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Table 5 Oxidative steam reforming of bio-butanol Patel and Patel | 9 Catalyst Co/ZnO (7.17 wt.% Co) CoIr/ZnO (7.20 wt.% Co, 0.30 wt.% Ir) CoRh/ZnO (6.70 wt.% Co, 0.19 wt.% Ru) CoRu/ZnO (6.71 wt.% Co, 0.20 wt.% Ru) CoPd/ZnO (6.63 wt.% Co, 0.26 wt.% Ru) Support ZnO ZnO ZnO ZnO ZnO Ce0.82Zr0.18500 (support calcined at 500 °C) Ce0.82Zr0.18700 (support calcined at 700 °C) Ce0.82Zr0.18900 (support calcined at 900 °C) ZnO TiO2 CeO2-ZrO2 (CeO2 18% by wt.) ZnO ZnO ZnO ZnO on stream data of 100 h. on stream data of 98 h. on stream data of 55 h. on stream data of 65 h. Preparation method Incipient wetness co-impregnation Incipient wetness co-impregnation Incipient wetness co-impregnation Incipient wetness co-impregnation Incipient wetness co-impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Incipient wetness impregnation Temperature Conversion (°C) (%) 500 ~64a 500 ~78a 500 ~85a 500 ~87a 500 ~76a 500 ~84b 500 ~74b 500 ~21b 500 ~82c 500 ~69c 500 ~87c 550 ~98d 550 ~96d 550 ~100d 550 ~98a H2 in gaseous stream (mol %) Reference ~20a [51] ~55a ~65a ~47a ~37a ~70b [52] ~58b ~23b ~56c [53] ~08c ~70c ~58d [54] ~60d ~66d ~65a CoIr/Ce0.82Zr0.18500 (Co and Ir 0.28% by wt.) CoIr/Ce0.82Zr0.18700 (Co and Ir 0.24% by wt.) CoIr/Ce0.82Zr0.18900 (Co 6.66% and Ir 0.27% by wt.) CoIr/ZnO (Co 7.20% and Ir 0.30% by wt.) CoIr/TiO2 (Co 6.80% and Ir 0.37% by wt.) CoIr/18CeZrO2 (Co 6.44% and Ir 0.46% by wt.) Co/ZnO (Co 7.17% by wt.) Ir/ZnO (Ir 0.24% by wt.) Co-0.3Ir/ZnO (Co 7.20% and Ir 0.30% by wt.) Co-1Ir/ZnO (Co 7.29% and Ir 0.86% by wt.) aData were recorded for time bData were recorded for time cData were recorded for time dData were recorded for time 6.46% 6.65% 4.2 Effect of operating conditions The exothermic nature of POX reaction makes it a self-sustained energy option as generated heat during re- action can be used to maintain the desired temperature within the reactor. This can be performed by regulating OBMR in the reactor. However, its limitation is the lower hydrogen yield compared to SR reaction. A well-designed catalyst operating at optimum reaction conditions will re- sult in a higher hydrogen production. In this section, the effects of important factors such as OBMR, temperature and catalyst are discussed. 4.2.1 Oxygen to butanol molar ratio With an increase in OBMR, hydrogen production increases to maximum and then decreases [62–65]. All the stud- ies showed that OBMR around 1.5–2M was found to be optimum for hydrogen production. At lower OBMR (less than 1M), methane was found to be one of the major con- stitutes of gas products and the hydrogen yield was very poor. This indicates that thermal decomposition of butanol in a fuel-rich environment is favorable. At optimum OBMR, methane decreases significantly and concentration of CO and CO2 increases, which clearly indicates dominance of POX and complete oxidation reaction in OBMR range from 1.5M to 2M. At higher OBMR (greater than 2M), formation of water was increased. This indicates that more hydrogen atoms are extracted from butanol and transformed into water [62]. 4.2.2 Effect of temperature The effect of temperature cannot be studied independ- ently, as temperature along with OBMR governs the overall heat of reaction, which ultimately decides the extent of Downloaded from https://academic.oup.com/ce/advance-article-abstract/doi/10.1093/ce/zkx008/4743500 by guest on 15 December 2017PDF Image | Renewable hydrogen production from butanol
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