The Experts below are selected from a list of 17007 Experts worldwide ranked by ideXlab platform
Akio Miyara - One of the best experts on this subject based on the ideXlab platform.
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measurement of viscosity of trans 1 chloro 3 3 3 trifluoropropene r 1233zd e by tandem capillary tubes method
International Journal of Refrigeration-revue Internationale Du Froid, 2018Co-Authors: Akio Miyara, Md Jahangir Alam, Keishi KariyaAbstract:Abstract Measurements of viscosity of trans-1‑chloro‑3,3,3-trifluoropropene (R-1233zd(E)) in liquid and Vapor Phases are the key attention of the present study and we developed correlations to predict viscosities of saturated liquid and Vapor by extrapolating the data to saturation condition, which are useful in industrial design and simulation. R-1233zd(E) is being introduced as a potential candidate to be an alternative working fluid for high temperature heat pumps and organic Rankine cycles (ORCs). In this work, the viscosity of R-1233zd(E) was measured by a tandem capillary tubes method up to 4.07 MPa pressure over a temperature ranges from 314 K (40.85 °C) to 434 K (160.85 °C) and 394 K (120.85 °C) to 474 K (200.85 °C) for liquid and Vapor Phases, respectively. Total standard combined uncertainties in liquid and gas viscosity measurements are lower than ± 3.0% and ± 3.1%, respectively. On the other hand, there were large deviations between experimental data and REFPROP version 9.1 for the liquid viscosity in a range of -25 to -37% and those of Vapor phase are −7 to −16%. Experimental data of condensation heat transfer which cannot be correlated well with Nusselt's theory by REFPROP version 9.1 viscosity give a good agreement by using the present viscosity data.
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measurement of viscosity of trans 1 chloro 3 3 3 trifluoropropene r 1233zd e by tandem capillary tubes method
International Journal of Refrigeration-revue Internationale Du Froid, 2018Co-Authors: Akio Miyara, Md Jahangir Alam, Keishi KariyaAbstract:Abstract Measurements of viscosity of trans-1‑chloro‑3,3,3-trifluoropropene (R-1233zd(E)) in liquid and Vapor Phases are the key attention of the present study and we developed correlations to predict viscosities of saturated liquid and Vapor by extrapolating the data to saturation condition, which are useful in industrial design and simulation. R-1233zd(E) is being introduced as a potential candidate to be an alternative working fluid for high temperature heat pumps and organic Rankine cycles (ORCs). In this work, the viscosity of R-1233zd(E) was measured by a tandem capillary tubes method up to 4.07 MPa pressure over a temperature ranges from 314 K (40.85 °C) to 434 K (160.85 °C) and 394 K (120.85 °C) to 474 K (200.85 °C) for liquid and Vapor Phases, respectively. Total standard combined uncertainties in liquid and gas viscosity measurements are lower than ± 3.0% and ± 3.1%, respectively. On the other hand, there were large deviations between experimental data and REFPROP version 9.1 for the liquid viscosity in a range of -25 to -37% and those of Vapor phase are −7 to −16%. Experimental data of condensation heat transfer which cannot be correlated well with Nusselt's theory by REFPROP version 9.1 viscosity give a good agreement by using the present viscosity data.
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measurement of viscosity of cis 1 1 1 4 4 4 hexafluoro 2 butene r 1336mzz z by tandem capillary tubes method
Journal of Chemical & Engineering Data, 2018Co-Authors: Jahangir Alam, Akio Miyara, Keishi Kariya, Konstantinos KontomarisAbstract:The principal goals of the present work are to measure the viscosity of Vapor and liquid cis-1,1,1,4,4,4-hexafluoro-2-butene (R-1336mzz(Z)) and propose simplified correlations of the extracted data under saturation conditions for industrial design and simulation. R-1336mzz(Z), a hydro-fluoro-olefin with a low global warming potential and attractive environmental properties, can be considered as a potential working fluid for high-temperature heat pumps and organic Rankine cycles. Nevertheless, reliable experimental R-1336mzz(Z) viscosity data are lacking. This study presents R-1336mzz(Z) viscosity data measured by a tandem capillary tube method at temperatures from 314 (40.85 °C) to 434 K (160.85 °C) and 375 (101.85 °C) to 475 K (201.85 °C) for liquid and Vapor Phases, respectively, at pressures up to 4.06 MPa. Total standard uncertainties in liquid and gas viscosity measurements were lower than 3.04 and 3.21%, respectively.
