrigerant Separation Using Extractive Distillation with Ionic Liquids

Study on the Interaction Coefficients in PR Equation with vdW Mixing Rules for HFC and HC Binary Mixtures

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