The composition (CuO/ZnO/Al2O3 = 30/60/10) of a commercial catalyst G66B was used as a reference for designing CuO/ZnO/CeO2/ZrO2/Al2O3 catalysts for the steam reforming of methanol (SRM). The effects of ZnO, CeO2, ZrO2 and Al2O3 on the SRM reaction were clearly identified. CeO2, ZrO2 and Al2O3 all improved the dispersions of CuO and ZnO in CuO/ZnO/CeO2/ZrO2/Al2O3 catalysts. Zirconium oxide promoted the SRM reaction and slightly reduced the concentration of CO, but CeO2 and Al2O3 weakened the SRM reaction. The introduction of ZrO2 into CuO/ZnO/Al2O3 (30/60/10) improved the reducibility and stability of the catalyst. The addition of CeO2 or Al2O3 hindered the reducibility of the catalyst and weakened the interaction between CuO and ZnO. Nevertheless, an appropriate amount of Al2O3 was needed for the stability and the mechanical strength of the catalysts. The CuO/ZnO/ZrO2/Al2O3 (30/40/20/10) and CuO/ZnO/ZrO2/Al2O3 (40/30/20/10) catalysts are good candidates for the SRM, as determined by comparison with the commercial catalyst G66B.
Article Outline
1. Introduction
2. Experimental
2.1. Preparation of catalysts
2.2. Characterization of catalysts
2.3. Steam reforming of methanol
3. Results and discussion
3.1. Effect of CeO2/ZrO2 ratio
3.2. Effect of ZnO/ZrO2 ratio
3.3. Effect of ZnO/Al2O3
3.4. Effect of CuO/ZnO
4. Conclusion
Acknowledgements
References Purchase
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Graphical abstract
During the design of CuO/ZnO/CeO2/ZrO2/Al2O3 catalysts for steam reforming of methanol (SRM), the effects of CeO2, ZrO2 and Al2O3 were clearly identified. ZrO2 promoted the SRM reaction, but CeO2 and Al2O3 weakened it. An appropriate amount of Al2O3 was still needed for the mechanical strength of catalysts. The CuO/ZnO/ZrO2/Al2O3 (30/40/20/10 and 40/30/20/10) catalysts are good candidates for SRM as compared with G66B (CuO/ZnO/Al2O3 = 30/60/10).
388
Microstructural characterization of Cu/ZnO/Al2O3 catalysts for methanol steam reforming—A comparative study Original Research Article
Applied Catalysis A: General, Volume 348, Issue 2, 15 October 2008, Pages 153-164
Patrick Kurr, Igor Kasatkin, Frank Girgsdies, Annette Trunschke, Robert Schl?gl, Thorsten Ressler
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Graphical abstract
The microstructure of Cu/ZnO/Al2O3 catalysts for methanol steam reforming was investigated and compared to structure–activity correlations of binary Cu/ZnO model catalysts. Similar to the binary system, characteristic defects (e.g. lattice strain) in the Cu phase of Cu/ZnO/Al2O3 catalysts are indicative of a homogeneous microstructure and superior catalytic performance.
389
Thermodynamic study of the supercritical water reforming of glycerol Original Research Article
International Journal of Hydrogen Energy, In Press, Corrected Proof, Available online 18 May 2011
F.J. Gutiérrez Ortiz, P. Ollero, A. Serrera, A. Sanz
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Highlights
? Hydrogen can be produced by supercritical water (SCW) reforming. ? One of the foreseeable features is that the catalyst will not be strictly necessary. ? A systematic thermodynamic analysis of glycerol reforming using SCW has been carried out. ? A sensitivity analysis has been conducted on SCW reforming of pure and pretreated crude glycerol. ? The thermodynamic favorable operating conditions for obtaining hydrogen were identified.
390
Methanol steam reforming: A comparison of different kinetics in the simulation of a packed bed reactor Original Research Article
Chemical Engineering Journal, Volume 154, Issues 1-3, 15 November 2009, Pages 69-75
R. Tesser, M. Di Serio, E. Santacesaria
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391
Hydrogen production for fuel cell by oxidative reforming of diesel surrogate: Influence of ceria and/or lanthana over the activity of Pt/Al2O3 catalysts Original Research Article
Fuel, Volume 87, Issue 12, September 2008, Pages 2502-2511
M.C. Alvarez-Galvan, R.M. Navarro, F. Rosa, Y. Brice?o, M.A. Ridao, J.L.G. Fierro
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392
Transport phenomena in a steam-methanol reforming microreactor with internal heating Original Research Article
International Journal of Hydrogen Energy, Volume 34, Issue 1, January 2009, Pages 314-322
Jeong-Se Suh, Ming-Tsang Lee, Ralph Greif, Costas P. Grigoropoulos
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393
Catalytic steam reforming of methane using Rh supported on Sr-substituted hexaaluminate Original Research Article
Chemical Engineering Science, Volume 64, Issue 24, 16 December 2009, Pages 5231-5239
Nicholas E. McGuire, Neal P. Sullivan, Robert J. Kee, Huayang Zhu, James A. Nabity, Jeffrey R. Engel, David T. Wickham, Michael J. Kaufman
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394
A crucial role of surface oxygen mobility on nanocrystalline Y2O3 support for oxidative steam reforming of ethanol to hydrogen over Ni/Y2O3 catalysts Original Research Article
Applied Catalysis B: Environmental, Volume 81, Issues 3-4, 24 June 2008, Pages 303-312
G.B. Sun, K. Hidajat, X.S. Wu, S. Kawi
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395
Poly-dimethylsiloxane (PDMS) based micro-reactors for steam reforming of methanol Original Research Article
Fuel Processing Technology, Volume 91, Issue 11, November 2010, Pages 1725-1730
Ji Won Ha, Arunabha Kundu, Jae Hyuk Jang
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396
Steam reforming of liquid hydrocarbon fuels for micro-fuel cells. Pre-reforming of model
jet fuels over supported metal catalysts Original Research Article
