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Zeshao Chen - One of the best experts on this subject based on the ideXlab platform.
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vapor liquid equilibria measurements of 1 1 1 2 tetrafluoroethane hfc 134a 2 3 3 3 tetrafluoroprop 1 ene hfo 1234yf isobutane hc 600a ternary system
Fluid Phase Equilibria, 2016Co-Authors: Wanbao Zhu, Longxiang Chen, Xudong Cai, Zeshao ChenAbstract:Abstract Vapor–liquid equilibrium data for the ternary mixture of 1,1,1,2-tetrafluoroethane (HFC-134a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) + isobutane (HC-600a) were measured at temperatures from 283.15 K to 323.15 K using a recirculation apparatus. The uncertainties of the experimental data are estimated within 5 mK, 0.5 kPa, and 0.003 for the temperature, pressure, and the equilibrium liquid and vapor mole fractions, respectively. The experimental data were compared with the predicted data by the Peng Robinson equation of state with the vdW Mixing Rule and the Wong Sandler Mixing Rule, respectively. The binary interaction parameters of each binary mixture were determined from the experimental data in literature. The results show that the predicted data agree well with the experimental data. It indicates that the PR equation can be used to predict VLE data of ternary mixture of HFC-134a + HFO-1234yf + HC-600a. The proposed ternary mixture has potential to be refrigerant with low GWP and excellent thermodynamic performance.
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vapor liquid equilibria for binary system of 2 3 3 3 tetrafluoroprop 1 ene hfo 1234yf isobutane hc 600a
Fluid Phase Equilibria, 2014Co-Authors: Longxiang Chen, Zeshao ChenAbstract:Abstract Isothermal vapor–liquid equilibrium data for the binary mixture of 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) + isobutane (HC-600a) were measured at temperatures from 283.15 to 323.15 K using a recirculation apparatus. The experimental data were correlated using the Peng–Robinson equation of state with vdW Mixing Rule and Wong–Sandler Mixing Rule, respectively. The comparison between the correlation results and experimental data showed a good agreement, and Wong–Sandler Mixing Rule gave more accurate calculations for this binary system. Azeotropic behavior was found at high mole fraction of HFO-1234yf.
Longxiang Chen - One of the best experts on this subject based on the ideXlab platform.
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vapor liquid equilibria measurements of 1 1 1 2 tetrafluoroethane hfc 134a 2 3 3 3 tetrafluoroprop 1 ene hfo 1234yf isobutane hc 600a ternary system
Fluid Phase Equilibria, 2016Co-Authors: Wanbao Zhu, Longxiang Chen, Xudong Cai, Zeshao ChenAbstract:Abstract Vapor–liquid equilibrium data for the ternary mixture of 1,1,1,2-tetrafluoroethane (HFC-134a) + 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) + isobutane (HC-600a) were measured at temperatures from 283.15 K to 323.15 K using a recirculation apparatus. The uncertainties of the experimental data are estimated within 5 mK, 0.5 kPa, and 0.003 for the temperature, pressure, and the equilibrium liquid and vapor mole fractions, respectively. The experimental data were compared with the predicted data by the Peng Robinson equation of state with the vdW Mixing Rule and the Wong Sandler Mixing Rule, respectively. The binary interaction parameters of each binary mixture were determined from the experimental data in literature. The results show that the predicted data agree well with the experimental data. It indicates that the PR equation can be used to predict VLE data of ternary mixture of HFC-134a + HFO-1234yf + HC-600a. The proposed ternary mixture has potential to be refrigerant with low GWP and excellent thermodynamic performance.
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vapor liquid equilibria for binary system of 2 3 3 3 tetrafluoroprop 1 ene hfo 1234yf isobutane hc 600a
Fluid Phase Equilibria, 2014Co-Authors: Longxiang Chen, Zeshao ChenAbstract:Abstract Isothermal vapor–liquid equilibrium data for the binary mixture of 2,3,3,3-tetrafluoroprop-1-ene (HFO-1234yf) + isobutane (HC-600a) were measured at temperatures from 283.15 to 323.15 K using a recirculation apparatus. The experimental data were correlated using the Peng–Robinson equation of state with vdW Mixing Rule and Wong–Sandler Mixing Rule, respectively. The comparison between the correlation results and experimental data showed a good agreement, and Wong–Sandler Mixing Rule gave more accurate calculations for this binary system. Azeotropic behavior was found at high mole fraction of HFO-1234yf.
