Fischer–Tropsch process - Wikipedia
 Dry, M.E. "The Fischer-Tropsch Process: 1950-2000," Catal. Today 71, 227 (2002).
Fischer–Tropsch Synthesis in a Fixed Bed Reactor - …
AB - This study covers the performance of five cobalt-based catalytic systems with different support characteristics in Fisher-Tropsch synthesis (FTS) under conventional gas-phase using syngas, and the manner in which the reaction medium is influenced by the addition of solvents such as n-hexane and squalane has been also investigated. The reaction was conducted in a fixed bed high-pressure FTS reactor setup at a reaction temperature of 220 °C to 260 °C. In terms of the effect of the reaction medium, higher CO conversion was obtained in gas phase reaction, whereas the olefin selectivity was higher in n-hexane medium than in gas phase and squalane medium. In addition, the undesired production of CH4 and CO2 was relatively reduced in solvent addition compared to the gas phase FTS. The reaction performance was also compared according to the type of catalyst. CO conversion by type of catalyst decreased in the following order: 20% Co/SiO2>20% Co/Al2O3>20% Co/HAS>20% Co/Si-MMS>20% Co/TiO2. However, the C5+ content of products was little affected by catalyst supports.
N2 - Fischer-Tropsch synthesis (FTS) over unsupported coprecipitated cobalt catalysts in n-decane in a batch slurry phase reactor by adding water vapor (H2O/CO=0.12 in molar ratio) prior to reaction has been studied. The addition of water vapor exhibits a marked effect on the product selectivity. In the absence of water, the carbon number distribution of FT products follows the classical Anderson-Schulz-Flory (ASF) pattern resulting in a low selectivity (32%) in the desired C10+ hydrocarbons. In contrast, with the promotion of water vapor, the formation of heavy products is appreciably increased up to 87.3% in C10+ hydrocarbons so that the selectivity in the range of C8-C30 increases obviously along with an increase in carbon number (n), which leads to a substantial deviation from ASF pattern. The effect of water is explained by suppressing secondary hydrogenation of 1-olefins and facilitating their readsorption and chain growth.
Fischer−Tropsch Synthesis with Cobalt Catalysts …
Synthesis gas is converted into a hydrocarbon wax (a mixture of long-chain alkanes) by heating it and passing the vapour over a cobalt catalyst (the Fischer-Tropsch process) (Figure 2, route 5). The (SMDS) is a modern development of this process. The hydrocarbon waxes are subsequently catalytically cracked with excess hydrogen () (Figure 2, route 9) to form smaller alkanes, for example:
Smaller amounts of light gases are also produced in the Fischer-Tropsch reactor and the hydrocracker (for example, ethane and propane). These can either be recycled back to the gasifier or used for heat and power production in the biorefinery.
Talk:Fischer–Tropsch process - Wikipedia
Another way to produce propene is via methanol (produced from biomass via synthesis gas), which is an example of the MTO (Methanol To Olefins) process. (Olefin is the older name for the homologous series, alkenes). Methanol can be converted into high purity ethene and propene via dimethyl ether (Figure 3, routes 10 and 9). Methanol vapour is passed over alumina at ca 600 K. An equilibrium mixture of methanol, dimethyl ether and steam is produced, containing about 25% methanol:
Any solid biomass including for example agricultural, city and industrial waste can be used to make synthesis gas using techniques similar to its production from . More recent developments includes a plant in the Netherlands, which is using liquid propane-1,2,3-triol (glycerol), a by-product from the production of , from animal fats and vegetable oils.
Fischer–Tropsch process | Gas To Liquids | Catalysis
Fischer-Tropsch Process - Commercial Aspects.
Cobalt catalysts are more active for Fischer–Tropsch synthesis when the feedstock is natural gas
Fischer–Tropsch process - OilfieldWiki
How to simulate Fischer Tropsch Synthesis on Aspen …
Kinetics of the Fischer-Tropsch Synthesis on Iron Catalysts, report, Date Unknown; Washington D.C..
Compact Fischer-Tropsch Synthesis Technology
where the elemental carbon bond is included. The reaction energy is then EB = -1.42 eV, which is less (0.13 eV = 1574°C) than the Fischer-Tropsch reaction.  It follows that an efficient cooling system is necessary to produce transport fuels and maintain an activated catalyst.
MultiFuel Fischer-Tropsch (FT) Reactor
Figure no. 11a : Sasol "slurry" Reactor - Fischer-Tropsch Gasification. (source, CSFB Global Oil & Gas Conference, 8th June 2005, Enrico Ganter, Sasol Limited)
Greener Fischer-Tropsch Processes for Fuels and Feedstocks
Preheated synthesis gas is fed to the bottom of the reactor, where it is distributed into the slurry consisting of liquid wax and catalyst particles. As the gas bubbles upwards through the slurry, it diffuses into the slurry and is converted into more wax by the Fischer-Tropschreaction. The heat given off by the reaction is removed using cooling coils inside the Slurry Phase Reactor that generate steam. The product wax is separated from the slurry containing the catalyst particles in a proprietary process. The lighter, more volatile fractions leave in a gas stream from the top of the reactor. The gas stream is cooled to recover the lighter cuts and water. The hydrocarbon streams are sent to the product upgrading unit, while the water stream is treated in the water recovery unit.
FISHER TROPSH SYNTHESIS IN A CIRCULATING FLUIDIZED …
Ruthenium can also be used as a catalyst, but it is 50,000 times more expensive than iron. [6,9] Ruthenium has the advantage of working at a lower temperature (but higher pressure) than the other metals and producing the highest molecular weight hydrocarbons without the addition of any promoters.  Since it functions as a pure metal, this additionally makes ruthenium the ideal catalyst to study the mechanism behind the Fischer-Tropsch synthesis.
Fischer–Tropsch Hydrocarbons Synthesis from a …
A numerical simulation that models the Fischer–Tropsch (FT) synthesis in a tubular multitube reactor packed with an iron-based catalyst is conducted to assess the effects of process parameters on product distribution. The study adopts the alkyl and alkenyl mechanisms in predicting the formation of paraffins and olefins. The effects of the desorbed hydrocarbons on the gaseous flow and reaction kinetics are accounted for in the computational algorithm. The extent of the variation of the syngas molar feed ratio, reactor inlet pressure, and reactor length on paraffin and olefin selectivities and mass flow rates is documented. Three distinct regions of the FT synthesis in the packed tube are documented. In the first region, the polymerization reactions are characterized with the absence of termination reactions that result in chain propagation reactions reaching higher carbon atom numbers with increasing axial length. The beginning of the second region is marked with the initial formation of desorbed species. The second region is characterized initially with chain termination reactions reaching higher carbon atom numbers with increasing axial length. This results in the decrease of the extent of the chain propagation reactions to lower carbon atom numbers, which itself limits the termination reactions to lower carbon atom numbers. This is the only region where liquid olefin and paraffins are formed, as the end of the second region is marked with the propagation reactions not reaching carbon number atoms beyond = 19. In the third region, with the chain propagation reactions keep diminishing to lower carbon atom numbers, the termination reactions themselves decrease to lower carbon atom numbers. This region is characterized with constant gas flow rates, as in the absence of desorbed liquids any decrease in syngas results in the formation of low carbon number gaseous olefins and paraffins.
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