TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION

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TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION ( temperature-swing-adsorption-processes-for-gas-separation )

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Table C.2 Calculation of heat and mass transfer coefficients Input Equations Output This table shows calculation of heat and mass transfer coefficients and corresponding resistances in the microchannel for the initial and final states as shown in the schematic (Figure C.2). Hydraulic radius, Rh = 235×10-6 [m] Binary diffusion coefficient, DAB = 3.05 × 10-7 [m2 s-1] Mixture diffusion coefficient Mass transfer coefficient for gas phase Reynolds numbers: Re = 2898 (before liquid displaces gas) Re = 1105 (after liquid   2 5  2200Re     365  10 2Rh 10 e  1   hmSh0 2   DAB  Sh0 Sh0.079RefScG  0 4556   1Sc  Mass transfer coefficient for liquid phase 2Rh 10  365  hm,L 10e 1   2 5    2200Re  Heat   Sh  02  DAB,water   Sh0 Sh 0.079Re fScL    transfer coefficient for all scenarios  2200Re   10 365   0 4556   1Sc    2 5    2Rh 10e 1   h T  Nu      k  0 g  Nu2 0.079RefPr  0Nu0 g 56   1Pr45   in water, DAB,water = 2.23 × 10- 9 [m2 s-1] Laminar Sherwood number, Sh0 = 4.01 Gas Schmidt number, Sc = 0.72 (before liquid displaces gas) Liquid Schmidt number, ScL = 500 (after liquid displaces gas) Interface velocity, u = 1.83 [m s-1] ρG = 50.44 [kg m-3] displaces gas) Convection mass transfer coefficient for gas in channel, hm,G = 0.006 [m s-1] (before liquid displaces gas) Convection mass transfer coefficient for liquid in channel, hm,L = 0.002 [m s-1] (after liquid displaces gas) Convection heat transfer coefficient for gas in channel, hT,G = 800 [W m-2 K-1] (before liquid displaces gas) ρL = 951.68 [kg m-3] μG = 1.5 × 10-5 [kg m-3 s-1] μL = 7.37 × 10-4 [kg m-3 s-1] Liquid and gas velocity are the same for displacement phase. (Churchill, 1977a; Churchill, 1977b) Single phase Reynolds number and friction factor Re  2uRh   1    0 . 9   1 6    1 . 5    1 2  12 16 7  f 8 8  37530 2.457lnRe       Re  Re   0.27eps      2R     h  Convection heat transfer coefficient for liquid in channel, hT,L = 5767 [W m-2 K-1] (after liquid displaces gas) f = 0.047 (before liquid displaces gas) f = 0.057 (after liquid displaces gas) 182

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