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Research Papers

Catalytic Steam Reforming of Glycerol Over Cerium and Palladium-Based Catalysts for Hydrogen Production

[+] Author and Article Information
Ali Ebshish

Department of Chemical and Process Engineering,
Faculty of Engineering,
Universiti Kebangsaan Malaysia (UKM),
Bangi, 43600, Selangor, Malaysia
e-mail: aliebshish@gmail.com

Zahira Yaakob

Department of Chemical and Process Engineering,
Faculty of Engineering,
Universiti Kebangsaan Malaysia (UKM),
Bangi, 43600, Selangor, Malaysia;
Fuel Cell Institute,
Universiti Kebangsaan Malaysia,
(UKM), Bangi, Malaysia

Y. H. Taufiq-Yap

Centre of Excellence for Catalysis Science and Technology,
Faculty of Science,
Universiti Putra Malaysia,
43400 UPM Serdang,
Selangor, Malaysia

Abdulmajid Shaibani

Department of Chemical and Process Engineering,
Faculty of Engineering,
Universiti Kebangsaan Malaysia (UKM),
Bangi, 43600, Selangor, Malaysia

Contributed by the Advanced Energy Systems Division of ASME for publication in the JOURNAL OF FUEL CELL SCIENCE AND TECHNOLOGY. Manuscript received July 26, 2012; final manuscript received November 2, 2012; published online March 21, 2013. Assoc. Editor: Ken Reifsnider.

J. Fuel Cell Sci. Technol 10(2), 021003 (Mar 21, 2013) (6 pages) Paper No: FC-12-1066; doi: 10.1115/1.4023687 History: Received July 26, 2012; Revised November 02, 2012

In this work, catalytic steam reforming of glycerol for hydrogen production was performed over Ce/Al2O3 and Pd/Al2O3 catalysts prepared via the impregnation method. The catalysts were characterized by scanning electron microscopy (SEM-EDX), transmission electron microscopy (TEM), BET surface area, and X-ray diffraction (XRD). Two sets of catalytic reactions were conducted, one comparing 1% Pd/Al2O3 to 1% Ce/Al2O3 and the second comparing 1% Ce/Al2O3 loading to 10% Ce/Al2O3 loading. All catalytic reactions were performed using a fixed-bed reactor operated at 600 °C and atmospheric pressure. Aglycerol–water mixture at a molar ratio of 1:6 was fed to the reactor at 0.05 ml/min. In the first set of experiments, Pd/Al2O3 exhibited higher hydrogen productivity than Ce/Al2O3. A maximum hydrogen yield of 56% and a maximum selectivity of 78.7% were achieved over the Pd/Al2O3 catalyst. For the second set of experiments, the results show that the reaction conversion increased as the cerium loading increased from 1% to 10%. A total average hydrogen yield of 28.0% and a selectivity of 45.5% were obtained over 1% Ce/Al2O3, while the total average hydrogen yield and selectivity were 42.2% and 52.7%, respectively, for 10% Ce/Al2O3.

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Figures

Grahic Jump Location
Fig. 1

XRD analysis for (a) Al2O3, (b) 1 wt. % Pd/Al2O3, (c) 1 wt. % Ce/Al2O3 and (d) 10 wt. % Ce/Al2O3

Grahic Jump Location
Fig. 2

SEM for (a) 1 wt. % Ce/Al2O3, (b) 10 wt. % Ce/Al2O3, (c) 1 wt. % Pd/Al2O3, (d) 1 wt. % Ce/Al2O3 with Ce indicated in red, (e) 10 wt. % Ce/Al2O3 with Ce indicated in red and (f) 1 wt. % Pd/Al2O3 with Pd indicated in red. (See online article for color.)

Grahic Jump Location
Fig. 3

TEM analysis for (a) 10 wt. % Ce/Al2O3 and (b) 1 wt. % Pd/Al2O3

Grahic Jump Location
Fig. 4

Reforming activity over 1 wt. % Pd/Al2O3 and 1 wt. % Ce/Al2O3 (a) H2 yield, (b) moles of H2 produced, (c) glycerol conversion into gases, and (d) H2 selectivity

Grahic Jump Location
Fig. 5

Reforming activity over 1 wt. % Ce/Al2O3 and 10 wt. % Ce%Al2O3: (a) H2 yield, (b) moles of H2 produced, (c) glycerol conversion into gases, and (d) H2 selectivity

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