| Shell core Ni-Mg/Al | Co-precipitation, then wet impregnation and finally calcination at 700˚C for 6 h | 700˚C | Shell core catalyst exhibited better hydrogen yield for per mol of Ni atoms than the conventional Ni-Mg-Al-Htlc catalyst | Considerable deposition of both encapsulating and filaments C species on the catalyst surface | 75 | [146] |
| Ni–Fe-Htlc | Co-precipitation and then calcination in static air at 500 and 800˚C for 3 h | 500˚C | Calcination temperature was found to affect catalytic performance and Fe presence in the Ni-Htlc catalyst found to increase catalytic activity and H2 selectivity | High calcination temperature (800˚C) of the catalyst caused higher carbon deposition and Ni˚ sintering during ethanol steam reforming | 60 | [147] |
| Ni-Fe Htlc | Co-precipitation and then calcination at 500˚C for 6 h in static air | 400˚C - 600˚C | Iron in Ni-based Htlc catalyst enhances activity and h2 selectivity by promoting ni dispersion and lowering Ni˚ crystal size | Excess iron in the catalyst decreases activity | 60 | [148] |
| Cu impregnated Mg-Al(Htlc) | Wet impregnation, grinding and thermal treatment at 275˚C for 24 h | 200˚C - 600˚C | Improved H2production and good stability during sorption enhanced ethanol steam reforming | High CO content of around 5000 ppm due to poor catalytic activity for WGS reaction during pre-breakthrough periods | 90 | [149] |
| Co-Mg/Al Htlc | Co-precipitation followed by calcination at 550˚C for 3 h | 250˚C - 550˚C & atmospheric pressure | Improved activity and selectivity towards H2 at moderate temperature and good stability even under higher ethanol loadings | The catalyst showed slow deactivation over time | 65 | [143] |
| Htlc based Co-Mg/Al Rh-Mg/Al &RhCo-Mg/Al | Co-precipitation and then wet impregnation for support (Rh & Co) and finally calcination at 800˚C for 2 h | 500˚C & atmospheric pressure | Mg-Al Htlc based catalyst supported with both Rh and Co showed high H2yield from EtOH and low ethane selectivity | Mg containing catalysts generated higher amounts of CH4 and CO as compared to magnesium-free catalysts | 40 | [150] |
| Htlc derived Co-Zn/Al, Co-Mg/Al, Co-Al, Ni-Mg/Al &Cu-Mg/Al | Urea hydrolysis followed by calcination at 450˚C for 7 h | 575˚C - 675˚C | Presence of Zn increased the reducibility of Co in the catalyst. Thus, at 575˚C CoZnA was the best catalyst for H2 production | CuMgAl exhibited low catalytic activity and selectivity to H2 | 63.7 | [151] |
| Htlc derived Ni/Zn-Mg-Al | Co-precipitation and calcination | 700˚C & atmospheric pressure | Catalyst containing Mg/Zn ratio of 4 exhibited improved performance and impressive H2 yield of 5.15 mol per mol Et-OH at 700˚C | Comparatively high coke formation during EtOH steam reforming | 5.15 mol/mol Et-OH | [152] |
| Htlc derived Ni-Co-Zn-Al | Urea hydrolysis followed by calcination at 700˚C for 5 h | 497˚C - 597˚C | At temperatures between 447 and 597˚C presence of Co increased the selectivity of the catalyst to H2 and CO2 and decreased selectivity to CH4 | Catalytic performance decreased at temperatures higher than 550˚C | 90 | [153] |
| La&Ce promoted hydrotalcite (Ni-Mg/Al) | Co-precipitation followed by La and Ce addition by anion exchange and finally calcination in air at 500˚C for 15 h | 550˚C & 650˚C and atmospheric pressure | Incorporation of both Ce and La in the catalyst (Ni/Mg/Al) improved H2 yield and at 650˚C catalysts achieved near 100% ethanol conversion | Ethanol conversion decreased at low temperature | 75 | [154] |