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Frontiers of Chemical Science and Engineering

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Front. Chem. Sci. Eng.    2018, Vol. 12 Issue (2) : 315-325    https://doi.org/10.1007/s11705-017-1698-z
VIEWS & COMMENTS
Mature versus emerging technologies for CO2 capture in power plants: Key open issues in post-combustion amine scrubbing and in chemical looping combustion
Giorgia De Guido1(), Matteo Compagnoni2, Laura A. Pellegrini1, Ilenia Rossetti2
1. Department of Chemistry, Materials and Chemical Engineering “Giulio Natta”, Politecnico di Milano, Piazza Leonardo da Vinci 32, 20133 Milan,Italy
2. Department of Chemistry, Università degli Studi di Milano, INSTM Unit Milano-Università and CNR-ISTM, Via Camillo Golgi 19, 20133 Milan, Italy
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Abstract

Carbon capture and storage (CCS) have acquired an increasing importance in the debate on global warming as a mean to decrease the environmental impact of energy conversion technologies, by capturing the CO2 produced from the use of fossil fuels in electricity generation and industrial processes. In this respect, post-combustion systems have received great attention as a possible near-term CO2 capture technology that can be retrofitted to existing power plants. This capture technology is, however, energy-intensive and results in large equipment sizes because of the large volumes of the flue gas to be treated. To cope with the demerits of other CCS technologies, the chemical looping combustion (CLC) process has been recently considered as a solution for CO2 separation. It is typically referred to as a technology without energy penalty. Indeed, in CLC the fuel and the combustion air are never mixed and the gases from the oxidation of the fuel (i.e., CO2 and H2O) leave the system as a separate stream and can be separated by condensation of H2O without any loss of energy. The key issue for the CLC process is to find a suitable oxygen carrier, which provides the fuel with the activated oxygen needed for combustion. The aim of this work is to explore the feasibility of using perovskites as oxygen carriers in CLC and to consider the possible advantages with respect to the scrubbing process with amines, a mature post-combustion technology for CO2 separation.
Keywords CO2 capture      monoethanolamine      chemical looping combustion      oxygen carrier      perovskites     
Corresponding Author(s): Giorgia De Guido   
Just Accepted Date: 30 November 2017   Online First Date: 18 January 2018    Issue Date: 09 May 2018
 Cite this article:   
Giorgia De Guido,Matteo Compagnoni,Laura A. Pellegrini, et al. Mature versus emerging technologies for CO2 capture in power plants: Key open issues in post-combustion amine scrubbing and in chemical looping combustion[J]. Front. Chem. Sci. Eng., 2018, 12(2): 315-325.
 URL:  
https://academic.hep.com.cn/fcse/EN/10.1007/s11705-017-1698-z
https://academic.hep.com.cn/fcse/EN/Y2018/V12/I2/315
Technology Advantages Disadvantages
Absorption Well established process
High operational confidence		 Energy penalty for solvent regenerationa)
Equipment corrosion in presence of O2
Pre-absorption treatment required to remove solvent-detrimental components (e.g., SOx and NOx)
Possible environmental impact and safety problems due to solvent degradationb)
Adsorption Lower regeneration energy relative to solvent-based processes Particle attrition
Large volumes of solid sorbents
Thermal management of large scale adsorber vessels
Currently not suitable for processing very high gas flows containing many impurities
Membranes Low energy requirements relative to solvent-based processes
Small foot-print
Possible modular designc)		 Strongly affected by flue gas conditions (e.g., low CO2 concentration and pressure)
Potential fouling of membrane surfaces
Uncertainty about the possibility of integration into a power plant
Not a mature technology
Cryogenics Mature technology already adopted for CO2 recovery
Viable for very high CO2 concentrations		 Low operating temperatures
Hydrate-based Small energy penaltyd) At the R&D stage
Tab.1  Comparison among existing CO2 separation technologies
Test run [24] LL /(molCO2·molMEA−1) Mole inlet CO2 /mol-% Gas rate /(m3·min−1) Liquid rate
/(L·min−1)		 CO2 removal
/%		 Actual reboiler duty /(MJ·h−1)
29 0.28 16.6 11.00 54.9 70 918
30 0.28 16.6 11.00 54.9 70 918
43 0.23 17.0 11.00 39.4 72 756
44 0.23 17.0 11.00 39.4 72 754
47 0.28 18.0 8.23 30.1 69 738
48 0.28 18.0 8.23 30.1 69 775
Tab.2  Operating conditions and energy contributions for the experimental tests performed by Dugas [24] that have been chosen in this work for model validation (packing for the absorber: IMTP #40)
Test run [24] Exp. Aspen Plus® default [20] Proposed model [25]
y CO2,out y CO2,out Abs. err. /% y CO2,out Abs. err. /%
29 0.0532 0.04619 13.18 0.05156 3.08
30 0.0591 0.05022 15.03 0.05558 5.96
43 0.0558 0.04698 15.81 0.05238 6.13
44 0.0540 0.04655 13.80 0.05203 3.65
47 0.0638 0.06682 4.73 0.06753 5.85
48 0.0619 0.06339 2.41 0.06374 2.97
AAD% 10.82 AAD% 4.61
Tab.3  CO2 mole fraction in the purified gas stream leaving the absorber in the test runs [24] considered in this work
Fig.1  Parity plot for the concentration (mole fraction) of CO2 in the purified gas stream leaving the absorber for the test runs reported in Table 3
Fig.2  Schematic representation of the CLC technology (MexOy denotes the generic metal oxide acting as oxygen carrier, MexOy−δ the reduced material sent to the regeneration step)
Fig.3  Examples of (a) TPD analysis of sample La0.9Ce0.1MnO3 (blu, solid line) and LaMnO3 (red, dotted line); (b) TPR pattern relative to sample LaCoO3
Sample Titrated oxygen /(mol·kgcat−1) Oxygen ratio, RO
LaCoO3 6.88 0.110
La0.9Sr0.1 CoO3 6.10 0.098
La0.9Ce0.1 CoO3 6.45 0.103
0.5wt-% Pt- LaCoO3 5.60 0.090
0.5wt-% Pd- LaCoO3 6.67 0.107
LaMnO3 6.21 0.099
La0.9Sr0.1 MnO3 7.55 0.121
La0.9Ce0.1 MnO3 6.82 0.109
0.5wt-% Pt- LaMnO3 3.65 0.058
0.5wt-% Pd- LaMnO3 4.91 0.079
Fe2O3a) 9.37b) 0.30
NiOa) 6.56b) 0.21
Tab.4  Quantitative titration of oxygen (as mol/kgcat) by TPR analysis (experimental data from ref. [51])
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