Activated Carbon Supported Iron Catalyst for the Fischer-Tropsch Synthesis

2013 ◽  
Vol 805-806 ◽  
pp. 232-235 ◽  
Author(s):  
Hong Yan Ban ◽  
Zi Wei Wang ◽  
Zhi Qiang Wang ◽  
Zhi Gang Fang
Keyword(s):  
Activated Carbon ◽  
Surface Chemistry ◽  
Iron Catalyst ◽  
Catalytic Performance ◽  
Physical Structure ◽  
Fischer Tropsch ◽  
Syngas Conversion ◽  
Ft Synthesis ◽  
Reaction Performance ◽  
Methane Selectivity

The catalyst prepared using the AC as support showed remarkably improvement of reaction performance. The improvement of the reaction performance obtained for the AC is probably ascribed to the physical structure and surface chemistry of AC. The support and corresponding catalyst are characterized by N2 adsorption. Catalytic performance of the catalyst during FT synthesis was excellent. Syngas conversion was about 74%, whereas methane selectivity was low (~2 %).

Activated Carbon Supported Iron Catalyst for the Fischer-Tropsch Synthesis

2011 ◽  
Vol 335-336 ◽  
pp. 161-164
Author(s):  
Hong Yan Ban ◽  
Jiao Wei ◽  
Xiao Zhi Sun ◽  
Zhi Gang Fang
Keyword(s):  
Activated Carbon ◽  
Iron Catalyst ◽  
Catalytic Performance ◽  
Physical Structure ◽  
Tropsch Synthesis ◽  
Fischer Tropsch ◽  
Fischer Tropsch Synthesis ◽  
Syngas Conversion ◽  
Reaction Performance ◽  
Methane Selectivity

The application of activated carbon (AC) supported Fe-Cu-K catalyst for Fischer-Tropsch synthesis (FTS) is studied. The catalyst prepared using the AC as support showed remarkably improvement of reaction performance. The improvement of the reaction performance obtained for the AC is probably ascribed to the physical structure and surface chemistry of AC. The support and corresponding catalyst are characterized by N2 adsorption. Catalytic performance of the catalyst during FT synthesis was excellent. Syngas conversion was about 74%, whereas methane selectivity was low (~2 %).

scholarly journals The Potential Use of Raw Iron Ore in Fischer-Tropsch Synthesis

2021 ◽  
Vol 8 ◽  
pp. 99-115
Author(s):  
Samuel Mubenesha ◽  
Chike George Okoye-Chine ◽  
Franscina Katuchero Ramutsindela ◽  
Joshua Gorimbo ◽  
Mahluli Moyo ◽  
...  
Keyword(s):  
Iron Ore ◽  
Iron Catalyst ◽  
Fixed Bed ◽  
Catalytic Performance ◽  
Pilot Scale ◽  
Manufacturing Cost ◽  
Fischer Tropsch ◽  
Ft Synthesis ◽  
Co Conversion ◽  
The Cost

Fischer-Tropsch (FT) synthesis has been studied in the literature as a greener pathway to cleaner and sustainable hydrocarbons production. However, the cost to upscale laboratory FT formulations to pilot scale is significantly expensive. This work proposes a cheaper and scalable low-temperature FT modified iron ore catalyst that is mechanically suited for fixed bed reactors. The mechanical strength reported in this investigation was three times more than commercial alumina spherical pellets and, therefore, suitable for pilot scale scenarios. A manufacturing cost analysis of iron ore was estimated to be US$38.45/kg using the CatCost model, and the conventionally prepared iron catalyst was US$71.44/kg using the same model. The manufacturing cost estimations of modified iron ore were found to be 46% cheaper than a conventional commercial iron catalyst. The catalytic performance of the modified iron ore catalyst showed a CO conversion of 72.1% ±4.24, with WGS and C5+ selectivity 48.6% ±1.96 and 83.2% ± 5.24, respectively. These findings were comparable (both in CO conversion and product selectivity) to the ones reported by other researchers.

