Abstract: A catalyst in a calcined state has a specific surface area of 20-50 m2/g of catalyst, and a specific surface area of nickel metal after reduction of the catalyst of 8 to 11 m2/g, wherein the average particle size of nickel metal is 3-8 nm, the dispersion of the particles is 10-16%, and the content of nickel is 5-15 wt. % based on the weight of calcined catalyst. A support has a specific surface area of 40-120 m2/g with a pore volume of the support of 0.2-0.4 cm3/g, wherein the support is selected from a mixture of zirconium oxide and cerium oxide or magnesium oxide, cerium oxide and the ballast being zirconium oxide. The catalyst further contains a promoter selected from the group consisting of palladium and ruthenium, in an amount of from 0.01 to 0.5 wt. %.

Abstract: The invention relates to Fischer-Tropsch synthesis in a compact version. A compact reactor comprises a housing, rectangular reaction channels inside the housing, which are filled with a cobalt catalyst, synthesis gas injection nozzles in the number determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, an input and output nozzle for heat transfer medium on which a pressure controller installed, and an assembly for withdrawing synthetic hydrocarbons. The cobalt catalyst is activated by passing hydrogen through it. Synthetic hydrocarbons are produced by passing synthesis gas through the reaction channels filled with the activated cobalt catalyst. The space velocity of synthesis gas is increased every 300-500 h, followed by returning to the initial process conditions. This provides a high-molecular-weight hydrocarbon output per unit mass of the reactor.

Abstract: The invention relates to Fischer-Tropsch synthesis in a compact version. A compact reactor comprises a housing, rectangular reaction channels inside the housing, which are filled with a cobalt catalyst, synthesis gas injection nozzles in the number determined by the ratio of the number of channels to the number of synthesis gas injection nozzles, an input and output nozzle for heat transfer medium on which a pressure controller installed, and an assembly for withdrawing synthetic hydrocarbons. The cobalt catalyst is activated by passing hydrogen through it. Synthetic hydrocarbons are produced by passing synthesis gas through the reaction channels filled with the activated cobalt catalyst. The space velocity of synthesis gas is increased every 300-500 h, followed by returning to the initial process conditions. This provides a high-molecular-weight hydrocarbon output per unit mass of the reactor.

Abstract: A catalyst in a calcined state has a specific surface area of 20-50 m2/g of catalyst, and a specific surface area of nickel metal after reduction of the catalyst of 8 to 11 m2/g, wherein the average particle size of nickel metal is 3-8 nm, the dispersion of the particles is 10-16%, and the content of nickel is 5-15 wt. % based on the weight of calcined catalyst. A support has a specific surface area of 40-120 m2/g with a pore volume of the support of 0.2-0.4 cm3/g, wherein the support is selected from a mixture of zirconium oxide and cerium oxide or magnesium oxide, cerium oxide and the ballast being zirconium oxide. The catalyst further contains a promoter selected from the group consisting of palladium and ruthenium, in an amount of from 0.01 to 0.5 wt. %.