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Research Papers

Syngas and Hydrogen Production by Cyclic Redox of ZrO2-Supported CeO2 in a Volumetric Receiver-Reactor

[+] Author and Article Information
Jong Tak Jang, Ki June Yoon

School of Chemical Engineering,
Sungkyunkwan University,
Suwon 440-746, South Korea

Gui Young Han

School of Chemical Engineering,
Sungkyunkwan University,
Suwon 440-746, South Korea
e-mail: gyhan@skku.edu

1Corresponding author.

Contributed by the Solar Energy Division of ASME for publication in the JOURNAL OF SOLAR ENERGY ENGINEERING. Manuscript received October 8, 2012; final manuscript received March 27, 2013; published online March 04, 2014. Assoc. Editor: Wojciech Lipinski.

J. Sol. Energy Eng 136(3), 031008 (Mar 04, 2014) (5 pages) Paper No: SOL-12-1270; doi: 10.1115/1.4026677 History: Received October 08, 2012; Revised March 27, 2013

In order to utilize sustainable solar energy, cyclic operations of syngas production by methane reforming (reduction) and subsequent hydrogen production by water splitting (oxidation) were performed by using simulated solar-light irradiation to ZrO2-supported CeO2 particles which were coated on a SiC ceramic foam disk. This redox process is a promising chemical pathway for storage and transportation of solar heat by converting solar energy to chemical energy. By properly adjusting the methane reforming time, carbon deposition due to the undesirable methane decomposition could be avoided. The produced syngas had the H2/CO ratio of 2.0, which is suitable for the Fischer–Tropsch synthesis or methanol synthesis, and the produced pure hydrogen can be used for fuel cells. When the cyclic reactions were repeated several times at two temperatures (800 °C, 900 °C), the conversion of CeO2 and the H2 yield were reasonable and were maintained nearly constant from the second cycle, exhibiting good stability of the redox process.

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Figures

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Fig. 1

Procedure for preparing the metal oxide sample on the SiC foam disk using drop-coating

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Fig. 2

The solar volumetric receiver-reactor (Alloy 625)

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Fig. 3

Schematic diagram of the experimental facility

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Fig. 4

H2 and CO production rates during MR for 50 wt. % CeO2/ZrO2/SiC at 900 °C (CH4 = 3 cm3/min, N2 = 27 cm3/min)

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Fig. 5

H2 production rate during WS for 50 wt. % CeO2/ZrO2/SiC at 900 °C (H2O = 10 cm3/min, N2 = 27 cm3/min)

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Fig. 6

H2 and CO yields during five repeated cycles of MR and WS for 50 wt. % CeO2/ZrO2/SiC at 800 °C

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Fig. 7

H2 and CO yields during five repeated cycles of MR and WS for 50 wt. % CeO2/ZrO2/SiC at 900 °C

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Fig. 8

SEM images of the 50 wt. % CeO2/ZrO2 samples: (a) fresh, (b) after the first cycle, (c) after the third cycle, and (d) after the fifth cycle (temperature = 900 °C)

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Fig. 9

XRD patterns of the fresh 50 wt. % CeO2/ZrO2 sample, the sample after the first MR at 900 °C, and the sample after five repeated cycle at 900 °C (▲: ZrO2, •:CeO2, ◆:Ce0.5Zr0.5O2)

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