High-pressure fluid-phase equilibria: Experimental methods and systems investigated (2000-2004)

Abstract This study reviews the current state of the art and the current research activities of high temperature heat pumps (HTHPs) with heat sink temperatures in the range of 90 to 160 °C. The focus is on the analysis of the heat pump cycles and the suitable refrigerants. More than 20 HTHPs from 13 manufacturers have been identified on the market that are able to provide heat sink temperatures of at least 90 °C. Large application potentials have been recognized particularly in the food, paper, metal and chemical industries. The heating capacities range from about 20 kW to 20 MW. Most cycles are single-stage and differ primarily in the refrigerant (e.g. R245fa, R717, R744, R134a or R1234ze(E)) and compressor type used. The COPs range from 2.4 to 5.8 at a temperature lift of 95 to 40 K. Several research projects push the limits of the achievable COPs and heat sink temperatures to higher levels. COPs of about 5.7 to 6.5 (at 30 K lift) and 2.2 and 2.8 (70 K) are achieved at a sink temperature of 120 °C. The refrigerants investigated are mainly R1336mzz(Z), R718, R245fa, R1234ze(Z), R600, and R601. R1336mzz(Z) enables to achieve exceptionally high heat sink temperatures of up to 160 °C.

High Temperature Heat Pumps: Market Overview, Stateof the Art, Research Status, Refrigerants, and Application Potentials

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Advanced Engineering Thermodynamics

Peng-Robinson equation of state: 40 years through cubics

The EU Regulation No 517/2014 is going to phase-out most of the refrigerants commonly used in refrigeration and air conditioning systems (R134a, R404A and R410A) because of their extended use and their high GWP values. There are very different options to replace them; however, no refrigerant has yet imposed. In this paper we review and analyze the different mixtures proposed by the AHRI as alternative refrigerants to those employed currently. These mixtures are composed by HFC refrigerants: R32, R125, R152a and R134a; and HFO refrigerants: R1234yf and R1234ze(E). It is concluded, from the theoretical analysis, that most of the new HFO/HFC mixtures perform under the HFC analyzed (although some experimental studies show the contrary) and, in most cases, do not meet the GWP restrictions approved by the European normative. Furthermore, some of the mixtures proposed would have problems due to their flammability.

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Analysis based on EU Regulation No 517/2014 of new HFC/HFO mixtures as alternatives of high GWP refrigerants in refrigeration and HVAC systems

The VLE data for the binary system of R1234ze(E) + R290 were measured with a recirculation method at four temperatures (258.150, 263.150, 273.150 and 283.150 K). The measured uncertainties of the temperature, pressure, and compositions are ±5 mK, ±0.0005 MPa, and ±0.005, respectively. All the experimental data were correlated by the Peng–Robinson (PR) EoS with the Huron–Vidal (HV) mixing rule involving the non-random two-liquid (NRTL) activity coefficient (PR–HV–NRTL) model. Azeotropic behavior can be found at the measured temperature range.

Experimental measurement of vapor–liquid equilibrium for (trans-1,3,3,3-tetrafluoropropene (R1234ze(E)) + propane (R290))

Experimental measurement of vapor pressures and (vapor + liquid) equilibrium for {1,1,1,2-tetrafluoroethane (R134a) + propane (R290)} by a recirculation apparatus with view windows

Measurements of isothermal (vapour + liquid) equilibria data for {1,1,2,2-Tetrafluoroethane (R134) + trans-1,3,3,3-tetrafluoropropene (R1234ze(E))} at T = (258.150 to 288.150) K

Phase equilibrium for the binary mixture of {1,1-difluoroethane (R152a)+trans-1,3,3,3-tetrafluoropropene (R1234ze (E))} at various temperatures from 258.150 to 288.150K

Vapor–liquid equilibrium (VLE) data for the binary system of trans-1,3,3,3-tetrafluoropropene (R1234ze(E)) + isobutane (2-methylpropane, R600a) were measured using a recirculation apparatus with view windows at four temperatures [(258.150, 268.150, 278.150, and 288.150) K]. The measured uncertainties of the temperature, pressure, and compositions are ± 5 mK, ± 0.0005 MPa, and ± 0.005, respectively. All of the experimental data were correlated with the Peng–Robinson (PR) EoS using the Huron–Vidal (HV) mixing rule involving the nonrandom two-liquid (NRTL) activity coefficient model. The maximum average absolute relative deviation of pressure is 0.32 %, while the maximum average absolute deviation of vapor phase mole fraction is 0.0029. Azeotropic behavior can be found at the measured temperature range.

Vapor–Liquid Equilibria of the trans-1,3,3,3-Tetrafluoropropene (R1234ze(E)) + Isobutane (R600a) System at Various Temperatures from (258.150 to 288.150) K

Xueqiang Dong

Papers

Experimental measurement of vapor–liquid equilibrium for (trans-1,3,3,3-tetrafluoropropene (R1234ze(E)) + propane (R290))

Experimental measurement of vapor pressures and (vapor + liquid) equilibrium for {1,1,1,2-tetrafluoroethane (R134a) + propane (R290)} by a recirculation apparatus with view windows

Measurements of isothermal (vapour + liquid) equilibria data for {1,1,2,2-Tetrafluoroethane (R134) + trans-1,3,3,3-tetrafluoropropene (R1234ze(E))} at T = (258.150 to 288.150) K

Phase equilibrium for the binary mixture of {1,1-difluoroethane (R152a)+trans-1,3,3,3-tetrafluoropropene (R1234ze (E))} at various temperatures from 258.150 to 288.150K

Vapor–Liquid Equilibria of the trans-1,3,3,3-Tetrafluoropropene (R1234ze(E)) + Isobutane (R600a) System at Various Temperatures from (258.150 to 288.150) K