M Gong - One of the best experts on this subject based on the ideXlab platform.
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the investigation on the vapor liquid phase equilibrium of trifluoromethane difluoromethane system at temperatures ranging from 223 150 to 273 150 k
The Journal of Chemical Thermodynamics, 2020Co-Authors: Xian Wang, M Gong, Xueqiang Dong, Yanxing Zhao, Xiaoyu Yao, Jun ShenAbstract:Abstract The trifluoromethane (R23) and difluoromethane (R32) are widely used in refrigeration and chemical industry. The isothermal vapor plus liquid equilibrium (VLE) data for the R23 plus R32 system were determined experimentally at six temperatures from 223.150 K to 273.150 K. Two models were employed to regress the experimental VLE data: Peng–Robinson (PR) equation of state with the one-parameter van der Waals (vdW) Mixing Rule; Peng–Robinson equation of state combined non-random two-liquid (NRTL) activity coefficient model with the modified Huron-Vidal two-order (MHV2) Mixing Rule. The maximum average absolute relative deviation of pressure (AARDp) and average absolute deviation of vapor phase mole fraction (AADy) for PR-vdW are 2.71% and 0.0175, respectively, while the maximum AARDp and AADy for PR-MHV2-NRTL are 1.53% and 0.0148, respectively.
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the investigation on the vapour liquid phase equilibrium of ammonia 1 1 1 2 tetrafluoroethane system over the temperatures ranging from 243 150 to 283 150 k
The Journal of Chemical Thermodynamics, 2017Co-Authors: Yanxing Zhao, M Gong, Xueqiang Dong, Quan Zhong, Jun ShenAbstract:Abstract To blend ammonia with some hydrofluorocarbons may give these mixed refrigerants lower flammability and global warming potential. In this paper, the isothermal vapour liquid equilibrium (VLE) of (ammonia + 1,1,1,2-tetrafluoroethane) system at temperatures ranging from (243.150 to 283.150) K are presented. Two models were employed to regress the experimental VLE results, namely the Peng–Robinson (PR) equation of state with the simple van der waals (VDW) Mixing Rule; the Peng–Robinson equation of state combined non-random two-liquid (NRTL) activity coefficient model with the modified Huron-Vidal one-order (MHV1) Mixing Rule. The maximum average absolute relative deviation of pressure (AARD p ) and average absolute deviation of the vapour phase mole fraction (AAD y ) for PR-VDW are 0.56% and 0.010, respectively, while the maximum AARD p and AAD y for PR-MHV1-NRTL are 0.27% and 0.014, respectively. Positive azeotropic behaviour was exhibited at each temperature investigated.
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measurements and correlations of isothermal vapour liquid equilibrium for the isobutane r600a cis 1 3 3 3 tetrafluoropropene r1234ze z system at temperatures from 303 150 to 353 150 k
The Journal of Chemical Thermodynamics, 2016Co-Authors: Xuedong Zhang, M Gong, Hao Guo, Xueqiang Dong, Jun ShenAbstract:Abstract In this paper, the (vapour + liquid) phase equilibrium for the (isobutane + cis-1,3,3,3-tetrafluoropropene) system was measured by the static-analytical method at six temperatures from (303.150 to 353.150) K. The combined standard uncertainties of the temperature, pressure and composition were less than ±5 mK, ±0.0005 MPa and ±0.005, respectively. The experimental results were correlated by means of the Peng–Robison (PR) equation of state (EoS) with Van der Waals (VDW) Mixing Rule and Huron–Vidal (HV) Mixing Rule involving the non-random two-liquid (NRTL) activity coefficient model. Good consistency is found by both models. The average absolute relative deviations of pressure are between 0.44% and 0.58% for the PR-VDW model, while the average absolute relative deviations of pressure are between 0.12% and 0.44% for the PR-HV-NRTL model. The average absolute deviations of vapour phase mole fraction lay between 0.007 and 0.008 for the PR-VDW model, while the average absolute deviations of vapour phase mole fraction lay between 0.004 and 0.008 for the PR-HV-NRTL model. The results show that the PR-HV-NRTL model has better performance than that of the PR-VDW model for the binary system. Obviously an azeotropic behaviour can be observed for the system.
