(Vapour + liquid) equilibrium data for the binary system of {trifluoroiodomethane (R13I1) + trans-1, 3, 3, 3-tetrafluoropropene (R1234ze (E))} at various temperatures from (258.150 to 298.150) K

doi:10.1016/j.jct.2011.11.024

The Journal of Chemical Thermodynamics

Volume 47, April 2012, Pages 397-401

https://doi.org/10.1016/j.jct.2011.11.024 Get rights and content

Abstract

(Vapour + liquid) equilibrium (VLE) data for the binary system of {trifluoroiodomethane (R13I1) + trans-1, 3, 3, 3-tetrafluoropropene (R1234ze (E))} were measured by a static-analytic method within the temperature range of (258.150 to 298.150) K. The experimental data were correlated using the Peng–Robinson equation of state (PR EoS) with the Huron–Vidal (HV) mixing rule involving the NRTL activity coefficient model. The results show good agreement with experimental values for the binary system at each temperature point. The maximum average absolute relative deviation of pressure is 0.28%, while the maximum average absolute deviation of vapour phase mole fraction is 0.0025. Obviously azeotropic behaviour can be found for the measured temperature range here.

Highlights

► VLE data for {R13I1 + R1234ze (E)} systems were measured. ► This work was based on the static-analytic method. ► The VLE data were correlated using the PR-HV-NRTL model. ► Obviously azeotropic behavior can be found.

Introduction

According to the Montreal protocol, traditional chlorofluorocarbon (CFC) and hydrochlorofluorocarbon (HCFC) refrigerants have already been or will be phased out owing to their ozone depletion potential (ODP) and high global warming potential (GWP). Hydrofluorocarbons (HFCs), hydrocarbons (HCs) and their mixtures are promising alternative refrigerants to replace those CFCs and HCFCs. Besides, there are a great variety of potential applications of HFCs, HCs and their mixtures in the organic Rankine cycle (ORC) [1]. Since it is very hard to find appropriate pure substance to replace the traditional refrigerants or ORC working fluids, mixtures especially azeotropic mixtures may be potential alternative working fluids. (Vapour + liquid) equilibrium data are one of the most important parameters used to calculate the performance of refrigeration cycle or organic Rankine cycle and optimize proportion.

In this work, VLE data for the binary system of {trifluoroiodomethane (R13I1) + trans-1, 3, 3, 3-tetrafluoropropene (R1234ze (E))} were measured by a static-analytic method and correlated using the Peng–Robinson [2] equation of state (PR EoS) with the Huron–Vidal (HV) mixing rule [3] involving the NRTL [4] activity coefficient model (PR-HV-NRTL model). The azeotropic behaviour was found within the experimental temperature range of (258.150 to 298.150) K.

Section snippets

Materials

The R13I1 and R1234ze (E) were supplied by Nanjing Yuji Tuohao Co. Ltd with a declared mole fraction purity of 0.990 and 0.995, respectively. Both of the materials were used without any further purification.

Experimental apparatus

All of the VLE data were determined by the same apparatus described by Dong et al. [5], [6]. The measurements in this work were conducted based on a static-analytic method by turning off the self-designed electromagnetic pump.

The equilibrium cell with two glasses was immersed in an

Results and correlation

The VLE data for the {R13I1 + R1234ze (E)} system were determined at various temperatures from (258.150 to 298.150) K. The experimental VLE data were correlated with the PR-HV-NRTL model. The critical temperature, critical pressure, and acentric factor for each pure component are listed in table 1 [7], [8], [9].

The PR EoS [2] is expressed as follows: $p = \frac{RT}{v - b} - \frac{a (T)}{v (v + b) + b (v - b)},$ where p is the pressure, R is the gas constant (R = 8.314 J · K⁻¹ · mol⁻¹), v is the molar volume, T is the temperature, while a

Conclusions

In this work, (vapour + liquid) equilibrium data for the binary system of {trifluoroiodomethane (R13I1) + trans-1, 3, 3, 3-tetrafluoropropene (R1234ze (E))} were determined by a static-analytic method within the temperature range of (258.150 to 298.150) K. All of the experimental data were correlated using the PR EoS with the HV mixing rule involving the NRTL activity coefficient model (PR-HV-NRTL model). The results show good agreement between experimental and calculated data at each temperature.

Acknowledgements

This work was financially supported by the National Basic Research Program of China under the contract number of 2011CB710701 and the National Natural Sciences Foundation of China under the contract number of 50890183.

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Citation Excerpt :
In this study, the PC-SAFT equation was chosen as a thermodynamic model for determining the azeotropic position for binary mixtures of new refrigerants. The method is verified with 8 binary systems, which are: R13I1 + R152a [16], R13I1 + R1234ze [17], R13I1 + R134 [18], R134 + R1234ze [19], R152a + R134 [20], R1234ze + R600a [21], R600 + R245fa [22] and R1234ze + R290 [23]. First, the thermodynamic model is described.
In this work, we present a novel approach to predict the location of azeotropes for binary mixtures using the perturbed-chain statistical associating fluid theory equation of state (PC-SAFT).The proposed method requires as input the pure-component parameters of the PC-SAFT equation: the segment number (m), the hard-core segment diameter (σ), and the segment-segment interaction energy parameter (ε/k) for every pure non-associating fluid. By using these parameters, PC-SAFT estimates with accuracy the azeotropes properties of binary mixtures as well as the successful prediction of vapour-liquid equilibria for many non-associating binary systems. In order to improve the predictive ability of the PC-SAFT equation, the interaction parameters of 8 binary systems containing novel refrigeration fluid, were estimated from binary vapour–liquid equilibrium data. For comparison, the data were also modelled using the (PR-MC-WS-NRTL) thermodynamic model. Good agreements are found between the calculated results and reference data and the relative error does not exceed 3.69% and 0.97% for the molar fraction and the pressure respectively.

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(Vapour + liquid) equilibrium data for the binary system of {trifluoroiodomethane (R13I1) + trans-1, 3, 3, 3-tetrafluoropropene (R1234ze (E))} at various temperatures from (258.150 to 298.150) K

Abstract

Highlights

Introduction

Section snippets

Materials

Experimental apparatus

Results and correlation

Conclusions

Acknowledgements

Renew. Sustain. Energ. Rev.

Fluid Phase Equilib.

J. Chem. Thermodyn.

J. Int. J. Refrigerat.

Int. J. Refrigerat.