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present work is 0.7/0.3 (CH4/CO2) by mole. The inlet and outlet pressures for the working fluid gases and the coupling liquid are assumed constant at 5500 and 5400 kPa, respectively. Thus, mass flow rates and velocities of the fluids adjust to match the fixed pressure drop imposed between the microchannel inlet and outlet, based on the chosen microchannel diameter and length. The selection of these pressure extremes is based on typical pressure values used for transportation of natural gas via pipelines (Schaal, 2013). Table 2.1 shows the numerical values of parameters chosen for the model simulation. The microchannel diameter, adsorbent layer thickness, adsorbent material and the HTF material are chosen to ensure a feasible and realistic process performance; their selection is discussed in detail in later sections. 2.2.1 Adsorption stage model For the adsorption stage modeling, an approach similar to that used by Pahinkar et al. (2015) is used. This approach involves radial lumping of the adsorbent microchannel fluid, adsorbent layer, and monolith wall regions. A 2-D axisymmetric model was also developed and its results are compared with those with the present approach in Appendix A. The heat loss from the microchannel monolith wall to the surroundings is neglected because several microchannels stacked together interact with each other thermally and all are considered to demonstrate a similar thermal state at any instant of the process. 23PDF Image | TEMPERATURE SWING ADSORPTION PROCESSES FOR GAS SEPARATION
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