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RESEARCH PAPERS

Production of Hydrogen With Low Carbon Monoxide Formation Via Catalytic Steam Reforming of Methanol

[+] Author and Article Information
Sanjay Patel

Department of Chemical Engineering, Indian Institute of Technology-Delhi, Hauz-Khas, New Delhi-110016, India

K. K. Pant

Department of Chemical Engineering, Indian Institute of Technology-Delhi, Hauz-Khas, New Delhi-110016, Indiakkpant@chemical.iitd.ac.in

J. Fuel Cell Sci. Technol 3(4), 369-374 (Mar 28, 2006) (6 pages) doi:10.1115/1.2349514 History: Received July 25, 2005; Revised March 28, 2006

The production of hydrogen was investigated in a fixed bed tubular reactor via steam reforming of methanol (SRM) using CuOZnOAl2O3 catalysts prepared by wet impregnation method and characterized by measuring surface area, pore volume, x-ray diffraction patterns, and scanning electron microscopy photographs. The SRM was carried out at atmospheric pressure, temperature 493573K, steam to methanol molar ratio 1–1.8 and contact-time (W/F) 315kg cat./(mol/s of methanol). Effects of reaction temperature, contact-time, steam to methanol molar ratio and zinc content of the catalyst on methanol conversion, selectivity, and product yields was evaluated. The addition of zinc enhanced the methanol conversion and hydrogen production. The excess steam promoted the methanol conversion and suppressed the carbon monoxide formation. Different strategies have been mentioned to minimize the carbon monoxide formation for the steam reforming of methanol to produce polymer electrolyte membrane (PEM) fuel cell grade hydrogen. Optimum operating conditions with appropriate composition of catalyst has been investigated to produce more selective hydrogen with minimum carbon monoxide. The experimental results were fitted well with the kinetic model available in literature.

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Copyright © 2006 by American Society of Mechanical Engineers
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Figures

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Figure 1

Effect of particle size on methanol conversion

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Figure 2

X-ray diffraction patterns of reduced fresh catalysts

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Figure 3

SEM photographs of CAT4 (a) fresh catalyst (b) spent catalyst

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Figure 4

Effect of contact-time on methanol conversion for different CuO∕ZnO∕Al2O3 catalysts (T=513K, S∕M=1.4molar, P=1atm)

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Figure 5

Effect of contact-time on methanol conversion at different temperatures (catalyst CAT4, S∕M=1.4Molar, P=1atm)

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Figure 6

Effect of contact-time on methanol conversion and product selectivity (catalyst CAT4, T=573K, S∕M=1.4molar, P=1atm)

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Figure 7

Effect of temperature on methanol conversion and selectivity (catalyst CAT4, W∕F=15kgcat./(mol/s of methanol), S∕M=1.4molar, P=1atm)

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Figure 8

Effect of S/M molar ratio on methanol conversion and carbon monoxide formation (catalyst CAT4, T=553K, W∕F=9kgcat./(mol/s of methanol), P=1atm)

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Figure 9

Experimental and model predicted methanol conversion as a function of contact-time (P=1atm, S∕MRatio=1.4Molar)

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Figure 10

Experimental and model predicted yield of H2, CO2, and CO at 553K as a function of contact-time

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