Testing of a Ni‐Al 2 O 3 Catalyst for Methane Steam Reforming Using Different Reaction Systems
Abstract Ni‐Al 2 O 3 catalyst activity was tested for methane steam reforming using two different reaction systems: a catalyst particle bed (0.42–0.5 mm catalyst particles diluted in SiC) with a surface area‐to‐volume ratio SA/V of 910 m –1 and a porosity ϵ of 52 % and a catalyst‐coated metal monoli...
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| Published in | Chemical engineering & technology Vol. 35; no. 4; pp. 720 - 728 |
|---|---|
| Main Authors | , , |
| Format | Journal Article |
| Language | English |
| Published |
01.04.2012
|
| Online Access | Get full text |
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| Abstract | Abstract
Ni‐Al
2
O
3
catalyst activity was tested for methane steam reforming using two different reaction systems: a catalyst particle bed (0.42–0.5 mm catalyst particles diluted in SiC) with a surface area‐to‐volume ratio SA/V of 910 m
–1
and a porosity ϵ of 52 % and a catalyst‐coated metal monolith with an SA/V of 3300 m
–1
and an ϵ of 86 %. Under a steam‐to‐carbon ratio of 2.5 and at a temperature of 700 °C, the highest specific reaction rates were found for the catalyst‐coated monolith. The high SA/V and ϵ, together with the high rate of heat transfer of the metal monolith were found to be responsible of this optimum behavior. However, in both systems, the Ni‐Al
2
O
3
catalyst suffered a catalyst deactivation during operation. |
|---|---|
| AbstractList | Abstract
Ni‐Al
2
O
3
catalyst activity was tested for methane steam reforming using two different reaction systems: a catalyst particle bed (0.42–0.5 mm catalyst particles diluted in SiC) with a surface area‐to‐volume ratio SA/V of 910 m
–1
and a porosity ϵ of 52 % and a catalyst‐coated metal monolith with an SA/V of 3300 m
–1
and an ϵ of 86 %. Under a steam‐to‐carbon ratio of 2.5 and at a temperature of 700 °C, the highest specific reaction rates were found for the catalyst‐coated monolith. The high SA/V and ϵ, together with the high rate of heat transfer of the metal monolith were found to be responsible of this optimum behavior. However, in both systems, the Ni‐Al
2
O
3
catalyst suffered a catalyst deactivation during operation. |
| Author | Manzanedo, J. de Miguel, N. Arias, P. L. |
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| CitedBy_id | crossref_primary_10_1155_2014_451919 crossref_primary_10_1002_ceat_201300006 crossref_primary_10_1021_acs_energyfuels_6b03423 crossref_primary_10_1002_ceat_201200555 crossref_primary_10_1002_ceat_201200632 crossref_primary_10_1002_ceat_201200643 crossref_primary_10_1088_1361_6528_ab27ce crossref_primary_10_1002_ceat_201400124 crossref_primary_10_1016_j_mcat_2023_113718 crossref_primary_10_1002_ceat_201200259 crossref_primary_10_1016_j_jics_2022_100430 crossref_primary_10_1002_ceat_201200170 crossref_primary_10_1016_j_ijhydene_2018_06_059 crossref_primary_10_1002_ceat_201200540 crossref_primary_10_1016_j_rser_2015_12_072 crossref_primary_10_1016_j_ijhydene_2015_12_116 crossref_primary_10_1016_j_ijhydene_2016_10_003 crossref_primary_10_1002_ceat_201300398 |
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Ni‐Al
2
O
3
catalyst activity was tested for methane steam reforming using two different reaction systems: a catalyst particle bed (0.42–0.5 mm... |
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