An ammonia decomposition apparatus comprises a casing, a heating zone, a heat exchange zone, a reaction section and a heat exchange coil. The heat exchange coil is spirally wound on an outer wall of the reaction section to efficiently heat ammonia gas. The reaction section has a first reaction zone and a second reaction zone communicated successively, the ammonia gas decomposed into a nitrogen-hydrogen mixture after entering the first reaction zone, with the second reaction zone decomposing for the second time the residual ammonia gas in the nitrogen-hydrogen mixture produced in the first reaction zone, so that the ammonia gas is decomposed more thoroughly. The conversion rate of ammonia gas can reach 99.9% or more, and the residual amount of ammonia gas in the nitrogen-hydrogen mixture can be less than 1000 ppm.

A multi-tubular chemical reactor includes an igniter for the initiation of gas phase exothermic reaction within the gas phase reaction zones of the tubular reactor units.

An olefin and methanol co-production plant for co-production of an olefin and methanol from a source gas containing methane includes: an olefin production unit for producing the olefin; and a methanol production unit for producing methanol from a carbon oxide gas in the olefin production unit. The olefin production unit includes a partial oxidative coupling device for producing the olefin by partial oxidative coupling reaction of methane contained in the source gas. The methanol production unit includes a reforming device for producing hydrogen by reforming reaction of methane, and a methanol production device for producing methanol by reaction with hydrogen produced by the reforming device. At least one of the reforming device or the methanol production device is configured to perform reaction using the carbon oxide gas in the olefin production unit.

Described herein is an improved conversion of nitrous oxide (N.sub.2O) present as a by-product in a chemical process to NO.sub.x which can be further converted to a useful compound or material, such as nitric acid.

Described herein is an improved conversion of nitrous oxide (N.sub.2O) present as a by-product in a chemical process to NO.sub.x which can be further converted to a useful compound or material, such as nitric acid.

The present invention provides materials for improving the ignition of gaseous reactants in metal catalyzed oxidation reactions comprising a metal catalyst gauze, preferably, a platinum/rhodium catalyst gauze, having in contact therewith, from 0.5 to 1.5 wt. %, based on the weight of the metal catalyst gauze, of one or more pieces of previously used metal catalyst gauze. Further, methods of making the metal catalyst materials comprise shaping the pieces of previously used metal catalyst gauze and placing them equidistant from each other in contact with or on the surface of the metal catalyst gauze. And methods of using the materials comprise feeding into the reactor a gas mixture of oxygen or air and one or more reactant gases, and igniting the gas mixture at the surface of one or more or all of the pieces of previously used metal catalyst.

A gas production device and a gas production system capable of continuously and stably manufacturing a produced gas containing carbon monoxide from a raw material gas containing carbon dioxide are provided. A gas production device 1 manufactures a produced gas containing carbon monoxide by bringing a raw material gas containing carbon dioxide into contact with a reducing agent containing a metal oxide that reduces the carbon dioxide. The gas production device 1 includes a connecting portion 2 that supplies the raw material gas, a reducing gas supply section 3 that supplies a reducing gas for reducing the reducing agent oxidized by contact with the carbon dioxide, a reaction section 4 that includes a plurality of reactors 4a and 4b to which the connecting portion 2 and the reducing gas supply section 3 are respectively connected, and a reducing agent arranged in the reactors 4a and 4b, and that is capable of switching between the raw material gas and the reducing gas to be supplied to the respective reactors 4a and 4b, a gas merging section J4 that merges gases after passing through the reactors 4a and 4b to produce a mixed gas, an exhaust gas heating section 10 that heats the exhaust gas before being supplied to the reactors 4a and 4b, and a reducing gas heating section 11 that heats the reducing gas before being supplied to the reactors 4a and 4b.

Process for the production of a product gas containing nitrogen and hydrogen from ammonia comprising the steps of non-catalytic partial oxidation of ammonia with an oxygen containing gas to a process gas containing nitrogen, water, amounts of nitrogen oxides and residual amounts of ammonia; cracking of at least a part of the residual amounts of ammonia to hydrogen and nitrogen in the process gas by contact with a nickel containing catalyst and simultaneously reducing the amounts of nitrogen oxides to nitrogen and water by reaction with a part of the hydrogen formed during cracking of the process gas by contact of the process gas with the nickel containing catalyst; and withdrawing the hydrogen and nitrogen containing product gas.

The invention is directed to a furnace suited for oxidation of a gaseous starting mixture comprising one or more sulphur compounds to obtain an oxidized gas mixture and reduction of the oxidized gas mixture to obtain a gaseous mixture of reduced sulphur compounds comprising an interior furnace space, an inlet conduit for the gaseous starting mixture, an inlet for supply of an oxygen comprising gas, a ceramic comprising outlet conduit provided with an inlet opening for the mixture of reduced sulphur compounds, an inlet for hydrogen and heating means, wherein the inlet opening of the outlet conduit is comprised of more than one opening which openings fluidly connect the interior furnace space and the interior of the outlet conduit.

In a method for producing hydrogen cyanide by passing a feed mixture comprising ammonia and methane through reaction tubes, coated on the inner surface with a catalyst comprising platinum, at a reaction temperature of 1000 C. to 1400 C., operated for a time period of at least 100 h, the concentration difference between the ammonia concentration and the methane concentration in the product gas mixture is maintained in a range of from 1.05 % by volume to 3.0% by volume for at least 80% of the time.