A system and method for producing olefin via dry reforming and olefin synthesis in the same vessel, including providing feed including methane and carbon dioxide to the vessel, converting methane and carbon dioxide in the vessel into syngas (that includes hydrogen and carbon monoxide) via dry reforming in the vessel, and cooling the syngas via a heat exchanger in the vessel. The method includes synthesizing olefin from the syngas in the vessel, wherein the olefin includes ethylene, propylene, or butene, or any combinations thereof.

The invention relates to a cyclic method of producing a hydrogen rich and/or a carbon monoxide rich stream using different materials, a first solid material, a second solid material and a CO.sub.2 sorbent material.

In a first step a first gas stream comprising steam and at least one reductant is brought in contact with the three materials resulting in a hydrogen rich outlet stream.

In a second step, the captured CO.sub.2 from the first step is released and converted to CO to produce a CO rich outlet stream.

The invention further relates to an installation for producing a hydrogen rich and/or carbon monoxide rich stream.

A method for producing phosphorus in which a reaction for forming gaseous phosphorus (g) by bringing phosphorus oxide generated by heating a liquid phosphoric acid compound into contact with a carbon material to reduce the phosphorus oxide and for condensing the gaseous phosphorus (g) to obtain liquid phosphorus (L) is conducted by a flow reaction with a nonoxidizing gas flow, wherein the reduction reaction of the phosphorus oxide is conducted in a carbon material-packed bed, and the condensation of the formed gaseous phosphorus (g) is substantially conducted in a condensation accelerator-packed bed which is disposed downstream of the carbon material-packed bed in contact with the carbon material-packed bed.

A process for estimating catalyst performance of catalyst used in refinery reforming processes for converting naphtha to gasoline. More in particular, the catalyst to be investigated is subjected to analysis in parallel over time at a temperature to achieve a desired RON on yield of e.g. C5+, for at least two different reaction times. The reactions are terminated after which coke deposition is determined, and relationships of coke deposition and yield, both as a function of reaction temperature for the catalyst used are established, thereby enabling comparison of catalyst performance as determined by a yield-temperature relationship at a given coke deposition degree.

A hybrid dehydrogenation reaction system includes: an acid aqueous solution tank having an acid aqueous solution; an exothermic dehydrogenation reactor including a chemical hydride of a solid state and receiving the acid aqueous solution from the acid aqueous solution tank for an exothermic dehydrogenation reaction of the chemical hydride and the acid aqueous solution to generate hydrogen; an LOHC tank including a liquid organic hydrogen carrier (LOHC); and an endothermic dehydrogenation reactor receiving the liquid organic hydrogen carrier from the LOHC tank and generating hydrogen through an endothermic dehydrogenation reaction of the liquid organic hydrogen carrier by using heat generated from the exothermic dehydrogenation reactor.

A burner combustion chamber (3), a burner (7) for performing a burner combustion in the burner combustion chamber (3) a reformer catalyst (4) to which burner combustion gas is fed, and a heat exchange part (13a) for heating the air fed to the burner (7) are provided. A switching device (16, 17) able to switch an air flow route for introducing the outside air to the burner (7) between a high temperature air flow route (13) for introducing the outside air flowing within the heat exchange part (13a) and heated at the heat exchange part(13a) to the burner (7) and a low temperature air flow route (14) for feeding the outside air, which does not flow within the heat exchange part (13a) and thereby is lower in temperature than the outside air heated at the heat exchange part (13a), to the burner (7) is provided.

A catalytic reaction analysis dual reactor system and a method for measuring the catalytic activity of a catalyst by correcting for non-catalytic effects with the catalytic reaction analysis dual reactor system. The dual reactor system contains a first reactor comprising a first catalyst on a first catalyst support, and a second reactor comprising a second catalyst support, wherein the particle size and amount of the first catalyst and the second catalyst support are substantially the same, and the effect of the catalyst is isolated by correcting the result obtained from the first reactor containing the catalyst with the result obtained from the second reactor containing the catalyst support.

A system for distribution of hydrogen gas in a metal hydride reactor is disclosed. The system comprises a hydrogen distribution conduit positioned within a metal tube so as to define an annular space between the hydrogen distribution conduit and the outer metal tube. The hydrogen distribution conduit provides a flow passage for the hydrogen gas. A metal sponge matrix containing hydrogen-storing metal powder or hydrogen-storing alloy powder is filled in the annular space. The system provides a more uniform distribution of hydrogen across the particles of the hydrogen-storing metal/alloy powder, provides mechanical support to the hydrogen distribution conduit, improves the thermal conductivity of the powdered metal/alloy bed and reduces the size and production cost of the reactor.

A multi-stage process for the production of an ISO 8217 compliant Product Heavy Marine Fuel Oil from ISO 8217 compliant Feedstock Heavy Marine Fuel Oil involving a Reaction System composed of one or more reactor vessels selected from a group reactor wherein said one or more reactor vessels contains one or more reaction sections configured to promote the transformation of the Feedstock Heavy Marine Fuel Oil to the Product Heavy Marine Fuel Oil. The Product Heavy Marine Fuel Oil has a Environmental Contaminate level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process for conducting the process is disclosed that can utilize a modular reactor vessel.

The present invention relates to the formation of silazane coatings. The invention provides a polysilazane coating method for limiting fragmentation of polysilazane and an assembly for performing said polysilazane coating method for limiting fragmentation of polysilazane.