Disclosed herein is a method and a reactor for the conversion of a hydrocarbon gas to syngas. The method and reactor utilizes a oxy-hydrogen flame to partially oxidize hydrocarbon gas to syngas by provide an excess flow of oxygen gas. The oxy-hydrogen flame is generated by a multi-tubular oxy-hydrogen burner.

An autothermal reforming catalytic structure for generating hydrogen gas from liquid hydrocarbons, steam and an oxygen source. The autothermal reforming catalytic structure includes a support structure and nanosized mixed metal oxide particles dispersed homogenously throughout the support structure.

A process and apparatus are provided for gasification of a carbonaceous material. The process produces a raw syngas that can be further processed in a tar destruction zone to provide a hot syngas. The process includes contacting said carbonaceous material with molecular oxygen-containing gas in a gasification zone to gasify a portion of said carbonaceous material and to produce a first gaseous product. A remaining portion of the carbonaceous material is contacted with molecular oxygen-containing gas in a burn-up zone to gasify additional portion of the carbonaceous material and to produce a second gaseous product and a solid ash. The first gaseous product and said second gaseous product are combined to produce a raw syngas that includes carbon monoxide (CO), carbon dioxide (CO.sub.2) and tar. The raw syngas is contacted with molecular oxygen containing gas in a tar destruction zone to produce said hot syngas.

A method for upgrading a hydrocarbon feed gas to methanol, including the steps of: providing a hydrocarbon feed gas; optionally, purifying the hydrocarbon feed gas in a gas purification unit; optionally, prereforming the hydrocarbon feed gas together with a steam feedstock in a prereforming unit; carrying out steam methane reforming in a reforming reactor heated by means of an electrical power source; providing the synthesis gas to a methanol synthesis unit to provide a product including methanol and an off-gas. Also, a system for upgrading a hydrocarbon feed gas to methanol.

A process and apparatus for producing a hydrogen-enriched product and recovering CO.sub.2 from an effluent stream from a hydrogen production process unit are described. The process utilizes a CO.sub.2 recovery system integrated with a PSA system that produces at least two product streams to recover additional hydrogen and CO.sub.2 from the tail gas stream of a hydrogen PSA unit in the hydrogen production process.

A process and apparatus for producing a hydrogen-enriched product and recovering CO.sub.2 from an effluent stream from a hydrogen production unit are described. The effluent from the hydrogen production unit, which comprises a mixture of gases comprising hydrogen, carbon dioxide, water, and at least one of methane, carbon monoxide, nitrogen, and argon, is sent to a PSA system that produces at least two product streams for separation. The PSA system that produces at least two product streams separates the gas mixture into a high-pressure hydrogen stream enriched in hydrogen, optionally a second gas stream containing the majority of the impurities, and a low-pressure tail gas stream enriched in CO.sub.2 and some impurities. The CO.sub.2-rich tail gas stream is compressed and sent to a CO.sub.2 recovery unit, where a CO.sub.2-enriched stream is recovered. The CO.sub.2-depleted overhead gas stream is recycled to the PSA system that produces at least two product streams.

A bio-renewable conversion process for making fuel from bio-renewable feedstocks is combined with a hydrogen production process that includes recovery of CO.sub.2. The integrated process uses a purge gas stream comprising hydrogen from the bio-renewable hydrocarbon production process in the hydrogen production process.

A three-product PSA system which produces three product streams from a feed gas mixture comprising a light key component, at least one heavy key component, and at least one intermediate key component is described. The three-product PSA system produces a high pressure product stream enriched in the light key component, a low pressure tail gas stream enriched in the at least one heavy key component, and an intermediate pressure vent gas stream enriched in the at least one intermediate key component.

A process for the production of ammonia and urea in an ammonia-urea integrated plant comprising an ammonia section and a tied-in urea section, wherein a hydrocarbon is reformed to produce ammonia make-up synthesis gas; said make-up gas is purified by shift conversion and removal of carbon dioxide; carbon dioxide is removed from the make-up gas by a first and a second CO2 removal sections; the first section removes CO2 by absorption with a suitable medium, and the second section removes CO2 by washing with a carbamate solution taken from the urea section; the make-up gas is reacted to produce ammonia; the CO2 removed from the make-up gas and at least part of the ammonia are used to produce urea.

The present disclosure relates to a reactor and a method of operation for an exothermal process being catalyzed by a catalytically active material receiving a reactant gas and providing a product gas, in which said exothermal process has a heat development having a potential for thermally degrading said catalytically active material, and which exothermal process operates at a temperature at which the reactants and at least 80% or all of the products are present as gases, said method comprising the steps of a) directing the reactant gas to a first zone of a material catalytically active in the exothermal process producing an first product gas, and b) directing the first product gas to a second zone of a material catalytically active in the exothermal process producing a product gas, with the option of fully or partially by-passing either said first zone or said second zone, while directing a non-condensing gas stream having a temperature at least 50° C. lower than the product gas to said by-passed zone, wherein the choice of by-passing said zone is made based on the time of operation or a process parameter reflecting the catalytic activity of the zone of catalytically active material which is not by-passed with the associated benefit of reducing the extent of thermal deactivation of the catalytically active material, and thus increasing the overall lifetime of the catalytically active material.