Vapor–liquid equilibria for pentafluoroethane + propane and difluoromethane + propane systems over a temperature range from 253.15 to 323.15 K

Isothermal VLE Measurements for Difluoromethane + Dimethyl Ether and an Evaluation of Hydrogen Bonding

“…The RKS−HV−NRTL model well describes data from Coquelet et al, with the AAD being within 0.0030 in terms of the vapor-phase composition and 0.3% in terms of the saturated pressure. The deviations in the data from Kim et al are a little bit higher, with absolute average deviations of 0.0060 in terms of the vapor molar fraction and 0.57 in terms of the saturated pressure percentage deviation, with maximum deviations of 0.02 in terms of the vapor composition and 3% in terms of the saturated pressure. The data from Lee et al are well represented by the RKS−HV−NRTL model in terms of saturated pressure, with AAD = 0.44%, but show higher deviations in terms of the vapor-phase composition, with AAD = 0.0133.…”

“…VLE data for the R32 + RE170 system have not been published in the literature. On the contrary, several VLE data can be found in the literature for the R32 + R290 system. ,− …”

The study of binary interaction parameters on VLE for alternative refrigerant mixtures

“…The SRK, PR, and CSD equations of states with van der Waals mixing rules could reasonably calculate the VLE properties of the HCs + HFCs and DME + HFCs. The values of the optimum interaction parameter k ij HFC23 + HC170 48 [6] 0.195 2.151 0.0142 0.199 0.891 0.0132 0.179 1.875 0.0098 HFC23 + HC290 27 [7] 0.195 1.456 0.0055 0.199 2.389 0.0066 0.179 3.058 0.0090 HFC23 + HC600 28 [7] 0.195 3.333 0.0030 0.199 3.567 0.0051 0.179 4.533 0.0029 HFC23 + HC600a 23 [8] 0.195 3.176 0.0085 0.199 2.784 0.0075 0.179 3.438 0.0089 HFC32 + HC290 63 [9] 0.188 0.707 0.0026 0.195 0.858 0.0036 0.157 1.948 0.0117 HFC32 + HC600 32 [10] 0.188 5.201 0.0134 0.195 5.681 0.0124 0.157 6.231 0.0163 HFC32 + HC600a 26 [11] 0.188 2.806 0.0100 0.195 2.699 0.0097 0.157 3.130 0.0098 HFC125 + HC290 89 [9] 0.156 1.450 0.0074 0.158 1.184 0.0044 0.144 0.855 0.0044 HFC125 + HC600 29 [12,13] 0.156 0.900 0.0030 0.158 1.158 0.0033 0.144 0.946 0.0064 HFC125 + HC600a 23 [14] 0.156 2.182 0.0079 0.158 2.245 0.0062 0.144 1.294 0.0058 HFC134a + HC290 37 [15] 0.168 0.789 0.0048 0.171 0.660 0.0056 0.157 0.835 0.0053 HFC134a + HC600 41 [16] 0.168 0.850 0.0059 0.171 1.046 0.0044 0.157 2.145 0.0100 HFC134a + HC600a 24 [17] 0.168 2.240 0.0093 0.171 2.223 0.0077 0.157 3.236 0.0107 HFC143a + HC290 22 [15] 0.113 1.693 0.0035 0.117 1.314 0.0043 0.101 2.803 0.0070 HFC143a + HC600 47 [18] 0.113 1.502 0.0044 0.117 1.077 0.0056 0.101 1.941 0.0098 HFC143a + HC600a 16 [8] 0.113 2.250 0.0136 0.117 1.994 0.0133 0.101 3.198 0.0153 HFC152a + HC290 25 [19] 0.127 4.149 0.0011 0.132 4.802 0.0184 0.108 1.927 0.0082 HFC152a + HC600 34 [20] 0.127 0.695 0.0051 0.132 1.395 0.0055 0.108 0.976 0.0072 HFC152a + HC600a 32 [11] 0.127 1.706 0.0071 0.132 2.232 0.0072 0.108 1.803 0.0107 HFC227ea + HC290 58 [21] 0.135 1.137 0.0044 0.136 0.953 0.0028 0.122 1.049 0.0083 HFC227ea + HC600 45 [22] 0.135 1.065 0.0038 0.136 1.274 0.0060 0.122 1.093 0.0080 HFC227ea + HC600a 37 [14] 0.135 0.597 0.0055 0.136 0.547 0.0042 0.122 0.298 0.0055 HFC236ea + HC290 37 [23] 0.141 1.663 0.0050 0.143 1.802 0.0071 0.128 1.760 0.0061 HFC236fa + HC290 37 [24] 0.141 1.413 0.0052 0.143 1.492 0.0078 0.128 1.208 0.0055 HFC236fa + HC600a 13 [17] 0.141 1.734 0.0028 0.143 1.873 0.0052 0.128...…”

“…[3,4] However, the blended refrigerants are preferable to pure working fluids on account of energy saving and the flexibility of operation. [5] Because the vapor-liquid equilibrium (VLE) properties are important in the optimization of thermodynamic cycles, the literature on VLE experimental measurement data for new alternative refrigerant mixtures (HCs + HFCs [6][7][8][9][10][11][12][13][14][15][16][17][18][19][20][21][22][23][24] and DME + HFCs binaries [23,[25][26][27][28][29] ) have increased considerably in the recent years. Due to the time-consuming nature of experimental measurement, the predictive models are valuable tools for estimating the VLE properties.…”

Cooling performance of several CO2/propane mixtures and glide matching with secondary heat transfer fluid

“…Performance comparison among several CO 2 /propane mixtures Propane is the refrigerant having a higher refrigerating effect and a much lower vapor density than CO 2 (Kim and Kim, 2005). Thus, one can easily expect that adding propane to CO 2 improves system efficiency and reduces the cooling capacity.…”