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7.4 PSA Case Study - Post Combustion CO2 Capture Table 7.2: Zeolite 13X properties and model parameters [111] Parameter Bed Length (L) Bulk porosity (εb) Adsorbent density (ρs) Mass transfer coefficient (k) Value 1 m 0.34 1870 kg m−3 CO2=0.1631 sec−1 N2=0.2044 sec−1 310 K Process temperature (T) Isotherm parameters CO2 qs1 2.708769 qs2 2.436388 b1 1.23×10−5 b2 4.78×10−4 N2 1.819949 1.819949 6.17×10−7 6.17×10−7 Table 7.3: Boundary conditions for each operating step pressurization yj|x=0 = yf,j P = Ph u|x=L = 0 adsorption yj|x=0 = yf,j P = Ph u|x=0 = ua depressurization — P = Pl u|x=L = 0 desorption yj|x=L = yj|x=L of other bed P = Pl u|x=L = 0.4u|x=L of other bed along the bed length, we solve component mass balance for only one component. Moreover, we don’t have to ensure that the mole fractions sum up to one as it implicitly happens because of the overall mass balance. We denote this model in Table 7.1 as the rigorous model for which we develop a reduced-order model. Boundary conditions for each step are shown in Table 7.3. We note that for the depressur- ization step a boundary condition for mole fraction is not needed since u|x=L = 0 automatically sets the inlet flux to be zero for the component mass balance. However, boundary conditions are needed for both velocity and mole fraction for the pressurization step due to the nature of the upwind-based spatial discretization scheme. Also, we note that the purge fraction of the outlet from x = L which goes from one bed to the other during the adsorption step is chosen to be 0.4, which appears in the boundary condition of velocity for the desorption step. Chapter 7. Trust-region Framework for ROM-based Optimization 148PDF Image | Design and Operation of Pressure Swing Adsorption Processes
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