There is provided a hydrocarbon producing apparatus according to the present invention for obtaining a product containing hydrocarbons from a raw material gas by a Fischer-Tropsch synthesis reaction using a reactor containing an FT reaction catalyst exhibiting activity in the FT synthesis reaction, the hydrocarbon producing apparatus including: a purge unit that executes an inert gas purge process that supplies a high-temperature inert gas to the reactor, maintains a temperature in the reactor in a temperature range during the FT synthesis reaction, and reduces a pressure in the reactor, when the FT synthesis reaction is terminated, so that the hydrocarbons adhering to the FT reaction catalyst are vaporized; and a recovery unit that is provided on a downstream side of the reactor, condenses the vaporized hydrocarbons, and recovers the condensed hydrocarbons in a liquid state.

A process and system for integrating a steam cracking unit with a blue hydrogen unit in which a methane-rich gas stream, a hydrogen-rich gas stream, or both from the steam cracking unit are fed to the blue hydrogen unit and a high purity hydrogen gas stream from the blue hydrogen unit is directed to the steam cracking unit.

A Fischer-Tropsch synthesis process (10) includes feeding gaseous reactants (20) including at least CO, H.sub.2 and CO.sub.2into a reactor (14) holding an iron-based catalyst. The H.sub.2 and CO are fed in a H.sub.2:CO molar ratio of at least 2:1 and the CO.sub.2 and CO are fed in a CO.sub.2:CO molar ratio of at least 0.5:1. The reactor (14) is controlled at an operating temperature in the range from about 260 C. to about 300 C. A liquid product (22) and a gaseous product (24) including hydrocarbons, CO, H.sub.2, water and CO.sub.2 are withdrawn from the reactor (14).

In various aspects, systems and methods are provided for operating an oxygen-fired catalyst regenerator with flue gas recycle and CO.sub.2 capture. An oxygen-fired catalyst regenerator contrasts with an air-fired regenerator. The oxygen-fired catalyst regenerator substantially reduces nitrogen within the system, which facilitates CO.sub.2 capture by reducing the energy required to capture CO.sub.2. In various aspects, a first portion of the regenerator flue gas is passed to a CO.sub.2 capture system and a second portion is recycled to the regenerator. Before the flue gas is recycled or diverted to the CO.sub.2 capture, it is passed to various processes that remove and/or reduce SO.sub.x, NO.sub.x, particulate, and water content. In various aspects, a portion of the treated flue gas may be combined with substantially pure O.sub.2 and recycled to the regenerator.

An integrated plant for the conversion of a hydrocarbon gas such as natural gas to useful hydrocarbon liquid fuels and feed-stocks comprises an H2+CO syn-gas generation system which provides feed gas to a Fischer-Tropsch catalytic hydrocarbon synthesis system with an associated power and heat energy system.

A method of converting carbon containing compounds such as coal, methane or other hydrocarbons into a liquid hydrocarbon fuel utilizes a high pressure, high temperature reactor which operates upon a blend of a carbon compound including CO.sub.2 and a carbon source, a catalyst, and steam. Microwave power is directed into the reactor. The catalyst, preferably magnetite, will act as a heating media for the microwave power and the temperature of the reactor will rise to a level to efficiently convert the carbon and steam into hydrogen and carbon monoxide.

The present invention relates to a method of subjecting a biomass feedstock to hydropyrolysis, the method at least comprising the steps of: a) supplying a biomass feedstock and a fluidizing gas comprising hydrogen to a bulk reactor zone of a fluidized bed reactor containing a deoxygenating catalyst; b) subjecting the biomass feedstock in the bulk reactor zone of the fluidized bed reactor to a hydropyrolysis reaction by contacting the biomass feedstock with the deoxygenating catalyst in the presence of the fluidizing gas, thereby obtaining a hydropyrolysis reactor output comprising at least one non-condensable gas, a partially deoxygenated hydropyrolysis product and char; wherein the bulk reactor zone is cooled by means of a cooling fluid flowing through a plurality of tubes running through the bulk reactor zone, the plurality of tubes having inlets into and outlets from the bulk reactor zone; and wherein the cooling fluid flowing in the tubes at the point (A) where the biomass feedstock enters the bulk reactor zone has a temperature of at least 320 C., preferably at least 340 C., more preferably at least 350 C., even more preferably at least 370 C., yet even more preferably at least 380 C.

A cracking furnace system for converting a hydrocarbon feedstock into cracked gas includes a convection section, a radiant section and a cooling section. The convection section includes a plurality of convection banks configured to receive only a hydrocarbon feedstock and a diluent. The radiant section includes a firebox comprising at least oxygen or oxygen enriched air burners and several radiant coils configured to heat up the feedstock to a temperature allowing a pyrolysis reaction. The cooling section includes at least two transfer line exchangers (TLE), a primary transfer line exchanger (PTLE) and a secondary transfer line exchanger (STLE).

The present disclosure identifies methods and compositions for modifying photoautotrophic organisms as hosts, such that the organisms efficiently convert carbon dioxide and light into n-alkanes, and in particular the use of such organisms for the commercial production of n-alkanes and related molecules.

A Fischer-Tropsch synthesis process (10) includes feeding gaseous reactants (20) including at least CO, H.sub.2 and C0.sub.2 into a reactor (14) holding an iron-based catalyst. The H.sub.2 and CO are fed in a H.sub.2:CO molar ratio of at least 2:1 and the C0.sub.2 and CO are fed in a C0.sub.2:CO molar ratio of at least 0.5:1. The reactor (14) is controlled at an operating temperature in the range from about 260 C. to about 300 C. A liquid product (22) and a gaseous product (24) including hydrocarbons, CO, H.sub.2, water and C0.sub.2 are withdrawn from the reactor (14).