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vapour liquid equilibrium data for the 1 1 difluoroethane r152a 1 1 1 3 3 pentafluoropropane r245fa system at temperatures from 323 150 to 353 150 k
The Journal of Chemical Thermodynamics, 2015Co-Authors: Lixiang Yang, M Gong, Hao Guo, Xueqiang DongAbstract:Abstract In this paper, (vapour + liquid) equilibrium (VLE) for the {1,1-difluoroethane (R152a) + 1,1,1,3,3-pentafluoropropane (R245fa)} system was determined by a static-analytical method at T = (323.150 to 353.150) K. Values of the VLE were correlated by the Peng–Robison equation of state (PR EoS) using two different models, the van der Waals (vdWs) Mixing Rule and the Huron–Vidal (HV) Mixing Rule involving the non-random two-liquid (NRTL) activity coefficient model. The correlated results show good agreement with the experimental values. For the two models, the maximum average absolute deviations of the vapour phase mole fraction are 0.0034 and 0.0035, respectively.
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a static analytical apparatus for vapour pressures and vapour liquid phase equilibrium measurements with an internal stirrer and view windows
The Journal of Chemical Thermodynamics, 2014Co-Authors: Hao Guo, M Gong, Xueqiang DongAbstract:Abstract A new static analytical apparatus for reliable vapour pressures and (vapour + liquid) equilibrium data of small-scale cell (≈150 mL) with internal stirrer and view windows was designed. In this work, the compositions of the phases were analyzed by a gas chromatograph connected on-line with TCD detectors. The operating pressure ranges from (0 to 3000) kPa, and the operating temperature range from (293 to 400) K. Phase equilibrium data for previously reported systems were first measured to test the credibility of the newly developed apparatus. The test included vapour pressure of 1,1,1,3,3-pentafluoropropane (R245fa) and isobutane (R600a), VLE of the (R600a + R245fa) system from T = (293.150 to 343.880) K. The measured VLE data are regressed with thermodynamic models using Peng–Robinson EoS with two different models, viz. the van der Waals Mixing Rule, and the Huron–Vidal Mixing Rule utilising the non-random two-liquid activity coefficient model. Thermodynamic consistency testing is also performed for the newly measured experimental data.
Martin Aznar - One of the best experts on this subject based on the ideXlab platform.
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density refraction index and vapor liquid equilibria of n methyl 2 hydroxyethylammonium butyrate plus methyl acetate or ethyl acetate or propyl acetate at several temperatures
The Journal of Chemical Thermodynamics, 2013Co-Authors: Victor H Alvarez, Silvana Mattedi, Martin AznarAbstract:Abstract This paper reports the densities, refraction indices, and vapor liquid equilibria for binary systems ester + N-methyl-2-hydroxyethylammonium butyrate (m-2-HEAB): methyl acetate (1) + m-2-HEAB (2), ethyl acetate (1) + m-2-HEAB and propyl acetate (1) + m-2-HEAB (2). The excess molar volumes, deviations in the refraction index, apparent molar volumes, and thermal expansion coefficients for the binary systems were fitted to polynomial equations. The Peng–Robinson equation of state, coupled with the Wong–Sandler Mixing Rule, is used to describe the experimental data. Since the predictive activity coefficient model COSMO-SAC is used in the Wong–Sandler Mixing Rule, the resulting thermodynamic model is a completely predictive one. The prediction results for the density and for the vapor–liquid equilibria have a deviation lower than 1.0% and 1.1%, respectively.
