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Productivity mol kg−1 h−1 Case 1 1.65 Case 1, no steam adsorption 1.66 Carbon capture ratio mol mol−1 0.967 0.986 CO2 purity mol mol−1 0.996 0.933 Table 5: Cycle performance for Case 1 (700 s, S/Crinse = 0.06, S/Cpurge = 0.1) 11 0.8 0.6 0.4 0.2 0 2 4 6 8 10 12 z [m] 0.8 0.6 0.4 0.2 0 2 4 6 8 10 12 z [m] ← countercurrent ← 389 s 466 s 544 s ← countercurrent ← 389 s 466 s 544 s (a) Complete isotherm Figure 8: CO2 loading qCO2 during purge with and without steam adsorption, Case 1 402 ure 8, leading to the cases with and without H2O adsorption to start the adsorption 403 step with an average amount of CO2 adsorbed of 0.25 mol kg−1and 0.23 mol kg−1, 404 respectively. These results clearly confirm the benefits of an adsorptive rinse. 405 For SEWGS, analogously, recompressed CO2 product could be employed as 406 rinse gas as an alternative for a H2O rinse, given the fact that CO2 also adsorbs. 407 Such a CO2 rinse was proposed by Allam et al. (2005). High pressure CO2 is 408 available from the compression section in a CCS plant. A more thorough evaluation 409 of the potential of the CO2 rinse cycle is currently being performed. 410 3.1.4. Implications of the linear driving force mass transfer coefficient 411 The present study uses the linear driving force model for simulating the in- 412 traparticle mass transfer resistances. The model has been derived and validated 413 previously (Boon et al., 2014), both for adsorption as well as desorption, based on 414 breakthrough and regeneration measurements, respectively. Nevertheless, the re- 415 sults of the current cycle simulations present such a marked decrease in the steam 416 requirement compared to literature studies, partly due to the new linear driving 417 force coefficient, that a further discussion is justified. 418 The linear driving force model and mass transfer coefficient (Table 2) have val- 419 ues in the range of 0.02–0.3 s−1, varying mainly with the slope of the adsorption 420 isotherm (∂qi/∂ci). The value of kLDF at the end of adsorption, rinse, depressurisa- 20 (b) No steam adsorption qCO2 [mol/kg] qCO2 [mol/kg]PDF Image | High-temperature pressure swing adsorption cycle design for sorption
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