Fig. 1. Application of syngas [1].
Fig. 2.Type of catalysts and reaction conditions for the heterogeneously catalyzed gas conversion [4].
Fig. 3. Schematic representation of the morphological and phase change that occur on the α-Fe2O3 catalyst as a result of activation and reaction conditions [5].
Fig. 4. Product distribution according to the Anderson-Schulz-Flory (ASF) model [6].
Fig. 5. A correlation between the acidity and the yield of olefins in the range of C2~C4 hydrocarbons [9].
Fig. 6. CO-TPR profiles of Fe-Cu-K/ZSM5 catalysts [10].
Fig. 7. Carbon number distribution of hydrocarbon product after FT and cracking reaction. Catalysts: FT = 6K/100Fe-6Cu-16AlOx; cracking = ZSM-5 (SiO2/Al2O3, T = 280 ℃). Reaction conditions-FT synthesis (0.5 g cat.): T = 300 ℃; P = 10 atm; GHSV = 3600 (syngas: 30 cm3/min), cracking reaction (0.15 g cat.) [13].
Fig. 8. Correlation of catalytic performance with the intensity ratio of C1s, which is the ratio of deposited carbon (I(dep)) and adsorbed carbon (I(ads)) peaks at binding energies of 288.2 and 284.4 eV respectively on the used catalysts [14].
Fig. 9. The yield to C2-C4 olefin with respect to the superficial gas velocity in FBR and BFBR [15].
Fig. 10. Carbon conversion and CH4 productivity on NixFe1-x/Al2O3 catalysts according to Fe contents [18].
Fig. 11. C2-C4 hydrocarbon selectivity as a function of the CO conversion over 5Co-15Fe/γ-Al2O3 at 10 bar and different reaction temperatures and H2/CO ratios [20].
Fig. 12. Correlation between the surface acidity and the selectivity of hydrocarbons [32].
Fig. 13. Catalytic performance (CO conversion and product distribution) with respect to the acid site density on the ZSM5-modified Co/SiO2 catalysts [33].
Fig. 14. Schematic diagram of ZSM5-modified Co/SiO2 and impregnated cobalt-based catalysts [33].
Fig. 15. Effct of Promoter on the correlation between the surface activity and the selectivity of hydrocarbons [34].
Fig. 16. Correlation between the Pt content and the yield of hydrocarbons [36].
Table 1. Literatures for middle distillates production by F-T synthesis
Table 2. CO hydrogenation over Co-Al2O3-promoter/ZSM-5 catalysts (CO hydrogenation was carried out at H2/CO=2, WHSV=4,000 ml/g·h and P=2.0MPa)
Table 3. Catalytic activity and product distribution on the ordered mesoporous Fe2O3-ZrO2 catalysts (CO hydrogenation was carried out at H2/CO=2, T=300 ℃, WHSV=8,000 L/kg·h and P=2.0MPa)
Table 4. Catalytic performances on the Fe/KIT-6 catalysts (CO hydrogenation was carried out at H2/CO=2, T=350 ℃, WHSV=4,000 L/kg·h and P=2.0MPa)
Table 5. Catalytic performances at a steady-state on the P/m-CoAl catalysts (CO hydrogenation was carried out at H2/CO=2, T=230 ℃, WHSV=6,000 L/kg·h and P=2.0MPa)
Table 6. Catalytic performances at a steady-state on the CoZrP/KIT-6 catalysts (CO hydrogenation was carried out at H2/CO=2, T=230 ℃, WHSV=8,000 L/kg·h and P=2.0MPa)
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