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A fundamental equation of state for cis-1,3,3,3-tetrafluoropropene (R-1234ze(Z))
International Journal of Refrigeration, 2014Co-Authors: Ryo Akasaka, Yukihiro Higashi, Akio Miyara, Shigeru KoyamaAbstract:Abstract A fundamental equation of state is presented for cis-1,3,3,3-tetrafluoropropene (R-1234ze(Z)). The equation of state is expressed explicitly in the Helmholtz energy with independent variables of temperature and density. The equation of state is based on experimental data for the critical parameters, Vapor pressures, densities of the liquid and Vapor Phases, and sound speeds in the Vapor phase. All thermodynamic properties can be derived as derivatives of the Helmholtz energy. The equation is valid for temperatures from 273 K to 430 K and for pressures up to 6 MPa. The estimated uncertainties of properties calculated from the equation are 0.15% in Vapor pressures, 0.4% in Vapor densities, 0.2% in liquid densities, and 0.05% in the Vapor phase sound speeds. The equation exhibits reasonable extrapolation behavior in regions away from the experimental data.
Keishi Kariya - One of the best experts on this subject based on the ideXlab platform.
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measurement of viscosity of trans 1 chloro 3 3 3 trifluoropropene r 1233zd e by tandem capillary tubes method
International Journal of Refrigeration-revue Internationale Du Froid, 2018Co-Authors: Akio Miyara, Md Jahangir Alam, Keishi KariyaAbstract:Abstract Measurements of viscosity of trans-1‑chloro‑3,3,3-trifluoropropene (R-1233zd(E)) in liquid and Vapor Phases are the key attention of the present study and we developed correlations to predict viscosities of saturated liquid and Vapor by extrapolating the data to saturation condition, which are useful in industrial design and simulation. R-1233zd(E) is being introduced as a potential candidate to be an alternative working fluid for high temperature heat pumps and organic Rankine cycles (ORCs). In this work, the viscosity of R-1233zd(E) was measured by a tandem capillary tubes method up to 4.07 MPa pressure over a temperature ranges from 314 K (40.85 °C) to 434 K (160.85 °C) and 394 K (120.85 °C) to 474 K (200.85 °C) for liquid and Vapor Phases, respectively. Total standard combined uncertainties in liquid and gas viscosity measurements are lower than ± 3.0% and ± 3.1%, respectively. On the other hand, there were large deviations between experimental data and REFPROP version 9.1 for the liquid viscosity in a range of -25 to -37% and those of Vapor phase are −7 to −16%. Experimental data of condensation heat transfer which cannot be correlated well with Nusselt's theory by REFPROP version 9.1 viscosity give a good agreement by using the present viscosity data.
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measurement of viscosity of trans 1 chloro 3 3 3 trifluoropropene r 1233zd e by tandem capillary tubes method
International Journal of Refrigeration-revue Internationale Du Froid, 2018Co-Authors: Akio Miyara, Md Jahangir Alam, Keishi KariyaAbstract:Abstract Measurements of viscosity of trans-1‑chloro‑3,3,3-trifluoropropene (R-1233zd(E)) in liquid and Vapor Phases are the key attention of the present study and we developed correlations to predict viscosities of saturated liquid and Vapor by extrapolating the data to saturation condition, which are useful in industrial design and simulation. R-1233zd(E) is being introduced as a potential candidate to be an alternative working fluid for high temperature heat pumps and organic Rankine cycles (ORCs). In this work, the viscosity of R-1233zd(E) was measured by a tandem capillary tubes method up to 4.07 MPa pressure over a temperature ranges from 314 K (40.85 °C) to 434 K (160.85 °C) and 394 K (120.85 °C) to 474 K (200.85 °C) for liquid and Vapor Phases, respectively. Total standard combined uncertainties in liquid and gas viscosity measurements are lower than ± 3.0% and ± 3.1%, respectively. On the other hand, there were large deviations between experimental data and REFPROP version 9.1 for the liquid viscosity in a range of -25 to -37% and those of Vapor phase are −7 to −16%. Experimental data of condensation heat transfer which cannot be correlated well with Nusselt's theory by REFPROP version 9.1 viscosity give a good agreement by using the present viscosity data.
