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Technical Briefs

Application of an Internally Circulating Fluidized Bed for Windowed Solar Chemical Reactor with Direct Irradiation of Reacting Particles

[+] Author and Article Information
Tatsuya Kodama1

Department of Chemistry and Chemical Engineering, Faculty of Engineering,  Niigata University, 8050 Ikarashi 2-nocho, Nishi-ku, Niigata 950-2181, Japan

Syu-ichi Enomoto, Nobuyuki Gokon

Department of Chemistry and Chemical Engineering, Faculty of Engineering,  Niigata University, 8050 Ikarashi 2-nocho, Nishi-ku, Niigata 950-2181, Japan; Graduate School of Science and Technology, Niigata University, 8050 Ikarashi 2-nocho, Nishi-ku, Niigata 950-2181, Japan

Tsuyoshi Hatamachi

Department of Chemistry and Chemical Engineering, Faculty of Engineering,  Niigata University, 8050 Ikarashi 2-nocho, Nishi-ku, Niigata 950-2181, Japan

1

Corresponding author.

J. Sol. Energy Eng 130(1), 014504 (Jan 07, 2008) (4 pages) doi:10.1115/1.2807213 History: Received September 21, 2006; Revised June 12, 2007; Published January 07, 2008

Solar thermochemical processes require the development of a high-temperature solar reactor operating at 10001500°C, such as solar gasification of coal and the thermal reduction of metal oxides as part of a two-step water splitting cycle. Here, we propose to apply “an internally circulating fluidized bed” for a windowed solar chemical reactor in which reacting particles are directly illuminated. The prototype reactor was constructed in a laboratory scale and demonstrated on CO2 gasification of coal coke using solar-simulated, concentrated visible light from a sun simulator as the energy source. About 12% of the maximum chemical storage efficiency was obtained by the solar-simulated gasification of the coke.

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Copyright © 2008 by American Society of Mechanical Engineers
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Figure 1

Concept of solar chemical reactor with an internally circulating fluidized bed

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Figure 2

Schematic of a prototype reactor with an internally circulating fluidized bed of reacting particles

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Figure 3

Variations of CO production rate as a function of (a) time or (b) the coke conversion at various Ua:Ud ratios. Ud was fixed to 2.5Nmmin−1.

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Figure 4

Variations of CO production rate as a function of (a) time or (b) the coke conversion at various total CO2 flow rates. The Ua:Ud ratio was 1:12.

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Figure 5

Time variation of the light-to-chemical energy conversion. The Ua:Ud ratio was 1:12.

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