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density refraction index and vapor liquid equilibria of n methyl 2 hydroxyethylammonium hexanoate plus methyl acetate ethyl acetate or propyl acetate at several temperatures
Industrial & Engineering Chemistry Research, 2012Co-Authors: Victor H Alvarez, Silvana Mattedi, Martin AznarAbstract:This paper reports the densities, refraction indices, and vapor liquid equilibria for binary systems ester + n-methyl2-hydroxyethylammonium hexanoate (m-2-HEAH): methyl acetate (1) + m-2-HEAH (2), ethyl acetate (1) + m-2-HEAH, and propyl acetate (1) + m-2-HEAH (2). The excess molar volumes, deviations in the refraction index, apparent molar volume, and thermal expansion coefficient for the binary systems were fitted to polynomial equations. The Peng—Robinson equation of state, coupled with the Wong―Sandler Mixing Rule, is used to describe the experimental data. Since the predictive activity coefficient model COSMO-SAC is used in the Wong—Sandler Mixing Rule, the resulting thermodynamic model is a completely predictive one. The prediction results for the density and for the vapor―liquid equilibria have a deviation lower than 1.6% and 1.1%, respectively.
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density refraction index and vapor liquid equilibria of n methyl 2 hydroxyethylammonium hexanoate plus methyl acetate ethyl acetate or propyl acetate at several temperatures
Industrial & Engineering Chemistry Research, 2012Co-Authors: V Alvarez, Silvana Mattedi, Martin AznarAbstract:This pap er reports the densities, refraction indices, and vapor liquid equilibria for binary systems ester + N-methyl-2-hydroxyethylammonium butyrat e (m-2-HEAB): methyl acetate (1) + m-2-HEAB (2), ethyl acetate (1) + m-2-HEAB and propy l acetate (1) + m-2-HEAB (2). The excess molar volumes, deviations in the refraction index, apparent molar volumes, and thermal expansion coefficients for the binary systems were fitted to polynomial equations. The Peng–Robinson equation of state, coupled with the Wong–Sandler Mixing Rule, is used to describe the experimen tal data. Since the predictive activity coefficient model COSMO-SAC is used in the Wong–Sandler Mixing Rule, the resulting thermodynamic model is a completely predictive one. The prediction results for the density and for the vapor–liquid equilibria have a deviation lower than 1.0% and 1.1%, respectively.
Xueqiang Dong - One of the best experts on this subject based on the ideXlab platform.
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the investigation on the vapor liquid phase equilibrium of trifluoromethane difluoromethane system at temperatures ranging from 223 150 to 273 150 k
The Journal of Chemical Thermodynamics, 2020Co-Authors: Xian Wang, M Gong, Xueqiang Dong, Yanxing Zhao, Xiaoyu Yao, Jun ShenAbstract:Abstract The trifluoromethane (R23) and difluoromethane (R32) are widely used in refrigeration and chemical industry. The isothermal vapor plus liquid equilibrium (VLE) data for the R23 plus R32 system were determined experimentally at six temperatures from 223.150 K to 273.150 K. Two models were employed to regress the experimental VLE data: Peng–Robinson (PR) equation of state with the one-parameter van der Waals (vdW) Mixing Rule; Peng–Robinson equation of state combined non-random two-liquid (NRTL) activity coefficient model with the modified Huron-Vidal two-order (MHV2) Mixing Rule. The maximum average absolute relative deviation of pressure (AARDp) and average absolute deviation of vapor phase mole fraction (AADy) for PR-vdW are 2.71% and 0.0175, respectively, while the maximum AARDp and AADy for PR-MHV2-NRTL are 1.53% and 0.0148, respectively.
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the investigation on the vapour liquid phase equilibrium of ammonia 1 1 1 2 tetrafluoroethane system over the temperatures ranging from 243 150 to 283 150 k
The Journal of Chemical Thermodynamics, 2017Co-Authors: Yanxing Zhao, M Gong, Xueqiang Dong, Quan Zhong, Jun ShenAbstract:Abstract To blend ammonia with some hydrofluorocarbons may give these mixed refrigerants lower flammability and global warming potential. In this paper, the isothermal vapour liquid equilibrium (VLE) of (ammonia + 1,1,1,2-tetrafluoroethane) system at temperatures ranging from (243.150 to 283.150) K are presented. Two models were employed to regress the experimental VLE results, namely the Peng–Robinson (PR) equation of state with the simple van der waals (VDW) Mixing Rule; the Peng–Robinson equation of state combined non-random two-liquid (NRTL) activity coefficient model with the modified Huron-Vidal one-order (MHV1) Mixing Rule. The maximum average absolute relative deviation of pressure (AARD p ) and average absolute deviation of the vapour phase mole fraction (AAD y ) for PR-VDW are 0.56% and 0.010, respectively, while the maximum AARD p and AAD y for PR-MHV1-NRTL are 0.27% and 0.014, respectively. Positive azeotropic behaviour was exhibited at each temperature investigated.