Improving C11+ Hydrocarbon Product Selectivity by Hydrogen Distribution in Fischer-Tropsch Synthesis

2008 ◽  
Vol 6 (1) ◽  
Author(s):  
Shahram Sharifnia ◽  
A. Khodadadi ◽  
Y. Mortazavi
Keyword(s):  
Strong Dependence ◽  
Operating Pressure ◽  
Product Selectivity ◽  
Hydrogen Distribution ◽  
Fischer Tropsch ◽  
Fischer Tropsch Synthesis ◽  
Ft Synthesis ◽  
Co Conversion ◽  
Methane Selectivity ◽  
Hydrocarbon Product

The present study examines the effect of hydrogen distribution (HD) along a Co/SiO2 catalyst bed on Fischer-Tropsch (FT) synthesis. The synthesis is performed under two pressures of 1.0 and 9.0 atm and different H2/CO ratios. The results are compared to those of the usual co-feed, in which both CO and H2 are introduced to the bed inlet. By HD strategy, the methane selectivity is suppressed by as much as 25% and the C11+ selectivity is enhanced up to 26%. CO conversion and product selectivity exhibited a strong dependence on the operating pressure and H2/CO ratio, when hydrogen is distributed.

scholarly journals Effect of Drying Temperature on Iron Fischer-Tropsch Catalysts Prepared by Solvent Deficient Precipitation

2017 ◽  
Vol 2017 ◽  
pp. 1-11 ◽  
Author(s):  
Michael K. Albretsen ◽  
Baiyu Huang ◽  
Kamyar Keyvanloo ◽  
Brian F. Woodfield ◽  
Calvin H. Bartholomew ◽  
...  
Keyword(s):  
Phase Transitions ◽  
Phase I ◽  
Pore Structure ◽  
Catalytic Properties ◽  
Catalytic Performance ◽  
Phase Iii ◽  
Fischer Tropsch ◽  
Two Phase ◽  
Methane Selectivity ◽  
Physical Changes

A novel solvent deficient precipitation (SDP) method to produce nanoparticles was studied for its potential in Fischer-Tropsch synthesis (FTS) catalysis. Using Fe(NO3)3·9H2O as the iron-containing precursor, this method produces ferrihydrite particles which are then dried, calcined, reduced, and carbidized to form the active catalytic phase for FTS. Six different drying profiles, including final drying temperatures ranging between 80 and 150°C, were used to investigate the effect of ammonium nitrate (AN), a major by-product of reaction between Fe(NO3)3·9H2O and NH4HCO3 in the SDP method. Since AN has two phase-transitions within this range of drying temperatures, three different AN phases can exist during the drying of the catalyst precursors. These AN phases, along with physical changes occurring during the phase transitions, may affect the pore structure and the agglomeration of ferrihydrite crystallites, suggesting possible reasons for the observed differences in catalytic performance. Catalysts dried at 130°C showed the highest FTS rate and the lowest methane selectivity. In general, better catalytic performance is related to the AN phase present during drying as follows: phase III > phase II > phase I. However, within each AN phase, lower drying temperatures led to better catalytic properties.

Combining Fischer-Tropsch (FT) and Hydrocarbon Reactions under FT Reaction Conditions -- Catalyst and Reactor Studies with Co or Fe and Pt/ZSM-5

2007 ◽  
Vol 5 (1) ◽  
Author(s):  
Alba Mena Subiranas ◽  
Georg Schaub
Keyword(s):  
Catalyst Deactivation ◽  
Reaction Rates ◽  
Fischer Tropsch ◽  
Transportation Fuels ◽  
Co Catalysts ◽  
Ft Synthesis ◽  
Acidic Sites ◽  
Hydrocarbon Molecules ◽  
Methane Selectivity ◽  
Hydrocarbon Reactions

Fischer-Tropsch synthesis (FTS) offers the potential to produce high-value transportation fuels or petrochemicals from biomass (``2nd generation biofuels"). Primary synthesis products contain mainly n-alkanes and n-alkenes, ranging from methane to high molecular weight waxes. Bifunctional catalysts, as used in petroleum refining, are capable of modifying hydrocarbon molecules. They are characterized by the presence of acidic sites, which provide the hydrocracking and isomerization functions, as well as metal sites, which provide hydro-/dehydrogenation functions, and thus avoid the formation of carbon. The present study addresses the combination of FT synthesis (with Co or Fe catalysts) and hydrocarbon modification reactions. Experimental results obtained in a dual layer configuration with Fe and Co catalysts and Pt/ZSM-5 indicate i) an increase of branched hydrocarbons in the gasoline range (C5-C10), ii) a decrease of alkene and alcohol yields, iii) partial hydrocracking of long chain hydrocarbon molecules leading to higher yields of gasoline and distillates, iv) nearly constant methane selectivity in comparison with the FT catalyst alone, and v) no significant catalyst deactivation. In addition, studies with 1-octene as the model compound were carried out, being mixed with synthesis gas H2/CO or with H2/Ar. The presence of CO decreases reaction rates of hydrogenation and hydrocracking, although all reactions still occur to a significant extent. For the conditions used in this study (1 MPa, 200-300 °C, 4000 kg s/m3), a significant change of hydrocarbon product composition with hydroprocessing catalyst functions added can be observed.

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