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Here we also consider temperature dependence of heat capacities and heat transfer through the wall of the column. As in the case of material balance, here T represents average temperature across cross-section. The effective heat transfer coefficient UA comprises contributions from both fluid-to-wall as well as fluid-to-particle heat transfer coefficients. Fluid-to-particle heat transfer coefficient can be obtained from Carberry equation and it depends on system’s Nusselt number, Prandtl number, and Reynolds number [181]. Fluid-to-wall heat transfer coefficient is usually obtained from empirical correlations. If only fluid-to-wall heat transfer is assumed, UA reduces to UA = 4hw (2.16) D where D is the column diameter and hw fluid-to-wall heat transfer coefficient. 2.3.5 Momentum Balance As the bulk fluid flows through the void spaces between adsorbent particles, it experiences a pressure drop due to viscous energy losses and drop in kinetic energy. Ergun equation is commonly used to describe such a pressure drop along the bed length ∂P 150μ(1−ε)2 b d 2p ε 3b 1.751−ε − = ∂ x v + d p ε 3b b Mwi Ci i v|v| (2.17) 2.3 PSA Modeling The first term on the right-hand side represents losses due to viscous flow (laminar part), while the second term accounts for the drop in kinetic energy (turbulent part). Often pressure drop across the bed is assumed negligible and is not considered in the analysis of the dynamic behavior of a PSA process [48, 47, 144]. Cruz et al. [58] suggest that such an assumption is valid for bench-scale PSA processes. They suggest that an overall material balance to obtain velocity profile along the bed length can be avoided and a constant or linear velocity profile is acceptable for PSA processes with low Reynolds number. Chapter 2. Pressure Swing Adsorption 21PDF Image | Design and Operation of Pressure Swing Adsorption Processes
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