A method of obtaining purified hydrogen and purified carbon monoxide from crude synthesis gas. A first crude synthesis gas stream is passed through a first separation zone to separate a hydrogen stream from a stream comprising carbon monoxide and methane. The carbon monoxide and methane are subjected to thermal reforming to produce a second crude synthesis gas, which is passed through a second separation zone to separate carbon monoxide from the second crude synthesis gas stream.

The invention includes a gas processing system for transforming a hydrocarbon-containing inflow gas into outflow gas products, where the system includes a gas delivery subsystem, a plasma reaction chamber, and a microwave subsystem, with the gas delivery subsystem in fluid communication with the plasma reaction chamber, so that the gas delivery subsystem directs the hydrocarbon-containing inflow gas into the plasma reaction chamber, and the microwave subsystem directs microwave energy into the plasma reaction chamber to energize the hydrocarbon-containing inflow gas, thereby forming a plasma in the plasma reaction chamber, which plasma effects the transformation of a hydrocarbon in the hydrocarbon-containing inflow gas into the outflow gas products, which comprise acetylene and hydrogen. The invention also includes methods for the use of the gas processing system.

Hydrogen purification devices and their components are disclosed. In some embodiments, the devices may include at least one foil-microscreen assembly disposed between and secured to first and second end frames. The at least one foil-microscreen assembly may include at least one hydrogen-selective membrane and at least one microscreen structure including a non-porous planar sheet having a plurality of apertures forming a plurality of fluid passages. The planar sheet may include generally opposed planar surfaces configured to provide support to the permeate side. The plurality of fluid passages may extend between the opposed surfaces. The at least one hydrogen-selective membrane may be metallurgically bonded to the at least one microscreen structure.

A method of integrating a fuel cell with a steam methane reformer is provided. The system includes at least one fuel cell including an anode and a cathode, and a steam methane reformer including a syngas stream, and a flue gas stream. The method includes introducing at least a portion of the flue gas stream to the cathode, thereby producing a CO2 depleted flue gas stream and introducing a hydrocarbon containing stream to the anode, thereby producing an electrical energy output and a carbon dioxide and hydrogen containing stream from the fuel cell.

A plant and process for producing a hydrogen rich gas are provided, said process comprising 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; shifting said synthesis gas in a shift configuration including a high temperature shift step; removal of CO.sub.2 upstream hydrogen purification unit, such as a pressure swing adsorption unit (PSA), and recycling off-gas from hydrogen purification unit and mix it with natural gas upstream prereformer feed preheater, prereformer, reformer feed preheater or ATR or shift as feed for the process.

Provided is a fuel-reforming device comprising: an ammonia tank (4); a reformer (5) for reforming ammonia and generating high-concentration hydrogen gas having a hydrogen content of at least 99%; a mixing tank (7) for mixing ammonia and hydrogen for temporary storage; and a control means (10) for controlling the respective supply amounts of ammonia and high-concentration hydrogen gas that are supplied to the mixing tank (7). The control means (10) calculates the combustion rate coefficient C of mixed gas with respect to a reference fuel on the basis of equation (1). Equation (1): S.sub.0=S.sub.H×C+S.sub.A×(1−C). In equation (1), S.sub.0 is the combustion rate of the reference fuel, S.sub.H is the combustion rate of hydrogen, S.sub.A is the combustion rate of ammonia, and C is the combustion rate coefficient of mixed gas. In addition, on the basis of equation (2), the control means (10) determines the volume fractions of ammonia and hydrogen that are supplied to the mixing tank. Equation (2): C=1−exp(−A×M.sub.B). In equation (2), M is the volume fraction of hydrogen in mixed gas, and A and B are constants.

The treatment plant comprises: a reactor for the sublimation of organic material in order to obtain a syngas; a filtration assembly for filtering the syngas in order to obtain a filtered gas, and a motor-generator assembly for producing electrical energy by means of the combustion of the filtered gas and thereby producing burnt gas; characterized in that said plant also comprises a methanation assembly, comprising: a catalyst that can extract carbon dioxide and nitrogen from the burnt gas; an electrolyzer that can separate water into oxygen and hydrogen by means of electrolysis; and a methanation reactor, which can produce methane by means of the Sabatier reaction using hydrogen and carbon dioxide originating from the electrolyzer and from the catalyst; the catalyst comprising a catalysis layer consisting of stone wool and nickel nanospheres, a plurality of steel microtubes containing copper microfilaments, and a system for controlling the reaction conditions.

The present invention relates to a separation and recovery system and method of hydrogen from a coke oven gas (COG) in a steel industry, and more particularly, to a separation and recovery system and method of hydrogen from a coke oven gas (COG) in a steel industry, the system including a pre-processing unit removing impurities including tar, moisture, oil, hydrogen sulfide, and dusts from the coke oven gas (COG), a membrane separation unit including a polymer separation membrane module to generate a hydrogen concentrated gas stream by membrane-separating the coke oven gas (COG) processed in the pre-processing unit, and an adsorption unit separate and recover the hydrogen by allowing the hydrogen concentrated gas stream to contact an absorbent.

A hydrogen production system including a steam reformer unit, a steam addition line arranged to add steam upstream the steam reformer unit, a hydrogen membrane unit comprising a hydrogen permeable membrane and being arranged to allow at least a part of a reformed stream and a hydrocarbon feed stream to pass on different sides of a hydrogen permeable membrane, so that hydrogen passes from the reformed stream into the hydrocarbon feed stream, thereby forming said hydrogen enriched hydrocarbon stream, and a separation unit downstream the first side of the hydrogen membrane unit, where the separation unit is arranged to separating the reformed stream exiting the first side of the hydrogen membrane unit into a hydrogen product gas and an off-gas.

Through the procedures of pretreatment, temperature swing adsorption (TSA) coarse desorption, pressure swing adsorption (PSA) purification and hydrogen purification, the hydrogenous waste gas from various procedures in the manufacturing process of semiconductor (especially silicon wafer), including the off-gas from chemical vapor deposition (CVD), doping (diffusion and ion implantation), photolithography and cleaning, the combusted and washed discharged gas of the off-gas in other procedures after field treatment and centralized treatment, or the hydrogenous waste gas entering the hydrogen discharge system are purified to meet the standard for the electronic grade hydrogen required for the manufacturing process of semiconductor, the recycling of hydrogen resources is realized, and the yield of hydrogen is greater than or equal to 70-85%. The present invention solves the technical difficulty the normal-pressure waste hydrogen recovered in the manufacturing process of semiconductor can't be returned to the manufacturing process of semiconductor for reuse.