TY - JOUR
T1 - A saturated liquid density equation in conjunction with the Predictive- Soave-Redlich-Kwong equation of state for pure refrigerants and LNG multicomponent systems
AU - Nasrifar, Khashayar
AU - Moshfeghian, Mahmood
PY - 1998/12
Y1 - 1998/12
N2 - An equation and a set of mixing rules for the prediction of liquid density of pure refrigerants and liquified natural gas (LNG) multicomponent systems have been developed. This equation uses the parameters of Mathias and Copeman [P.M. Mathias, T.W. Copeman, Fluid Phase Equilib. 13 (1983) 91-108] temperature dependent-term for the Predictive-Soave-Redlich-Kwong [T. Holderbaum, J. Gmehling, Fluid Phase Equilib. 70 (1991) 251-265] equation of state and hence it could be used together with this equation. The equation uses a characteristic parameter for each refrigerant; however, if it is not available, a value of zero is recommended. This model gives an average of absolute errors less than 0.42% for the prediction of liquid density of 28 pure refrigerants consisting of 2489 data points and 0.33% for 18 multicomponent LNG systems involving 132 data points. The model parameters were determined from pure component properties and reported. These parameters were then used without any adjustment to predict liquid density of multicomponent LNG mixtures and excellent results were obtained. The model was also compared with other available methods.
AB - An equation and a set of mixing rules for the prediction of liquid density of pure refrigerants and liquified natural gas (LNG) multicomponent systems have been developed. This equation uses the parameters of Mathias and Copeman [P.M. Mathias, T.W. Copeman, Fluid Phase Equilib. 13 (1983) 91-108] temperature dependent-term for the Predictive-Soave-Redlich-Kwong [T. Holderbaum, J. Gmehling, Fluid Phase Equilib. 70 (1991) 251-265] equation of state and hence it could be used together with this equation. The equation uses a characteristic parameter for each refrigerant; however, if it is not available, a value of zero is recommended. This model gives an average of absolute errors less than 0.42% for the prediction of liquid density of 28 pure refrigerants consisting of 2489 data points and 0.33% for 18 multicomponent LNG systems involving 132 data points. The model parameters were determined from pure component properties and reported. These parameters were then used without any adjustment to predict liquid density of multicomponent LNG mixtures and excellent results were obtained. The model was also compared with other available methods.
KW - Equation of state
KW - Liquid density equation
KW - LNG
KW - Refrigerant
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U2 - 10.1016/S0378-3812(98)00422-1
DO - 10.1016/S0378-3812(98)00422-1
M3 - Article
AN - SCOPUS:0032323617
SN - 0378-3812
VL - 153
SP - 231
EP - 242
JO - Fluid Phase Equilibria
JF - Fluid Phase Equilibria
IS - 2
ER -