The Fischer-Tropsch process can be used for the conversion of hydrocarbonaceous feed stocks into normally liquid and/or solid hydrocarbons (i.e. measured at 0 C., 1 bar). The feed stock (e.g. natural gas, associated gas, coal-bed methane, residual oil fractions, biomass and/or coal) is converted in a first step into a mixture of hydrogen and carbon monoxide. This mixture is often referred to as synthesis gas or syngas. The present invention relates to process for preparing a paraffin product from a carbonaceous feedstock and a system for preparing a paraffin product from a carbonaceous feedstock.

The present technology is directed to processes for conversion of synthesis gas in a tubular reactor to produce a synthetic product that utilizes high activity carbon monoxide hydrogenation catalysts and a heat transfer structure that surprisingly provides for higher per pass conversion with high selectivity for the desired synthetic product without thermal runaway.

The present application relates to a process for producing normally gaseous, normally liquid, and optionally normally solid hydrocarbons from synthesis gas in a three-phase reactor, said reactor comprising a top middle and bottom part wherein the bottom and top part are fluidly connected via one or more reactor tubes, wherein one or more reactor tubes comprise randomly stacked catalyst bodies held stationary in the reactor tube and the reactor is at least partially filled with a liquid medium, said process comprising the steps of: (i) introducing the synthesis gas into the reactor via the bottom part; and (ii) contacting the synthesis gas with a stationary catalyst to catalytically convert the synthesis gas at an elevated temperature to obtain the normally gaseous, normally liquid, and optionally normally solid hydrocarbons from synthesis gas; (iii) withdrawing the normally gaseous, normally liquid, and optionally normally solid hydrocarbons; wherein the catalyst bodies have an open celled foam structure.

The Fischer-Tropsch process can be used for the conversion of hydrocarbonaceous feed stocks into normally liquid and/or solid hydrocarbons. The feed stock (e.g. natural gas, associated gas and/or coal-bed methane, coal) is converted in a first step into a mixture of hydrogen and carbon monoxide (this mixture is often referred to as synthesis gas or syngas). The synthesis gas (or syngas) is then converted in one or more steps over a suitable catalyst at elevated temperature and pressure into paraffinic compounds ranging from methane to high molecular weight molecules comprising up to 200 carbon atoms, or, under particular circumstances, even more. The present invention relates to a catalyst, a method for manufacturing said catalyst. The present invention further relates to a catalyst obtainable by said method. The present invention further relates to a multi tubular reactor comprising said catalyst.

The invention provides methods of making laminated devices (especially microchannel devices) in which plates are assembled and welded together. Unlike conventional microchannel devices, the inventive laminated devices can be made without brazing or diffusion bonding; thus providing significant advantages for manufacturing. Features such as expansion joints and external welded supports are also described. Laminated devices and methods of conducting unit operations in laminated devices are also described.

The disclosed invention relates to a method for restarting a synthesis gas conversion process which has stopped. The synthesis gas conversion process may be conducted in a conventional reactor or a microchannel reactor. The synthesis gas conversion process may comprise a process for converting synthesis gas to methane, methanol or dimethyl ether. The synthesis gas conversion process may be a Fischer-Tropsch process.

The Fischer-Tropsch process can be used for the conversion of hydrocarbonaceous feed stocks into normally liquid and/or solid hydrocarbons (i.e. measured at 0 C., 1 bar). The feed stock (e.g. natural gas, associated gas, coal-bed methane, residual oil fractions, biomass and/or coal) is converted in a first step into a mixture of hydrogen and carbon monoxide. This mixture is often referred to as synthesis gas or syngas. The present invention relates to process for preparing a paraffin product from a carbonaceous feedstock and a system for preparing a paraffin product from a carbonaceous feedstock.

The present invention relates to a process for treating a catalyst to improve performance, and more specifically to a process for treating a Fischer-Tropsch catalyst using a high hydrogen syngas to improve catalyst performance.

The disclosure deals with a slurry bubble column reactor for converting a gas mixture comprising carbon monoxide and hydrogen into liquid hydrocarbons. The slurry bubble column reactor features a slurry bed of catalyst particles, an inlet conduit for feeding the gas mixture into the slurry bed, a filtration zone for separating the liquid hydrocarbons from the catalyst particles and a liquid outlet conduit for withdrawing the separated hydrocarbons from the filtration zone. The filtration zone is situated in the slurry bubble column reactor such that the slurry bed is found in a first and a second heat exchange zone with the filtration zone arranged between the first and the second heat exchange zone.

Disclosed herein are reactors comprising: a) a first mixing zone, b) a first reaction zone, c) a first cooling zone, d) a first H.sub.2O separation zone, e) a second mixing zone, f) a second reaction zone, g) a second cooling zone, and h) a second H.sub.2O separation zone, wherein the first mixing zone is in fluid communication with the first reaction zone, wherein the first reaction zone is in fluid communication with the first cooling zone, wherein the first cooling zone is in fluid communication with the first H.sub.2O separation zone, wherein the first H.sub.2O separation zone is in fluid communication with the second mixing zone, wherein the second mixing zone is in fluid communication with the second reaction zone, wherein the second reaction zone is in fluid communication with the second cooling zone, and wherein the second cooling zone is in fluid communication with the second H.sub.2O separation zone.