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of adsorption because estimation of the separation performance of an adsorptive process requires several sets of averaging of kinetic properties and the effect of local characteristics are lumped during integration. Based on the above assumptions, the mathematical model for the PSA superstructure is listed in Table 3.1. The equations are written for light product L and heavy product H. Here we consider a lumped mass transfer coefficient for the LDF equation. Since a smaller magnitude of UA makes energy balance a weak function of the ambient temperature, Tw is assumed constant. As a convention, flow in the counter-current bed is considered negative and a minus sign is used for vd. Since the bed model is based on fluxes, the feed throughput and the bed diameter can be adjusted as long as the specified feed flux is achieved and the model assumptions are not violated. The purities and recoveries of light (L) and heavy (H) products are calculated by the following equations. purityL = purityH = recoveryL = recoveryH = Qf eed,i = (1 − β(t))va(t) (3.14a) (3.14b) (3.14c) (3.14d) (3.14e) (1 − β(t))va(t)Ca,L(t) dt 3.3 Model Equations Ca,i(t) dt (1 − α(t))(−vd(t))Cd,H (t) dt i (1 − α(t))(−vd(t)) (1 − β(t))va(t)Ca,L(t) dt i Cd,i(t) dt Q (1 − α(t))(−vd(t))Cd,H (t) dt f eed,L Q φ(t)vfeedCfeed,i dt i ∈ {L, H} Here Qfeed is the feed flux. The total power consumption, given by the following equations, is the sum of the work done by the compressors and the vacuum generator. We note that in the following equations we do not consider the compression work for the light or the heavy f eed,H Chapter 3. PSA Superstructure 43PDF Image | Design and Operation of Pressure Swing Adsorption Processes
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