Abstract: A process for converting carbon dioxide and hydrogen into a product stream comprising carbon monoxide, water and hydrogen by introducing carbon dioxide, hydrogen and oxygen into a reaction vessel, and performing a reverse water gas shift reaction at elevated temperature, wherein (a) no catalyst is present in vessel (b) gas stream comprising carbon dioxide, a hydrogen and an oxygen rich gas stream are introduced into the vessel in separate feed streams, (c) the hydrogen and oxygen rich gas stream being introduced in close vicinity of each other, via burner comprising coaxial channels wherein gases undergo a combustion reaction, providing the heating energy required for the reverse water-gas shift reaction; and (d) the temperature in vessel is in the range of 1000 to 1500° C. by varying the molar ratio of hydrogen to oxygen. It is useful in reducing the carbon footprint of certain industrial technologies, and in production of synthesis gas.

Abstract: The present invention relates to a method for the production of hydrogen. Hydrogen is used in many different chemical and industrial processes. Hydrogen is also an important fuel for future transportation and other uses as it does not generate any carbon dioxide emissions when used. The invention provides for a process for producing hydrogen comprising the steps of partially oxidizing a hydrocarbon to obtain a synthesis gas, providing the synthesis gas to a reactor in which carbon monoxide is converted to carbon dioxide, removing the carbon dioxide to obtain hydrogen. The carbon dioxide is used in a chemical process and/or stored in a geological reservoir.

Abstract: The present invention relates to a process for converting feed streams selected from (1) a gas stream comprising carbon dioxide and a hydrogen rich gas stream; (2) a methane rich gas stream; and (3) a combination of feed streams (1) and (2) into a product stream comprising carbon monoxide, water and hydrogen. The process may include introducing feed streams selected from (1), (2) or (3) and oxygen into a reaction vessel and switching modes between performing method I or method II in the reaction vessel wherein no catalyst is present. The reaction vessel may be provided with a burner located at the top of the reaction vessel, the burner may include coaxial channels for the separate introduction of the different gas streams. Method I may be a reverse water gas shift reaction at elevated temperature. Method II may be a partial oxidation reaction at elevated temperature.

Abstract: The present invention relates to a process for converting carbon dioxide and hydrogen by performing a reverse water gas shift reaction at elevated temperature, the process comprising introducing carbon dioxide, hydrogen and oxygen into a reaction vessel having an inlet and an outlet, and, wherein the reverse water gas shift reaction takes place in two different zones of the reaction vessel, being a top zone (z1) adjacent to a bottom zone (z2). The process produces a product stream comprising mainly carbon monoxide, hydrogen and water. The process is useful in reducing the carbon footprint of certain industrial technologies, and in addition, the process is useful in the production of synthesis gas.

Abstract: A process for converting carbon dioxide and hydrogen into a product stream comprising carbon monoxide, water and hydrogen by introducing carbon dioxide, hydrogen and oxygen into a reaction vessel, and performing a reverse water gas shift reaction at elevated temperature, wherein (a) no catalyst is present in vessel (b) gas stream comprising carbon dioxide, a hydrogen and an oxygen rich gas stream are introduced into the vessel in separate feed streams, (c) the hydrogen and oxygen rich gas stream being introduced in close vicinity of each other, via burner comprising coaxial channels wherein gases gas undergo a combustion reaction, providing the heating energy required for the reverse water-gas shift reaction; and (d) the temperature in vessel is in the range of 1000 to 1500° C. by varying the molar ratio of hydrogen to oxygen. It is useful in reducing the carbon footprint of certain industrial technologies, and in production of synthesis gas.

Abstract: A process for preparing a syngas from a methane comprising gas includes reacting the methane comprising gas with an oxidising gas at an operating temperature in the range of 1150 to 1370° C. by means of non-catalytic partial oxidation. A hot raw syngas mixture having a methane content higher than the methane content in a state of thermodynamic equilibrium at the operating temperature applied is passed through a bed of methane oxidation catalyst for oxidising methane with steam formed in the non-catalytic POX into carbon monoxide and hydrogen. The methane oxidation catalyst has at least one catalytically active metal supported on a refractory oxide support material where soot particles present in the hot raw syngas mixture are retained. The retained soot particles are converted to carbon monoxide. Soot depleted syngas is recovered in a state of thermodynamic equilibrium.

Abstract: A process for the production of synthesis gas by partial combustion of a hydrocarbon feed using a burner with a plurality of coaxial channels, the method comprising the following steps: supplying a non-gaseous hydrocarbon feed using at least one of the plurality of coaxial channels; supplying a gaseous hydrocarbon feed using at least one of the plurality of coaxial channels; supplying an oxidizer gas using at least one of the plurality of coaxial channels; separately supplying a moderator gas using at least one of the plurality of coaxial channels; arranging the at least one channel supplying the non-gaseous hydrocarbon feed between two adjacent channels among the plurality of coaxial channels, wherein the two adjacent channels both supplying a flow containing the gaseous hydrocarbon feed or respectively supplying a flow containing the gaseous hydrocarbon feed and a flow of the moderator gas.

Abstract: Process, reactor and burner for the gasification of a hydrocarbon fuel. The burner comprises coaxial channels for the separate supply of an oxidizer gas, a hydrocarbon fuel and a moderator gas. A coaxial channel with the smallest width is bordered by a separating wall with at least one gas exchange. The gas exchange passage can for example be formed by a retracted end of the separating wall and/or by openings in the separating wall.

Abstract: Process, reactor and burner for the gasification of a hydrocarbon fuel. The burner comprises coaxial channels for the separate supply of an oxidizer gas, a hydrocarbon fuel and a moderator gas. A coaxial channel with the smallest width is bordered by a separating wall with at least one gas exchange. The gas exchange passage can for example be formed by a retracted end of the separating wall and/or by openings in the separating wall.

Abstract: Process and reactor for the production of synthesis gas by partial combustion of a hydrocarbon feed. A burner is used with a plurality of coaxial burner channels, wherein at least one channel supplies a flow of a non-gaseous hydrocarbon feed, at least one other channel supplies a flow containing a gaseous hydrocarbon feed and at least one further channel supplies a non-hydrocarbon moderator gas.

Abstract: The invention provides a process to prepare a Fischer-Tropsch synthesis product from a gaseous mixture of hydrocarbons comprising methane, ethane and optional higher carbon number hydrocarbons comprising the steps of: (a) pre-reforming the hydrocarbon mixture adiabatically, (b) heating the gaseous mixture obtained in step (a) to a temperature greater than 650° C., (c) performing a non-catalyzed partial oxidation by contacting the heated mixture of step (b) yielding a reactor effluent having a temperature of between 1100 and 1500° C.

Abstract: The invention provides a process to prepare a Fischer-Tropsch synthesis product from a gaseous mixture of hydrocarbons comprising methane, ethane and optional higher carbon number hydrocarbons comprising the steps of: (a) pre-reforming the hydrocarbon mixture adiabatically, (b) heating the gaseous mixture obtained in step (a) to a temperature greater than 650° C., (c) performing a non-catalyzed partial oxidation by contacting the heated mixture of step (b) yielding a reactor effluent having a temperature of between 1100 and 1500 ° C.