An individual solid oxide cell (SOC) constructed of a sandwich configuration including in the following order: an oxygen electrode, a solid oxide electrolyte, a fuel electrode, a fuel manifold, and at least one layer of mesh. In one embodiment, the mesh supports a reforming catalyst resulting in a solid oxide fuel cell (SOFC) having a reformer embedded therein. The reformer-modified SOFC functions internally to steam reform or partially oxidize a gaseous hydrocarbon, e.g. methane, to a gaseous reformate of hydrogen and carbon monoxide, which is converted in the SOC to water, carbon dioxide, or a mixture thereof, and an electrical current. In another embodiment, an electrical insulator is disposed between the fuel manifold and the mesh resulting in a solid oxide electrolysis cell (SOEC), which functions to electrolyze water and/or carbon dioxide.

The plant control method includes the following. Calculating a first reference amount to be supplied for an amount of hydrogen to be supplied to a second production device (40). Making a decision on whether or not the amount of remaining hydrogen in a storage device (20) at the beginning of a subject term falls within a reference range.

The plant control method includes the following. Calculating a first reference amount to be supplied for an amount of hydrogen to be supplied to a second production device (40). Making a decision on whether or not the amount of remaining hydrogen in a storage device (20) at the beginning of a subject term falls within a reference range.

A wastewater to chemical fuel conversion device is provided that includes a housing having a first chamber and a second chamber, where the first chamber includes a bio-photoanode, where the second chamber includes a photocathode, where a backside of the bio-photoanode abuts a first side of a planatized fluorine doped tin oxide (FTO) glass, where a backside of the photocathode abuts a second side of the FTO glass, where a proton exchange membrane separates the first chamber from the second chamber, where the first chamber includes a wastewater input and a reclaimed water output, where the second chamber includes a solar light input and a H.sub.2 gas output, where the solar light input is disposed for solar light illumination of the first chamber and the second chamber.

A wastewater to chemical fuel conversion device is provided that includes a housing having a first chamber and a second chamber, where the first chamber includes a bio-photoanode, where the second chamber includes a photocathode, where a backside of the bio-photoanode abuts a first side of a planatized fluorine doped tin oxide (FTO) glass, where a backside of the photocathode abuts a second side of the FTO glass, where a proton exchange membrane separates the first chamber from the second chamber, where the first chamber includes a wastewater input and a reclaimed water output, where the second chamber includes a solar light input and a H.sub.2 gas output, where the solar light input is disposed for solar light illumination of the first chamber and the second chamber.

The invention relates to an offshore hydrocarbon production facility arrangement that is to be located on a body of water, which includes a floating hydrocarbon processing unit, a floating renewable electric energy source, and a hydrogen gas source, wherein the floating renewable electric energy source is configured to generate electric energy; the hydrogen gas source is configured to produce hydrogen gas using the electric energy from the floating renewable electric energy source; the floating hydrocarbon processing unit is configured with an electric power generator; the electric power generator is coupled to the hydrogen gas source and is configured for receiving produced hydrogen gas as fuel gas.

Integrated plants and associated processes for producing ammonia and sulfuric acid have been developed comprising air separation and water electrolysis subsystems and which make surprisingly efficient use of the products from these subsystems (i.e. oxygen and nitrogen from the former and hydrogen and oxygen from the latter). The invention is particularly suitable for use as part of an integrated fertilizer production plant.

A device for preparing high-purity hydrogen and/or oxygen by electrolyzing water, including an electrolyzer and a degasser for degassing desalted water. The degasser is located at the upstream of the electrolyzer. After desalted water is heated and degassed in the degasser, the content of gaseous impurities, particularly argon, can be reduced to several ppb (weight ratio). The hydrogen and oxygen generated after the desalted and degassed water is electrolyzed in the electrolyzer also contain an extremely small amount of argon, so that the requirements in semiconductor industry are met. Also involved is a method of preparing high-purity hydrogen and/or oxygen by using the device.

A device for preparing high-purity hydrogen and/or oxygen by electrolyzing water, including an electrolyzer and a degasser for degassing desalted water. The degasser is located at the upstream of the electrolyzer. After desalted water is heated and degassed in the degasser, the content of gaseous impurities, particularly argon, can be reduced to several ppb (weight ratio). The hydrogen and oxygen generated after the desalted and degassed water is electrolyzed in the electrolyzer also contain an extremely small amount of argon, so that the requirements in semiconductor industry are met. Also involved is a method of preparing high-purity hydrogen and/or oxygen by using the device.

A process for preparing a catalytic material of an electrode for electrochemical reduction reactions, said material comprising an active phase based on at least one group VIB metal and an electrically conductive support, which process is carried out according to at least the following steps:

a) bringing water into contact with said electrically conductive support,
b) bringing said wet support into contact with at least one metallic acid hydrate comprising at least one group VIB metal, of which the melting point of said metallic acid hydrate is between 20° C. and 100° C., the weight ratio of said metallic acid to said electrically conductive support being between 0.1 and 4,
c) heating, with stirring, to a temperature between the melting point of said metallic acid hydrate and 100° C.,
d) carrying out a sulfurization step at a temperature of between 100° C. and 600° C.