Fuel Processing Technology, Volume 89, Issue 4, April 2008, Pages 440-448
Jian Zheng, James Jon Strohm, Chunshan Song
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397
Catalytic stability of Ni3Al powder for methane steam reforming Review Article
Applied Catalysis B: Environmental, Volume 80, Issues 1-2, 15 April 2008, Pages 15-23
Yan Ma, Ya Xu, Masahiko Demura, Toshiyuki Hirano
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398
Reactor modeling of sorption-enhanced autothermal reforming of methane. Part I: Performance study of hydrotalcite and lithium zirconate-based processes Original Research Article
Chemical Engineering Journal, Volume 168, Issue 2, 1 April 2011, Pages 872-882
M.H. Halabi, M.H.J.M. de Croon, J. van der Schaaf, P.D. Cobden, J.C. Schouten
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399
Catalytic steam reforming of acetic acid in a fluidized bed reactor with oxygen addition Original Research Article
International Journal of Hydrogen Energy, Volume 33, Issue 16, August 2008, Pages 4387-4396
J.A. Medrano, M. Oliva, J. Ruiz, L. Garcia, J. Arauzo
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400
Novel zeolite-supported rhodium catalysts for ethanol steam reforming
Journal of Power Sources, Volume 183, Issue 2, 1 September 2008, Pages 713-716
Fabiana C. Campos-Skrobot, Roberta C.P. Rizzo-Domingues, Nádia R.C. Fernandes-Machado, Mauricio P. Cant?o
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Catalytic steam reforming of bio-oil is a promising process for producing hydrogen in a sustainable environmentally friendly way that can improve the utilization of local resources (natural sources or wastes). However, there remain drawbacks such as coke formation that
produce operational problems and deactivation of the catalysts. Coprecipitated Ni/Al catalysts are here used in a fluidized bed for reforming at 650 °C of acetic acid as a model compound of bio-oil–aqueous fraction. Different strategies are applied in order to study their effects on the catalytic steam reforming process: modification of the catalyst by increasing the calcination temperature or adding promoters such as calcium. The addition of small quantities of oxygen is also tested resulting in an optimum percentage to achieve a high carbon conversion process with less coke and without a hydrogen yield penalty production. The results for catalytic steam reforming are compared with other ones from literature.
Article Outline
1. Introduction
2. Experimental
2.1. Experimental system
2.2. Catalysts
2.3. Chemicals
3. Results and discussion
3.1. Influence of the calcination temperature of the catalyst
3.2. Influence of calcium addition as a promoter
3.3. Influence of oxygen addition to the steam reforming process
3.4. Literature comparison of acetic acid catalytic steam reforming
4. Conclusions
Acknowledgements
References
Renewable bioethanol is an interesting hydrogen source for fuel cells through steam reforming, but its C–C bond promotes parallel reactions, mainly coke and by-products formation. In this way, good ethanol reforming catalysts are still needed, which explains current research and development efforts around the world. Most catalysts proposed for ethanol reforming are based on oxide-supported noble metals with surface area below 100 m2 g?1 and reaction temperatures above 500 °C. Novel Rh and Rh–K catalysts supported on NaY zeolite with surface area above 440 m2 g?1 are presented in this work. Reaction temperature was fixed at 300 °C and H2O/EtOH molar ratio and reagent flow were varied. Ethanol conversion varied from 50 to 99%, with average increase of 50% due to K promoter, and hydrogen production yield achieved 68%.
Article Outline
1. Introduction
2. Experimental
2.1. Catalysts preparation and characterization
2.2. Catalytic testing
3. Results and discussion
3.1. Catalysts characterization
3.2. Steam reforming catalytic reactions
4. Conclusion
Acknowledgements
References
A miniaturized methanol steam reformer with a serpentine type of micro-channels was developed based on poly-dimethylsiloxane (PDMS) material. This way of fabricating micro-hydrogen generator is very simple and inexpensive. The volume of a PDMS micro-reformer is less than 10 cm3. The catalyst used was a commercial Cu/ZnO/Al2O3 reforming catalyst from Johnson Matthey. The Cu/ZnO/Al2O3 reforming catalyst particles of mean diameter 50–70 μm was packed into the micro-channels by injecting water based suspension of catalyst particles at the inlet point. The miniaturized PDMS micro-reformer was operated successfully in the operating temperatures of 180–240 °C and 15%–75% molar methanol conversion was achieved in this temperature r
ange for WHSV of 2.1–4.2 h?1. It was not possible to operate the micro-reformer made by pure PDMS at temperature beyond 240 °C. Hybrid type of micro-reformer was fabricated by mixing PDMS and silica powder which allowed the operating temperature around 300 °C. The complete conversion (99.5%) of methanol was achieved at 280 °C in this case. The maximum reformate gas flow rate was 30 ml/min which can produce 1 W power at 0.6 V assuming hydrogen utilization of 60%.
Article Outline
1. Introduction
2. Experimental section
2.1. Reactor concept
2.1.1. Chemicals and materials
2.1.2. Fabrication of PDMS micro-reformer
2.1.3. Fabrication of hybrid-PDMS micro-reformer
2.2. Catalyst loading and characterization
2.3. Experimental set-up and reaction conditions
3. Results and discussions
3.1. Performance with PDMS micro-reformer
3.2. Performance with hybrid-PDMS micro-reformer
4. Conclusions
References