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SPECIAL SECTION ON THE 2ND EUROPEAN FUEL CELL TECHNOLOGY AND APPLICATIONS CONFERENCE

Modeling Carbon Monoxide Direct Oxidation in Solid Oxide Fuel Cells

[+] Author and Article Information
Luca Andreassi

 University of Rome “Tor Vergata”, Via del Politecnico 1, Rome, 00133 Italyluca.andreassi@uniroma2.it

Claudia Toro1

 University of Rome “Sapienza”, Via Eudossiana 18, Rome, 00184 Italyclaudia.toro@uniroma1.it

Stefano Ubertini

 University of Naples “Parthenope”, Isola C4, Centro Direzionale, Naples, 80143 Italystefano.ubertini@uniparthenope.it

1

Corresponding author.

J. Fuel Cell Sci. Technol 6(2), 021307 (Mar 04, 2009) (15 pages) doi:10.1115/1.3080552 History: Received January 29, 2008; Revised May 30, 2008; Published March 04, 2009

In the present study, the results of the numerical implementation of a mathematical model of a planar anode-supported SOFC are reported. In particular, model results are validated and discussed when the fuel is a mixture of hydrogen and carbon monoxide, focusing on the importance of simulating direct oxidation of carbon monoxide. The mathematical model is solved in a 3D environment and the key issue is the validation comparing with experimental data, which is made in different operating conditions to establish the reliability of the presented model. The results show the importance of simulating direct oxidation of carbon monoxide and its effect on the fuel cell performance.

Copyright © 2009 by American Society of Mechanical Engineers
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References

Figures

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Figure 14

Numerical and experimental current-voltage curves with constant fuel and oxidant (Uox=0.4) utilization coefficients

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Figure 11

Current-voltage curves with constant Uf and oxidant Uox=0.4 (fuel: hydrogen)

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Figure 12

Numerical and experimental current-voltage curves for H2 oxidation and the simultaneous H2–CO oxidation (considering WGS within fuel channel in both cases)

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Figure 13

Hydrogen and carbon monoxide contributions to cell performance

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Figure 15

CO (a) and H2 (b) molar fraction along the gas channel (CO=4.60 N1/h, H2=18.45 N1/h, cell voltage at 0.7 V, and total current at 22 A)

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Figure 16

H2 (a), CO (b), and O2 (c) concentration (mol m−3) at electrode/electrolyte interface(CO=4.60 N1/h, H2=18.45 N1/h, cell voltage at 0.7 V, and Total current at 22 A)

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Figure 17

Current density [A/m2] produced by H2 (a) and CO (b) at anode/electrolyte interface (CO=4.60 N1/h, H2=18.45 N1/h, cell voltage at 0.7 V, total current at 22 A)

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Figure 1

Gas channel geometry

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Figure 2

Current-voltage curves with constant fuel (Uf) and oxidant (Uox) utilization coefficients (fuel: syngas)

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Figure 3

Single cell test rig setup

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Figure 4

Reference coordinate system and three-dimensional computational domains for the numerical simulation

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Figure 5

Scheme of governing equation applied in each domain

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Figure 6

Parallel electrical circuit analogy to model simultaneous H2 and CO oxidation

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Figure 7

Scheme of governing equations together with the boundary conditions solving the electrochemical problem

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Figure 8

External boundary conditions for thermal submodel

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Figure 9

Solution algorithm

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Figure 10

Numerical and experimental polarization curves for updating phase (fuel: hydrogen)

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Figure 18

Temperature (K) profile at cell middle plain (CO=4.60 N1/h, H2=18.45 N1/h, cell voltage at 0.7 V, total current at 22 A)

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Figure 19

CO molar fraction at anode/electrolyte interface: considering CO WGSR and oxidation (a), and considering only CO WGSR (b) (CO=4.60 N1/h, H2=18.45 N1/h, cell voltage at 0.7 V, total current 22 A)

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Figure 20

WGSR rate (mol m−3 s−1) within the gas channel: considering CO WGSR and oxidation (a), and considering only CO WGSR (b)

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