1 Introduction
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All generated CO2 can be formed in the fuel reactor, see Fig. 1 (right). In normal indirect gasification, the carbon dioxide is generated primarily in the combustion chamber, or air reactor and hence diluted with nitrogen. Thus, in CLG, a more concentrated stream of CO2 is generated together with the syngas, applicable for separation and storage. It should be pointed out that even in indirect gasification, there will be some CO2 generated in the gasifier, hence a carbon removal step is always going to be needed prior to the fuel production.
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Partial oxidation of the fuel with the oxygen carrier could enhance conversion of hydrocarbons to syngas.
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The higher H2O and CO2 concentrations in the fuel reactor in comparison to indirect gasification will likely mean less tar formation (Larsson et al. 2014).
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Oxygen carrier particles may provide additional sites for catalytic reforming reactions.
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Chemical looping could provide a solution for much cleaner conversion of wastes, as the fuel reactor may provide a sink for the impurities, keeping the air reactor—and hence the main exhaust gas flow—clean and free from corrosive components, see Fig. 1. This is likely especially important for alkali and chlorine compounds, common precursors for high-temperature corrosion in biomass-fired systems (Boström et al. 2012).
2 Experimental
2.1 Materials
Material | Mn | Fe | Si | Al | Ca | K |
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Sinaus | 53.1 | 8.1 | 3.5 | 2.4 | 0.9 | 0.9 |
Sinaus-K | 49.3 | 7.9 | 3.2 | 2.3 | 0.8 | 5.6 |
Mangagran | 59.7 | 3.6 | 1.6 | 2.6 | 0.2 | 0.4 |
Mangagran-K | 54.5 | 2.6 | 1.3 | 2.1 | 0.1 | 6.6 |
LD slag | 2.4 | 13.9 | 5.1 | 0.5 | 29.7 | 0.0 |
LD slag-K | 2.7 | 13.9 | 5.0 | 0.5 | 26.5 | 4.0 |
2.2 Experimental setup and procedure
Compound | Concentration (mol%) |
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H2O | 25 |
CO | 10.75 |
CO2 | 3.73 |
H2 | 5.78 |
CH4 | 3.5 |
C2H4 | 1.25 |
C6H6 | 0 or 1.4% |
N2 | Balance |
2.3 Gas analysis
2.4 Material characterization
2.5 Data evaluation
3 Results
3.1 Comparison of reactivity of the three untreated oxygen carriers
3.2 Effect of impregnation with potassium
3.3 Conversion of benzene (C6H6)
3.4 Characterization
Sample | Before experiment | After experiment |
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Mangagran | Mn3O4, Mn2−xFexO3, Ca1−xMnxO, Mn7SiO12, α-KAlO2 | Mn3O4, (Mg1−xFex)SiO4, Ca3−xMnxSi2O7 |
Mangagran-K | Mn3O4, α-KAlO2, K1.39Mn3O6, K < Al, Fe > Si2O8, K2CO3 | M0.95O, α-KAlO2 |
Sinaus | Mn7SiO12, Ca1−xMnxO, MnFeO3, Mn3O4, Fe3−xMnxO4 | (FeO)x (MnO)1−x |
Sinaus-K | Mn3O4, Fe3−xMnxO4, α-KAlO2 | (FeO)x (MnO)1−x, α-KAlO2 |
LD slag | CaO, Ca2SiO4, Ca3SiO5, Mg0,99Fe0,01O, Ca2FexMnyMgzSiwO5, Mg0,6Mn0,4Fe2O4, K3P3O9, SiO2 | CaO, Ca2SiO4, Ca3SiO5, Mg0,99Fe0,01O, Ca2FexMnyMgzSiwO5, Mg0,6Mn0,4Fe2O4, K3P3O9, SiO2 |
LD slag-K | Ca2SiO4, Ca3SiO5, Mg0,99Fe0,01O, Ca2FexMnyMgzSiwO5, Mg0,6Mn0,4Fe2O4, K3P3O9, SiO2 | Ca2SiO4, Ca3SiO5, Mg0,99Fe0,01O, Ca2FexMnyMgzSiwO5, Mg0,6Mn0,4Fe2O4, K3P3O9, SiO2, KAlSiO4 |
BET surface area (m2/g) | Pore volume (mL/g) | |||
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Name | Before experiment | After experiment | Before experiment | After experiment |
Mangagran | 0.16 | 0.89 | 1.8 | 6.3 |
Mangagran-K | 0.94 | 1.55 | 6.8 | 11.0 |
Sinaus | 0.072 | 0.84 | 1.2 | 5.7 |
Sinaus-K | 0.46 | 0.97 | 5.1 | 7.4 |
LD slag | 0.42 | 0.39 | 3.2 | 2.9 |
LD slag-K | 0.46 | 0.44 | 3.8 | 3.8 |
4 Discussion
5 Conclusions
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The two manganese oxygen carriers showed the highest degree of oxidation in comparison to LD slag, a waste product from the steel industry.
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The impregnation of alkali resulted in improved reactivity during the period where there was oxygen transfer, especially for the manganese ores.
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The increased oxygen transfer also resulted in a higher conversion of tar precursors C2H4 and C6H6, and the latter was converted completely by Mangagran-K.
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The fate of alkali in the oxygen carrier during testing varied extensively. For the Mangagran-K, most alkali remained in the particle, but was transferred throughout the particle. For Sinaus manganese ore, most alkali remained after testing but remained near the surface. Finally, the LD slag lost most of the alkali during redox testing.
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Certain oxygen carriers could likely be beneficial for use with high-alkali fuel, as they may react with alkali in the CLC/CLG reactor, which may not only decrease corrosion, but enhance reactivity.