Catalytic performance of activated carbon supported cobalt catalyst for CO 2 reforming of CH 4

Abstract

Syngas production by CO2 reforming of CH4 in a fixed bed reactor was investigated over a series of activated carbon (AC) supported Co catalysts as a function of Co loading (between 15 and 30wt.%) and calcination temperature (Tc=300, 400 or 500°C). The catalytic performance was assessed through CH4 and CO2 conversions and long-term stability. XRD and SEM were used to characterize the catalysts. It was found that the stability of Co/AC catalysts was strongly dependent on the Co loading and calcination temperature. For the loadings (25wt.% for Tc=300°C), stable activities have been achieved. The loading of excess Co (>wt.% 25) causes negative effects not only on the performance of the catalysts but also on the support surface properties. In addition, the experiment showed that ultrasound can enhance and promote dispersion of the active metal on the carrier, thus improving the catalytic performance of the catalyst. The catalyst activity can be long-term stably maintained, and no obvious deactivation has been observed in the first 2700min. After analyzing the characteristics, a reaction mechanism for CO2 reforming of CH4 over Co/AC catalyst was proposed.

How do Core–Shell Structure Features Impact on the Activity/Stability of the Co‐based Catalyst in Dry Reforming of Methane?

“…[21] Moreover,t he re-oxidationo fm etallic Co in Co/TiO 2 (rutile) during DRM was found to be the main cause for low activity and deactivation. [23] Besides the Co/Al 2 O 3 and Co/TiO 2 catalysts, other Co-based catalysts, including bimetallic ones, [11a, 14, 24] Co(Mg-Al-O) derived from the layered double hydroxides, [25] Co/SBA-15, [26] Co/CeO 2 , [27] Co/Nd 2 O 3 , [28] andC o/C, [29] have been developed for DRM. [23] Besides the Co/Al 2 O 3 and Co/TiO 2 catalysts, other Co-based catalysts, including bimetallic ones, [11a, 14, 24] Co(Mg-Al-O) derived from the layered double hydroxides, [25] Co/SBA-15, [26] Co/CeO 2 , [27] Co/Nd 2 O 3 , [28] andC o/C, [29] have been developed for DRM.…”

Process Modelling, Thermodynamic Analysis and Optimization of Dry Reforming, Partial Oxidation and Auto-Thermal Methane Reforming for Hydrogen and Syngas production

“…Furthermore, the yields of H 2 and CO were observed to increase from 400 to 800°C and thereafter remain constant till 1000°C. This observation could be explained in terms of severe conditions at temperature > 800°C which has been reported from experimental investigations to often lead to catalyst deactivation as a result of carbon deposition on the surface of the catalyst [45,46].…”

Hydrogen‐rich syngas production from chemical looping steam reforming of bio‐oil model compound: Effect of bimetal on LaNi 0.8 M 0.2 O 3 (M = Fe, Co, Cu, and Mn)

“…Its reaction condition is different doping of perovskite, 650°C, mixture sample flow (GHSV = 34 736 g of feed/ (g catalyst h)), and 2.5 hours. The calculation time was deducted at first 0.5 hours because the steam reforming reaction displays in the beginning wave . Therefore, the parameters of reforming, such as gas yield, carbon conversion, selectivity, and H 2 /CO, were calculated based on stable stage.…”