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Operating analysis of a fluidized bed carbonator to remove \(\text{CO}_{2}\)

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Abstract

This paper mainly focuses on the utilization of reversible carbonation reaction of CaO to capture \(\text{CO}_{2}\) from the flue gas. The operating analysis regarding the effects of superficial gas velocity, the particle diameter and the calcination/carbonation cycle number on the carbonation process has been performed and compared to experimental data. It is concluded that in order to optimize the carbonation process the superficial gas velocity can decrease gradually during the reaction and smaller-sized absorbent should be chosen. However, the limits of superficial gas velocity and absorbent size need to be taken into consideration as well to avoid entrainment.

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Abbreviations

\(C_{\mathrm{bCO}_{2}}\) :

   \(\text{CO}_{2}\) concentration in the bubble phase

\(C_{\mathrm{CO}_{2},\mathrm{eq}}\) :

   Equilibrium \(\text{CO}_{2}\) concentration over CaO

\(C_{\mathrm{eCO}_{2}}\) :

   \(\text{CO}_{2}\) concentration in the emulsion phase

\(d_b\) :

   Bubbles diameter

\(d_p\) :

   Particles diameter

\(e_0\) :

   Particle porosity

\(f_a\) :

   Fraction of active CaO in the carbonator

\(k_g\) :

   Mass transfer coefficient in the emulsion phase

\(k_s\) :

   Carbonation reaction rate constant at the CaO particle surface

\(K_\mathrm{be}\) :

   Overall gas interchange coefficient between bubble and emulsion phases

\(K_r\) :

   Overall carbonation rate constant of particles in the emulsion phase

\(K_{ri}\) :

   Carbonation reaction rate constant

N:

   The number of calcination/carbonation cycle

T:

   Temperature of carbonation

\(S_0\) :

   Initial surface area of CaO per unit volume of solid CaO

\(u_0\) :

   Superficial gas velocity

\(u_b^*\) :

   Effective gas velocity in bubble phase

\(u_\mathrm{mf}\) :

   Minimum fluidization velocity

\(X\) :

   Actual carbonation conversion of CaO to \(\text{CaCO}_{3}\)

\(X_{b,N}\) :

   Maximum carbonation conversion of CaO to \(\text{CaCO}_{3}\) in the Nth cycle

\(\delta \) :

   Bubble fraction in the fluidized bed

\(\varepsilon _\mathrm{mf}\) :

   Bed porosity at minimum fluidization

\(\rho _\mathrm{CaO}\) :

   True particle density

\(\gamma _b\) :

   Volume of solids in bubble phase divided by the volume of bubbles

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Acknowledgments

The work presented here is funded by China National Natural Science Foundation (No. 51106048) and the Program for 973 Project ‘Spatio-temporal Distribution and Evaluation Method and System Integration of Energy Consumption at Overall Working Conditions for Large-scale Coal-fired Power Generating Unit’ (No. 2009CB219801).

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Authors and Affiliations

  1. School of Energy Power and Mechanical Engineering, Beijing Key Laboratory of Energy Safety and Clean Utilization, Condition Monitoring and Control for Power Plant Equipment of Ministry of Education, North China Electric Power University, Beijing, 102206, China

    Rongrong Zhai, Yongping Yang, Yong Zhu & Kai Zhang

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  1. Rongrong Zhai
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Correspondence to Rongrong Zhai.

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Zhai, R., Yang, Y., Zhu, Y. et al. Operating analysis of a fluidized bed carbonator to remove \(\text{CO}_{2}\) . Energy Syst 4, 47–60 (2013). https://doi.org/10.1007/s12667-012-0065-x

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