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measurement of viscosity of cis 1 1 1 4 4 4 hexafluoro 2 butene r 1336mzz z by tandem capillary tubes method
Journal of Chemical & Engineering Data, 2018Co-Authors: Jahangir Alam, Akio Miyara, Keishi Kariya, Konstantinos KontomarisAbstract:The principal goals of the present work are to measure the viscosity of Vapor and liquid cis-1,1,1,4,4,4-hexafluoro-2-butene (R-1336mzz(Z)) and propose simplified correlations of the extracted data under saturation conditions for industrial design and simulation. R-1336mzz(Z), a hydro-fluoro-olefin with a low global warming potential and attractive environmental properties, can be considered as a potential working fluid for high-temperature heat pumps and organic Rankine cycles. Nevertheless, reliable experimental R-1336mzz(Z) viscosity data are lacking. This study presents R-1336mzz(Z) viscosity data measured by a tandem capillary tube method at temperatures from 314 (40.85 °C) to 434 K (160.85 °C) and 375 (101.85 °C) to 475 K (201.85 °C) for liquid and Vapor Phases, respectively, at pressures up to 4.06 MPa. Total standard uncertainties in liquid and gas viscosity measurements were lower than 3.04 and 3.21%, respectively.
Ki Hyun Park - One of the best experts on this subject based on the ideXlab platform.
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phase equilibria of cfc alternative refrigerant mixtures binary systems of trifluoromethane hfc 23 1 1 1 2 tetrafluoroethane hfc 134a and trifluoromethane hfc 23 1 1 1 2 3 3 3 heptafluoropropane hfc 227ea at 283 15 and 293 15 k
Journal of Chemical & Engineering Data, 2001Co-Authors: Ki Hyun ParkAbstract:Isothermal Vapor−liquid equilibria for the binary mixtures of trifluoromethane (HFC-23) + 1,1,1,2-tetrafluoroethane (HFC-134a) and trifluoromethane + 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea) were measured at 283.15 and 293.15 K. The experiments were carried out with a circulation-type equilibrium apparatus with measurement of the temperature, pressure, and compositions of the liquid and Vapor Phases. The experimental data were correlated with the Peng−Robinson equation of state using the Wong−Sandler mixing rules. Results calculated with this equation showed good agreement with the experimental data. Azeotropic behavior has not been found in either of these mixtures.
Md Jahangir Alam - One of the best experts on this subject based on the ideXlab platform.
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measurement of viscosity of trans 1 chloro 3 3 3 trifluoropropene r 1233zd e by tandem capillary tubes method
International Journal of Refrigeration-revue Internationale Du Froid, 2018Co-Authors: Akio Miyara, Md Jahangir Alam, Keishi KariyaAbstract:Abstract Measurements of viscosity of trans-1‑chloro‑3,3,3-trifluoropropene (R-1233zd(E)) in liquid and Vapor Phases are the key attention of the present study and we developed correlations to predict viscosities of saturated liquid and Vapor by extrapolating the data to saturation condition, which are useful in industrial design and simulation. R-1233zd(E) is being introduced as a potential candidate to be an alternative working fluid for high temperature heat pumps and organic Rankine cycles (ORCs). In this work, the viscosity of R-1233zd(E) was measured by a tandem capillary tubes method up to 4.07 MPa pressure over a temperature ranges from 314 K (40.85 °C) to 434 K (160.85 °C) and 394 K (120.85 °C) to 474 K (200.85 °C) for liquid and Vapor Phases, respectively. Total standard combined uncertainties in liquid and gas viscosity measurements are lower than ± 3.0% and ± 3.1%, respectively. On the other hand, there were large deviations between experimental data and REFPROP version 9.1 for the liquid viscosity in a range of -25 to -37% and those of Vapor phase are −7 to −16%. Experimental data of condensation heat transfer which cannot be correlated well with Nusselt's theory by REFPROP version 9.1 viscosity give a good agreement by using the present viscosity data.
