Adsorption of Off‐Gases from Steam Methane Reforming (H₂, CO₂, CH₄, CO and N₂) on Activated Carbon

Pressure swing adsorption for CO2 capture in Fischer-Tropsch fuels production from biomass

“…The adsorption equilibrium and kinetics for all the compounds in the feed stream in this activated carbon have been determined by Grande et al (2008). The Virial isotherm was used to fit the experimental adsorption data .…”

Response Surface Methodology and Aspen Plus Integration for the Simulation of the Catalytic Steam Reforming of Ethanol

“…The net energy produced in the system was obtained according to Equation (18), where ΔHNET is the net available energy of the system, ΔHFC is the change in enthalpies in the FC, ΔHHE4 is the change in enthalpies in the heating of the stream entering the FC, ΔHPROX is the change in enthalpies during the PROX, ΔHHE2 is the change in enthalpies in the heating of the stream entering the PROX, ΔHCDS is the change in enthalpies in the condenser, ΔHSRE is the change in enthalpies during the SRE, ΔHHE1 is the change in enthalpies during the initial heat exchange, and ΔHHE3 is the change in The net energy produced in the system was obtained according to Equation (18), where ∆H NET is the net available energy of the system, ∆H FC is the change in enthalpies in the FC, ∆H HE4 is the change in enthalpies in the heating of the stream entering the FC, ∆H PROX is the change in enthalpies during the PROX, ∆H HE2 is the change in enthalpies in the heating of the stream entering the PROX, ∆H CDS is the change in enthalpies in the condenser, ∆H SRE is the change in enthalpies during the SRE, ∆H HE1 is the change in enthalpies during the initial heat exchange, and ∆H HE3 is the change in enthalpies in the cooling of the stream entering the ADS. CH 4 and CO 2 separator (ADS) was not taken into account in the energy analysis because it was considered as an non-reactant, isothermal, and adiabatic process ∆H = 0, which operates at 70 • C and 1 bar [66]. However, the precooling (HE3) to ensure the operating temperature in ADS was included.…”

“…Then, a total separator (ADS) with precooling (HE3) was used to completely remove CH 4 and CO 2 assuming isothermal and adiabatic adsorption, due to their low concentration in the stream. ADS simulates an adsorber filled with activated carbon that operates at 70 • C, 1 bar, and 100% efficiency [66]. Finally, the FC was modeled as a reactor (FC) operating at 150 • C [67], with a preheating (HE4) to ensure this condition, and 80% H 2 conversion and 40% electrical efficiency were assumed in FC [68].…”

“…Figure 2 shows the flowsheet of the simulation used. The process can be divided into three general stages: (i) H 2 production by SRE with preheating (HE1) to ensure the reaction temperature; (ii) H 2 purification by water condensation (CDS), CO elimination by carbon monoxide preferential oxidation (PROX) with preheating (HE2) to ensure the reaction temperature (150 • C [65]), and CH 4 and CO 2 adsorption (ADS) with activated carbon and precooling (HE3) to ensure the adsorption temperature (70 • C [66]); and (iii) energy generation in FC with preheating (HE4) to ensure the reaction temperature (150 • C [67]). The energy divisor (ED) indicates that the FC produces both electrical (40%) and heat (60%) energy [68].…”

“…CO2 and CH4 adsorption (ADS) with activated carbon was selected among other methods like adsorption with oxides [69,70], because the first ensures simultaneously removal of CO2 and CH4 in post-reforming streams, requires less power consumption, and minimizes H2 losses [66]. ADS was considered as an isothermal and adiabatic process due to the low contents of the adsorbates in the streams, operating at 70 °C, 1 bar, and 100% efficiency, as reported by [66]. (Figure 3b) during SRE over Rh-Pt/CeO2.…”