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Research Papers: Fuel Combustion

The Indirectly Heated Carbonate Looping Process for CO2 Capture—A Concept With Heat Pipe Heat Exchanger

[+] Author and Article Information
Daniel Hoeftberger

Chair of Energy Process Engineering,
University of Erlangen-Nuremberg,
Fuerther Strasse 244f,
Nuremberg 90429, Germany
e-mail: daniel.hoeftberger@fau.de

Juergen Karl

Chair of Energy Process Engineering,
University of Erlangen-Nuremberg,
Fuerther Strasse 244f,
Nuremberg 90429, Germany
e-mail: juergen.karl@fau.de

Contributed by the Advanced Energy Systems Division of ASME for publication in the JOURNAL OF ENERGY RESOURCES TECHNOLOGY. Manuscript received July 22, 2015; final manuscript received March 23, 2016; published online April 19, 2016. Assoc. Editor: Ashwani K. Gupta.

J. Energy Resour. Technol 138(4), 042211 (Apr 19, 2016) (7 pages) Paper No: JERT-15-1272; doi: 10.1115/1.4033302 History: Received July 22, 2015; Revised March 23, 2016

The carbonate looping process using the reversible calcination/carbonation reaction of limestone is a promising way to reduce CO2 emissions of fossil fired power plants. This paper describes the concept of an indirectly heated version of this process in which heat pipes accomplish the heat transfer from an air-blown fluidized bed combustor to a bubbling fluidized bed calciner. It defines the calciner's specific heat demand which is a pendant to the heating value of coal. The dimensioning depends on the processes inside heat pipes as well as heat transfer of immersed heating surfaces. Experimental investigations in an electrically heated batch reactor with a similar pipe grid provide heat transfer coefficients under calcination conditions.

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Figures

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Fig. 1

Schematic sketch of the indirectly heated carbonate looping process

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Fig. 2

Schematic sketch and working principle of a heat pipe

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Fig. 3

Example for the specific heat demand of the indirectly heated calciner according to Eq.(1)

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Fig. 4

Different reactor arrangements for calciner and combustor

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Fig. 5

Schematic sketch of a 50 MWth indirectly heated calciner design

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Fig. 6

Determination of the maximum heat pipe length

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Fig. 7

Profiles of superficial gas velocities over calciner height for an inlet temperature of 650 and 800 °C for the 50 MWth calciner design

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Fig. 8

Concept of heat transfer measurement and pictures of the pipe grid of batch reactor and measuring probe for the experimental determination of heat transfer coefficients at elevated temperatures

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Fig. 9

Comparison of calculated and experimentally determined heat transfer coefficients for two types of limestone and sand at a temperature level of 915 °C

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