A process and a related equipment for making ammonia make-up synthesis gas are disclosed, where: a hydrocarbon feedstock is reformed obtaining a raw ammonia make-up syngas stream; said raw syngas is purified in a cryogenic purification section refrigerated by a nitrogen-rich stream produced in an air separation unit; the nitrogen-rich stream at output of said cryogenic section is further used for adjusting the hydrogen/nitrogen ratio of the purified make-up syngas; an oxygen-rich stream is also produced in said air separation unit and is fed to the reforming section.

A method for producing ammonia may be provided. The method may include supplying ammonia synthesis gas to a synthesis gas screw compressor and compressing the synthesis gas. The compressed synthesis gas may be joined with a flow of recycle gas compressed in a recycle gas screw compressor. The compressed combined flow may then be introduced to an ammonia reactor. The ammonia reactor may discharge ammonia, purge gas, and unconverted gas, which may be the recycle gas.

A method for producing hydrogen product having a low carbon intensity is provided. The method includes the steps of: (a) converting a hydrocarbon feedstock to a hydrogen product using a hydrocarbon reforming process; (b) providing at least some of the required energy for the hydrogen production process from a biomass power plant; and (c) processing one or more flue gas streams from the biomass power plant in a carbon capture unit to reduce CO.sub.2e emissions. The hydrogen product has a carbon intensity preferably less than about 1.0 kg CO.sub.2e/kg H.sub.2, more preferably less than 0.45 kg CO.sub.2e/kg H.sub.2, and most preferably less than 0.0 kg CO.sub.2e/kg H.sub.2.

Method for the production of ammonia, and optionally urea, from a flue gas effluent from an oxy-fired process, wherein the production of ammonia and optionally urea includes a net power production. Also provided is a method to effect cooling in an oxy-fired process with air separation unit exit gases utilizing either closed or open cooling loop cycles.

The present invention discloses a method and a process of producing ammonia from methane extracted from methane-hydrate at the site of methane-hydrate extraction. The method and the process comprise coupled chemical reactions. During the first reaction, carbon dioxide reacts methane-hydrate to produce carbon-dioxide-hydrate and methane: carbon dioxide+methane-hydratecarbon-dioxide-hydrate+methane (CO.sub.2+CH.sub.4-hydrateCO.sub.2-hydrate+CH.sub.4). The produced methane is reacted with water to produced carbon dioxide and hydrogen via the second reaction: methane+watercarbon dioxide+hydrogen (CH.sub.4+2H.sub.2OCO.sub.2+4H.sub.2). One embodiment of the second reaction is a combination of the methane steam reforming reaction (CH.sub.4+H.sub.2OCO+3H.sub.2) and the water-gas shift reaction (CO+H.sub.2OCO.sub.2+H.sub.2), both are widely known in the art. The carbon dioxide produced in the second reaction is recycled and used for the first reaction. The hydrogen produced in the second reaction is reacted with nitrogen produced from an air separation process that is known in the art to produce ammonia via the third reaction: nitrogen+hydrogen.fwdarw.ammonia (N.sub.2+3H.sub.2.fwdarw.2NH.sub.3). One embodiment of the third reaction is the well-known Haber-Bosch process. The current invention is related to co-locating the ammonia synthesis at the methane-hydrate extraction sites to minimize the cost of transporting both methane and carbon dioxide over long distances. The process and the associated method also have the advantage of on-site carbon sequestration. The ammonia product produced via the current invention is easily transportable in liquid form from the production sites to the end-use sites as a carbon-free liquid fuel, a fertilizer and a chemical feedstock.

A method is described for revamping an ammonia production facility said ammonia production facility having a front end comprising one or more reformers fed with a hydrocarbon feedstock at a hydrocarbon feed stock feed rate and a high-temperature shift reactor fed with a reformed gas obtained from said one or more reformers and containing a fixed bed of iron-containing water-gas shift catalyst, said front end operating at a first steam- to-carbon ratio and a first pressure drop, said method comprising the steps of (i) replacing the iron-containing water-gas shift catalyst with a low-steam water-gas shift catalyst to form a modified front end, (ii) operating the modified front end at a second steam-to-carbon ratio and a second pressure drop, wherein the second steam-to-carbon ratio is at least 0.2 less than the first steam-to-carbon ratio and the second pressure drop is less than the first pressure drop, and (iii) increasing the hydrocarbon feed stock feed rate to said one or more reformers.

A process for producing an ammonia synthesis gas, said process including the steps of: reforming a hydrocarbon feed in a reforming step thereby obtaining a synthesis gas comprising CH.sub.4, CO, CO.sub.2 , H.sub.2 and H.sub.2O; and shifting said synthesis gas in a high temperature shift step over a promoted zinc-aluminum oxide based high temperature shift catalyst, wherein the steam/carbon ratio in the reforming step is less than 2.6.

A method for producing ammonia may be provided. The method may include supplying ammonia synthesis gas to a synthesis gas screw compressor and compressing the synthesis gas. The compressed synthesis gas may be joined with a flow of recycle gas compressed in a recycle gas screw compressor. The compressed combined flow may then be introduced to an ammonia reactor. The ammonia reactor may discharge ammonia, purge gas, and unconverted gas, which may be the recycle gas.

A process for producing ammonia synthesis gas from a hydrocarbon-containing feedstock, with steps of primary reforming, secondary reforming with an oxidant stream, and further treatment of the synthesis gas including shift, removal of carbon dioxide and methanation, wherein the synthesis gas delivered by secondary reforming is subject to a medium-temperature shift (MTS) at a temperature between 200 and 350.degree. C., and primary reforming is operated with a steam-to-carbon ratio lower than 2. A corresponding method for revamping an ammonia plant is disclosed, where an existing HTS reactor is modified to operate at medium temperature, or replaced with a new MTS reactor, and the steam-to-carbon ratio in the primary reformer is lowered to a value in the range 1-5-2, thus reducing inert steam in the flow rate trough the equipments of the front-end.

The present invention relates to a method for forming a three-dimensional article through successively depositing individual layers of powder material that are fused together so as to form the article, the method comprising the step of heating a first portion of a support surface while depositing a layer of powder material on a second portion of the support surface.