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 – continued Effective diffusion coefficient, Deff = 8.39 × 10-8 [m2 s-1] Channel perimeter, Peri = 1477×10-6 [m] Gas mass transfer coefficient, hm,G = 0.006 [m s-1] (before liquid displaces gas) Liquid mass transfer coefficient, hm,L = 0.002 [m s-1] (after liquid displaces gas) Channel hydraulic radius, Rh = 235×10-6 [m] R0 = 250×10-6 [m] For gas occupied node yg,CH4 = 0.45 yg,CO2 = 0.55 For liquid occupied node (yg,CH4 = 0.02 yg,CO2 = 0.024, iteratively solved species equation, described later) Mass transfer resistance during gas flows lnR0  1 R Req,Mass,G    h  hmPeri 2Deff1yg,i Total mass transfer resistance in liquid filled region during bubbly flow (Pressure driven) Total mass transfer resistance in liquid filled region during diffusive flow (diffusion driven) Req,Mass,L  D h  2 eff1yg,i lnR0  R lnR0  1 R Req,Mass,L h Peri D h  m,L 2 eff1yg,i Total mass transfer resistance in liquid filled region during cooling (diffusion driven, after water enters the adsorbent layer) 1 R Req,Mass,L  D h hm,LPeri 2 eff,L1yg,i lnR0  Mass transfer resistance during gas flows Req,Mass,G,CH4 = 69696 [m-2 s] Req,Mass,G,CO2 = 84558 [m-2 s] (Not used after liquid occupies the node at 0.5 m) Pressure driven: Req,Mass,L,CH4 = 64773 [m-2 s] Req,Mass,L,CO2 = 52496 [m-2 s] Diffusion driven: Req,Mass,L,CH4 = 3.276×107 [m-2 s] Req,Mass,L,CO2 = 3.275×107 [m-2 s] Liquid filled diffusion driven: Req,Mass,L,CH4 = 3.514×107 [m-2 s] Req,Mass,L,CO2 = 3.467×107 [m-2 s] Total heat transfer resistance lnR0  1 R Req,Heat    h  hT Peri 2kw Req,Heat,G = 0.88 [W-1 m K] (Before liquid displaces gas) Req,Heat,G = 0.15 [W-1 m K] (After liquid displaces gas) 183

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