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10 Appendix 94 in which D and E are fitting parameters, and T is temperature [K]. Therefore, gas thermal conductivity is implemented in the process simulation straightforward according to equation A.2-3 in which kg is thermal conductivity of gaseous mixture [MW/m/K]. kg = (7.79310−11T + 2.45610−9 )yOxygen + (6.91410−11T + 4.11810−9 )yNitrogen (Eq. A.2-3) 10.3 Gas-solid heat transfer coefficient The heat transfer coefficient between gas and solid phases h is calculated as a function of Reynolds and Prandtl numbers according to the algorithm presented in Eq. A.3-1–A.3-4 in which h is gas-solid heat transfer coefficient [MW/m2/K]. Re= 2rpMgvg ; Pr = Cpg (Eq.A.3-1;A.3-2) kgM If Re 190 then j =1.66Re−0.51 else j = 0.983Re−0.41 ; h = jCpgvg g Pr−2/3 (Eq. A.3-3; A.3-4) 10.4 Adsorbed phase heat capacity Adsorbed phase heat capacity is calculated according to empirical equation [75] as shown in Eq. A.4-1 Cpak =f(T) (Eq. A.4-1) in which Cpak is adsorbed phase heat capacity of component k [J/mol/K], and T is temperature [K]. Because the gas temperature in the studied system is always higher than the critical temperature of oxygen and nitrogen, the adsorbed phase heat capacity is calculated in terms of ideal gases [76]. The adsorbed phase heat capacity of oxygen and nitrogen is calculated according to the empirical equation A.4-2 presented in Tab. A.4-1 along with regression coefficients and temperature range of application. Tab. A.4-1 Heat capacity of pure gases [75] Oxygen 29.526 -8.8999 3.8083 -32.629 88.607 50 – 1500 The parameter Cpak is determined in the temperature range of -50 °C – 100 °C in order to increase the precision of estimation. For that reason, Cpak is calculated from an approximation function as shown in Eq. A.4-3 Cpak =FT2 +GT+H C =A+BT+CT2+DT3+ET4 J pa mol K (Eq. A.4-2) Temperature [K] A B×103 C×105 D×109 E×1013 Nitrogen 29.342 -3.5395 1.0076 -4.3116 2.5935 50 – 1500 (Eq. A.4-3)PDF Image | Modelling and Simulation of Twin-Bed Pressure Swing Adsorption Plants
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