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measurements and correlations of isothermal vapour liquid equilibrium for the isobutane r600a cis 1 3 3 3 tetrafluoropropene r1234ze z system at temperatures from 303 150 to 353 150 k
The Journal of Chemical Thermodynamics, 2016Co-Authors: Xuedong Zhang, M Gong, Hao Guo, Xueqiang Dong, Jun ShenAbstract:Abstract In this paper, the (vapour + liquid) phase equilibrium for the (isobutane + cis-1,3,3,3-tetrafluoropropene) system was measured by the static-analytical method at six temperatures from (303.150 to 353.150) K. The combined standard uncertainties of the temperature, pressure and composition were less than ±5 mK, ±0.0005 MPa and ±0.005, respectively. The experimental results were correlated by means of the Peng–Robison (PR) equation of state (EoS) with Van der Waals (VDW) Mixing Rule and Huron–Vidal (HV) Mixing Rule involving the non-random two-liquid (NRTL) activity coefficient model. Good consistency is found by both models. The average absolute relative deviations of pressure are between 0.44% and 0.58% for the PR-VDW model, while the average absolute relative deviations of pressure are between 0.12% and 0.44% for the PR-HV-NRTL model. The average absolute deviations of vapour phase mole fraction lay between 0.007 and 0.008 for the PR-VDW model, while the average absolute deviations of vapour phase mole fraction lay between 0.004 and 0.008 for the PR-HV-NRTL model. The results show that the PR-HV-NRTL model has better performance than that of the PR-VDW model for the binary system. Obviously an azeotropic behaviour can be observed for the system.
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vapour liquid equilibrium data for the 1 1 difluoroethane r152a 1 1 1 3 3 pentafluoropropane r245fa system at temperatures from 323 150 to 353 150 k
The Journal of Chemical Thermodynamics, 2015Co-Authors: Lixiang Yang, M Gong, Hao Guo, Xueqiang DongAbstract:Abstract In this paper, (vapour + liquid) equilibrium (VLE) for the {1,1-difluoroethane (R152a) + 1,1,1,3,3-pentafluoropropane (R245fa)} system was determined by a static-analytical method at T = (323.150 to 353.150) K. Values of the VLE were correlated by the Peng–Robison equation of state (PR EoS) using two different models, the van der Waals (vdWs) Mixing Rule and the Huron–Vidal (HV) Mixing Rule involving the non-random two-liquid (NRTL) activity coefficient model. The correlated results show good agreement with the experimental values. For the two models, the maximum average absolute deviations of the vapour phase mole fraction are 0.0034 and 0.0035, respectively.
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a static analytical apparatus for vapour pressures and vapour liquid phase equilibrium measurements with an internal stirrer and view windows
The Journal of Chemical Thermodynamics, 2014Co-Authors: Hao Guo, M Gong, Xueqiang DongAbstract:Abstract A new static analytical apparatus for reliable vapour pressures and (vapour + liquid) equilibrium data of small-scale cell (≈150 mL) with internal stirrer and view windows was designed. In this work, the compositions of the phases were analyzed by a gas chromatograph connected on-line with TCD detectors. The operating pressure ranges from (0 to 3000) kPa, and the operating temperature range from (293 to 400) K. Phase equilibrium data for previously reported systems were first measured to test the credibility of the newly developed apparatus. The test included vapour pressure of 1,1,1,3,3-pentafluoropropane (R245fa) and isobutane (R600a), VLE of the (R600a + R245fa) system from T = (293.150 to 343.880) K. The measured VLE data are regressed with thermodynamic models using Peng–Robinson EoS with two different models, viz. the van der Waals Mixing Rule, and the Huron–Vidal Mixing Rule utilising the non-random two-liquid activity coefficient model. Thermodynamic consistency testing is also performed for the newly measured experimental data.