A system and method for conducting high-temperature thermolysis of a waste mixture formed by sewage sludge and wood waste (e.g., creosote-impregnated wooden railway sleepers and utility poles) are proposed. The products of the high-temperature thermolysis may be used to produce thermal energy, electrical energy, carbon black, and liquid fractions which may be used profitably for various purposes.

A process and a plant for producing pure hydrogen by steam reforming of a feed gas containing hydrocarbons, preferably natural gas or naphtha, with reduced carbon dioxide emissions are proposed. The reduction in carbon dioxide emissions is achieved in accordance with the invention in that carbon dioxide is separated both out of a PSA tail gas stream and out of the flue gas from the reformer furnace by means of suitable measures.

Provided is a production facility for liquefied hydrogen and a liquefied natural gas from a natural gas, including: a first heat exchanger configured to cool a hydrogen gas through heat exchange between the hydrogen gas and a mixed refrigerant for liquefying a natural gas containing a plurality of kinds of refrigerants selected from the group consisting of methane, ethane, propane, and nitrogen; a second heat exchanger configured to cool the mixed refrigerant through heat exchange between the mixed refrigerant and propane; and a third heat exchanger configured to cool the hydrogen gas through heat exchange between the hydrogen gas and a refrigerant containing hydrogen or helium, wherein the first heat exchanger has a precooling temperature of from 100 C. to 160 C.

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.

An ethanol engine system stabilizes components of reformed gas generated by a reformer and a calorific value of fuel supplied to an engine. The ethanol engine system includes a reservoir tank for an aqueous ethanol solution, a first supply device that supplies the aqueous ethanol solution to the reformer, a separator that cools mixed gas fed from the reformer, including the reformed gas, condenses water vapor included in the mixed gas and separates into gas and liquid, a reformed gas supply device that supplies the reformed gas separated by the separator to the engine, a recovery tank that collects a recovery solution separated by the separator, and a first recovery solution supply device that supplies the recovery solution in the recovery tank to the reformer or a second recovery solution supply device that supplies the recovery solution in the recovery tank to a combustion chamber of the engine.

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.

A process for the production of a gas stream with a hydrogen concentration equal to or greater than 99.9% utilizing a pressure swing adsorption unit with a main gas stream having at least 70 mol % of hydrogen, wherein a secondary stream, representing less than 20% of the molar flow rate of the main gas stream and having a hydrogen content of less than 25 mol %, is introduced into the main gas stream upstream of the PSA is presented.

A process and apparatus for utilization of an absorption chiller for hydrogen production can include an arrangement configured for providing at least one heated waste stream of fluid from at least one hydrogen production unit to an absorption chiller generator to power the absorption chiller. Coolant can be generated via the heated waste stream for feeding coolant from the generator to an evaporator for cooling a chilling medium to a pre-selected chilling temperature to provide cooling to one or more process elements. The warmed chilling medium can be returned to the absorption chiller evaporator for subsequent cooling back to the pre-selected chilling temperature to provide a closed-circuit cooling arrangement. The waste fluid fed to the generator can be output as a cooled waste fluid for returning to hydrogen production for further use or be output for treatment and/or disposal.

A method of direct reduction of iron (DRI) is disclosed, the method comprising generating metallic iron by removing oxygen from iron ore using a reducing gaseous mixture with excess carbon monoxide that produces an excess CO.sub.2 by-product is provided. CO.sub.2 by-product is optionally sequestered. A system for carrying out the method is also disclosed.

A process and/or system for producing biomethane, hydrogen, or fuel, fuel intermediate, and/or chemical product from the biomethane or hydrogen. The biomethane and/or hydrogen is produced in a process that converts biomass to biomethane. In certain embodiments, the biomethane production process includes anaerobic digestion, which produces biogas and digestate. Carbon-containing material (e.g., derived from the biomass) is stored and/or used as part of at least one carbon capture and storage process, where the carbon-containing material includes (i) carbon dioxide produced from the biomethane production process (e.g., produced from anaerobic digestion), and (ii) carbon-containing material obtained or derived from residue of the biomethane production process, and optionally includes (iii) carbon dioxide produced from the hydrogen production process.