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measurement of viscosity of trans 1 chloro 3 3 3 trifluoropropene r 1233zd e by tandem capillary tubes method
International Journal of Refrigeration-revue Internationale Du Froid, 2018Co-Authors: Akio Miyara, Md Jahangir Alam, Keishi KariyaAbstract:Abstract Measurements of viscosity of trans-1‑chloro‑3,3,3-trifluoropropene (R-1233zd(E)) in liquid and Vapor Phases are the key attention of the present study and we developed correlations to predict viscosities of saturated liquid and Vapor by extrapolating the data to saturation condition, which are useful in industrial design and simulation. R-1233zd(E) is being introduced as a potential candidate to be an alternative working fluid for high temperature heat pumps and organic Rankine cycles (ORCs). In this work, the viscosity of R-1233zd(E) was measured by a tandem capillary tubes method up to 4.07 MPa pressure over a temperature ranges from 314 K (40.85 °C) to 434 K (160.85 °C) and 394 K (120.85 °C) to 474 K (200.85 °C) for liquid and Vapor Phases, respectively. Total standard combined uncertainties in liquid and gas viscosity measurements are lower than ± 3.0% and ± 3.1%, respectively. On the other hand, there were large deviations between experimental data and REFPROP version 9.1 for the liquid viscosity in a range of -25 to -37% and those of Vapor phase are −7 to −16%. Experimental data of condensation heat transfer which cannot be correlated well with Nusselt's theory by REFPROP version 9.1 viscosity give a good agreement by using the present viscosity data.
Deresh Ramjugernath - One of the best experts on this subject based on the ideXlab platform.
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isothermal Vapor liquid equilibrium data for binary mixtures of hexafluoroethane r116 n pentane or n hexane at two temperatures 288 and 296 k
Journal of Chemical & Engineering Data, 2018Co-Authors: Deresh Ramjugernath, Alain Valtz, Dominique Richon, Mark D Williamswynn, Christophe CoqueletAbstract:The isothermal Vapor–liquid equilibrium (VLE) data for two hexafluoroethane (R-116)/n-alkane systems were each measured at two temperatures of 288 and 296 K. The two n-alkanes of interest are n-pentane and n-hexane. The pressures which were measured ranged from 0.017 to 7.040 MPa. A “static-analytic” VLE apparatus, equipped with pneumatic Rapid Online Sampler-Injector (ROLSI) capillary samplers, was used to perform the measurements. The ROLSI gives this apparatus the capability of sampling both the liquid and the Vapor Phases, without significant equilibrium perturbation with respect to the estimated analytical uncertainties. Vapor–liquid–liquid equilibria and liquid–liquid equilibria were experienced at R-116 compositions close to unity for the R-116 and n-hexane system. Each of the four P–x–y VLE data sets was correlated with the Peng–Robinson equation of state, modified by the inclusion of the Mathias-Copeman alpha function in preference to the original Peng-Robinson configuration. The Wong-Sandler mix...
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isothermal Vapor liquid equilibrium data for the 1 1 2 2 tetrafluoroethene 1 1 2 2 3 3 4 4 octafluorocyclobutane binary system measurement and modeling from 248 to 283 k
Journal of Chemical & Engineering Data, 2012Co-Authors: Francois Jacobus Conradie, Philippus L. Crouse, Xavier Courtial, Izak J. Van Der Walt, Deresh RamjugernathAbstract:High pressure Vapor–liquid equilibrium data are presented for the 1,1,2,2-tetrafluoroethene + 1,1,2,2,3,3,4,4-octafluorocyclobutane binary system. The isothermal measurements were undertaken at (248.3, 263.0, and 282.9) K, with pressures ranging from (0.040 to 2.340) MPa. A static–analytical apparatus was used to carry out the measurements. The liquid and Vapor Phases were sampled at equilibrium using a movable rapid on-line sampler–injector (ROLSI). The uncertainties in the measurements are less than 0.1 K, 1.5 kPa, and 0.007 for the temperature, pressure, and equilibrium phase mole fractions, respectively. The experimental data were correlated with the Peng–Robinson equation of state incorporating the Mathias–Copeman alpha function, with the Wong–Sandler mixing rule utilizing the nonrandom two-liquid (NRTL) activity coefficient model. The model accurately describes the experimental data.
