A process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide is disclosed. This is achieved by a process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide, hydrogen and more than 1 ppb of sulfur, using a catalyst comprising aluminum oxide, an Ni active composition and Mn. It has surprisingly The Mn-containing Ni catalyst has a high sulfur resistance and also a high sulfur capacity.

A process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide is disclosed. This is achieved by a process for the methanation of carbon monoxide and/or carbon dioxide in a feed stream containing carbon monoxide and/or carbon dioxide, hydrogen and more than 1 ppb of sulfur, using a catalyst comprising aluminum oxide, an Ni active composition and Mn. It has surprisingly The Mn-containing Ni catalyst has a high sulfur resistance and also a high sulfur capacity.

Disclosed are a Fischer-Tropsch synthesis catalyst, a preparation method therefor and use thereof in a Fischer-Tropsch synthesis reaction. Wherein the catalyst comprises: an active component, being at least one selected from VIIIB transition metals; an optional auxiliary metal; and a nitride carrier having a high specific surface area. The catalyst is characterized in that the active metal is supported on the nitride carrier having the high specific surface, such that the active component in the catalyst is highly dispersed. The catalyst has a high hydrothermal stability, an excellent mechanical wear resistance, a high Fischer-Tropsch synthesis activity and an excellent high-temperature stability.

A catalyst for synthesizing aromatic hydrocarbons, a preparation method thereof and a method for synthesizing aromatic hydrocarbons by using the catalyst. The catalyst comprises acidic molecular sieve particles and zinc-aluminum composite oxide particles. The catalyst has relatively high selectivity to aromatic hydrocarbons, particularly BTX, stable performance, and a long single-pass life.

A method (10) of synthesizing Fischer-Tropsch products (20) includes feeding a synthesis gas (30) to a moving-bed Fischer-Tropsch synthesis reactor (16) containing a Fischer-Tropsch catalyst in a moving catalyst bed and catalytically converting at least a portion of the synthesis gas (30) in the moving catalyst bed to Fischer-Tropsch products (20). The Fischer-Tropsch products (20) are removed from the moving-bed Fischer-Tropsch synthesis reactor (16). The method (10) further includes, while the moving-bed Fisher-Tropsch synthesis reactor (16) is on-line, withdrawing a portion (50) of the Fischer-Tropsch catalyst from the moving-bed Fischer-Tropsch synthesis reactor (16), adding a reactivated Fischer-Tropsch catalyst (57, 58) to the moving-bed Fischer-Tropsch synthesis reactor (16), and adding a fresh Fischer-Tropsch catalyst (60,58), in addition to the reactivated catalyst (57,58), to the moving-bed Fischer-Tropsch synthesis reactor (16).

The present disclosure relates to processes for regenerating catalysts. In certain aspects, a process for regenerating a deactivated catalyst disposed in a first organic material includes removing a substantial portion of the first organic material from the catalyst to provide a dewaxed catalyst having less than about 40 wt % (e.g., less than about 20%) organic material disposed thereon. The dewaxed catalyst is then contacted with a flow of a substantially inert gas at a temperature of at least about 200 C. to provide an inert gas-treated catalyst having less than about 10 wt % organic material disposed thereon. The inert gas-treated catalyst is then contacted with an oxygen-containing gas at a temperature of at least about 200 C. to form an oxidized catalyst (e.g., having less than 2 wt % carbonaceous material disposed thereon). The oxidized catalyst is then contacted with a hydrogen-containing gas at a temperature of at least about 200 C. to form a regenerated catalyst. Finally, the regenerated catalyst can be disposed in a second organic material. The regenerated catalysts can be useful, for example, in Fischer-Tropsch processes.

A system for preventing a catalyst from overheating is provided. The system includes: a first reactor filled with a catalyst at least in part and configured to receive reaction gas and produce product gas; and a second reactor configured to cool a catalyst discharged from the first reactor. The catalyst is circulated between the first reactor and the second reactor by injecting the catalyst cooled in the second reactor into the first rector.

The invention relates to a method for start-up and operation of a Fischer-Tropsch reactor comprising the steps of: (a) providing a reactor with a fixed bed of reduced Fischer-Tropsch catalyst that comprises cobalt as catalytically active metal; (b) supplying a gaseous feed stream comprising carbon monoxide and hydrogen to the reactor, wherein the gaseous feed stream initially comprises a nitrogen-containing compound other than molecular nitrogen in an initial concentration in the range of from 0.1 to 50 ppmv based on the volume of the gaseous feed stream; (c) converting carbon monoxide and hydrogen supplied with the gaseous feed stream to the reactor into hydrocarbons at an initial reaction temperature, wherein the initial reaction temperature is set at a value of at least 200 C. and hydrocarbons are produced at a first yield; (d) maintaining the initial reaction temperature at the set value and maintaining the first yield by decreasing the concentration of the nitrogen-containing compound in the gaseous feed stream supplied to the reactor; (e) optionally increasing the reaction temperature after the concentration of the nitrogen-containing compound in the gaseous feed stream has decreased to a value below 100 ppbv.

The present disclosure relates to processes for regenerating catalysts. In certain aspects, a process for regenerating a deactivated catalyst disposed in a first organic material includes removing a substantial portion of the first organic material from the catalyst to provide a dewaxed catalyst having less than about 40 wt % (e.g., less than about 20%) organic material disposed thereon. The dewaxed catalyst is then contacted with a flow of a substantially inert gas at a temperature of at least about 200 C. to provide an inert gas-treated catalyst having less than about 10 wt % organic material disposed thereon. The inert gas-treated catalyst is then contacted with an oxygen-containing gas at a temperature of at least about 200 C. to form an oxidized catalyst (e.g., having less than 2 wt % carbonaceous material disposed thereon). The oxidized catalyst is then contacted with a hydrogen-containing gas at a temperature of at least about 200 C. to form a regenerated catalyst. Finally, the regenerated catalyst can be disposed in a second organic material. The regenerated catalysts can be useful, for example, in Fischer-Tropsch processes.

The invention relates to a method for start-up and operation of a Fischer-Tropsch reactor comprising the steps of: (a) providing a reactor with a fixed bed of reduced Fischer-Tropsch catalyst that comprises cobalt as catalytically active metal; (b) supplying a gaseous feed stream comprising carbon monoxide and hydrogen to the reactor, wherein the gaseous feed stream initially comprises a nitrogen-containing compound other than molecular nitrogen in an initial concentration in the range of from 0.1 to 50 ppmv based on the volume of the gaseous feed stream; (c) converting carbon monoxide and hydrogen supplied with the gaseous feed stream to the reactor into hydrocarbons at an initial reaction temperature, wherein the initial reaction temperature is set at a value of at least 200 C. and hydrocarbons are produced at a first yield; (d) maintaining the initial reaction temperature at the set value and maintaining the first yield by decreasing the concentration of the nitrogen-containing compound in the gaseous feed stream supplied to the reactor; (e) optionally increasing the reaction temperature after the concentration of the nitrogen-containing compound in the gaseous feed stream has decreased to a value below 100 ppbv.