Design and Operation of Pressure Swing Adsorption Processes

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Design and Operation of Pressure Swing Adsorption Processes ( design-and-operation-pressure-swing-adsorption-processes )

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Table 6.1: Physical properties and basic simulation parameters parameter Bed Length (L) Bed porosity (εb) Bed radius (Rb) Particle radius (Rp) Particle porosity (εp) Diffusivity (Dx) Particle density (ρp) Bed density (ρb) Thermal diffusivity (KL) Heat capacity of solid (Cps) Heat transfer coefficient (h) Lumped mass transfer coefficient (k) Heat of adsorption (∆H) Gas viscosity (μ) R Ambient temperature (Tw) Feed temperature (Tfeed) Feed composition Feed pressure (Pfeed) Purge pressure (Ppurge) Pressurization time (tp) Adsorption time (ta) value 1 m 0.404 0.25 m 5.41 × 10−3 m 0.546 1.3 × 10−5 m2/sec 716.3 kg/m3 426.7 kg/m3 1.2 × 10−6 J/m/sec/K 1046.7 J/kg/K 60 J/m2/sec/K (0.136,0.259)(CH4,H2) 1/s (24124,8420)(CH4,H2) J/mole 3.73 × 10−8 kg/m/sec 8.314 J/mol/K 300 K 310 K (0.7,0.3)(CH4,H2) 600 kPa 150 kPa 5 s 50 s 6.5 Case Study - Hydrogen PSA 3. The gas and the solid phases are in thermal equilibrium and bulk density of the solid phase remains constant. 4. Pressure drop along the bed is calculated by the Ergun equation. 5. The adsorption behaviors are described by the single-site Langmuir isotherm. 6. The adsorption rate is approximated by the linear driving force (LDF) expression. 7. A linear profile is assumed for superficial gas velocity for all the steps. Cruz et al. [58] suggested that this kind of an assumption is valid for bench-scale PSA processes and an overall mass balance is not required. Based on the above assumptions, the mathematical model for the PSA process is listed in Table 6.2. Here we use a lumped mass transfer coefficient for the LDF model. The temperature Chapter 6. Reduced-order Modeling for Optimization 113

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