This invention provides a preparation method of a catalyst for preferential oxidization of CO in a hydrogen-enriched atmosphere, and a catalyst product obtained from the method and its applications thereof. Particularly, in this invention, a wide-temperature catalyst for preferential oxidization of CO in a hydrogen-enriched atmosphere is obtained by depositing one or more of an iron oxide, cobalt oxide, and nickel oxide as a promoter onto the surface of a supported Pt-group noble metal catalyst precursor via chemical vapor deposition or atomic layer deposition. In the wide-temperature catalyst, the active noble metal component has a content of 0.1 to 10 wt %, and the promoter has a content of 0.1 to 10 wt % in terms of the metal element thereof. In the reaction of preferential oxidation of CO in a hydrogen-enriched atmosphere, the catalyst prepared by this invention can exhibit excellent catalytic performance and can achieve high conversion of CO with high selectivity in a wide temperature range of −80 to 200° C., for example. Also, the catalyst can remain stable for a long time even in a case where steam and CO.sub.2 are present in the hydrogen-enriched atmosphere.

A method of removing CO from a mixture of CO and saturated and unsaturated hydrocarbons CO to CO.sub.2 is provided. In one embodiment, the method is to contact feed stream with an oxygen transfer agent; and then oxidize at least a portion of the CO to CO.sub.2 to produce a stream enriched in CO.sub.2. The saturated and unsaturated hydrocarbons in the feed are not further oxidized during the oxidation. The oxygen transfer agent includes at least one of: i) water; ii) at least one reducible metal oxide; iii) at least one reducible chalcogen; or mixtures thereof. In another embodiment, the CO is converted to methane. The unsaturated hydrocarbons in the feed are not hydrogenated. In both of these alternatives, the CO.sub.2 or methane are then removed. Systems for removing the CO are also provided.

A process to synthesize a catalyst performing Water-Gas shift reaction at a temperature more than 300° C. using a precursor having general formula [(Cu, Zn).sub.1−x (Al, M).sub.x (OH).sub.2].sup.x+ (A.sup.n−.sub.x/n).kH.sub.2O with M=Al, La, Ga or In, A=CO.sub.3, 0.33<x<0.5, 1<n<3.

A method of removing CO from a mixture of CO and saturated and unsaturated hydrocarbons CO to CO.sub.2 is provided. In one embodiment, the method is to contact feed stream with an oxygen transfer agent; and then oxidize at least a portion of the CO to CO.sub.2 to produce a stream enriched in CO.sub.2. The saturated and unsaturated hydrocarbons in the feed are not further oxidized during the oxidation. The oxygen transfer agent includes at least one of: i) water; ii) at least one reducible metal oxide; iii) at least one reducible chalcogen; or mixtures thereof. In another embodiment, the CO is converted to methane. The unsaturated hydrocarbons in the feed are not hydrogenated. In both of these alternatives, the CO.sub.2 or methane are then removed. Systems for removing the CO are also provided.

A method of removing CO from a mixture of CO and saturated or unsaturated hydrocarbons is provided. In one embodiment, the method is to contact a feed stream with an oxygen transfer agent; and then oxidize at least a portion of the CO to CO.sub.2 to produce a stream enriched in CO.sub.2. The saturated and unsaturated hydrocarbons in the feed are not further oxidized during the oxidation. The oxygen transfer agent includes at least one of: i) water; ii) at least one reducible metal oxide; iii) at least one reducible chalcogen; or mixtures thereof. In another embodiment, the CO is converted to methane. The unsaturated hydrocarbons in the feed are not hydrogenated. In both of these alternatives, the CO.sub.2 or methane are then removed. Systems for removing the CO are also provided.

In a fuel cell system for a submarine, hydrogen gas having a reduced carbon monoxide content while the hydrogen gas passes through a purification unit using a selective oxidation reaction can be supplied as a raw material to a fuel cell, so that electrode activity deterioration which may be caused by carbon monoxide can be prevented. In addition, the fuel cell system for a submarine can be miniaturized and weight-reduced and allows gas unreacted in a fuel cell stack to be burnt and recycled to supply heat to a reforming unit, thereby minimizing the amount of discharge gas.

Provided is a hydrogen production reactor as a reactor producing a reforming gas including hydrogen, in which a burning unit and a reforming unit are sequentially arranged and spaced apart from each other in a concentric structure based on a raw material transfer pipe positioned at a central axis of the reactor, including a heating raw material transfer pipe supplying a raw material to the burning unit, a burning unit burning the supplied raw material and supplying heat to the reforming unit, a reforming raw material phase change pipe positioned within the burning unit and heating the supplied raw material, and a reforming unit reforming the phase-changed raw material supplied from the reforming raw material phase change pipe, wherein the reforming raw material phase change pipe is provided as a coil surrounding an outer circumferential surface of a lower end of the heating raw material transfer pipe.

This invention relates to a method of chemical looping using non-stoichiometric materials with a variable degree of non-stoichiometry. One application of these methods is in the water gas shift reaction for H.sub.2 production. The methods of the invention can overcome limitations, e.g. those associated with chemical equilibria, which prevent chemical processes from proceeding with complete conversion of starting materials to products.

The invention relates to a method of starting-up a fuel cell arrangement (1) comprising a fuel processor (2) and a fuel cell (70), wherein the fuel processor (2) comprises the following components: a first evaporator (10), a reformer (20) arranged downstream of the first evaporator (10), a water-gas shift reactor (30), a PrOx reactor (40), a first heat exchanger (11), an afterburner (21) and a startup burner (50), wherein the method comprises the following steps: a) electrically heating a heating arrangement in the fuel processor (2) to heat a first gas (G1), b) heating the components of the fuel processor (2) to a fixed operating temperature by circulating the heated first gas (G1) through at least the first heat exchanger (11) and the afterburner (21), c) catalytically combusting an atomized or evaporated fuel (B) in the startup burner (50) and then afterburning hydrogen in the afterburner (21) for further heating of the first gas (G1) via at least one heat exchanger, d) introducing the fuel (B) into the preheated components of the fuel processor (2) and stopping the catalytic combustion in the startup burner (50), e) starting up at least one reaction in the components of the fuel processor (2), until an exit gas from a PrOx reactor (40) has a given CO content, and f) switching on the fuel cell (70). The invention further relates to a fuel cell arrangement.

The invention relates to a PrOx reactor (R) comprising a housing that encloses a reaction space and has a first inlet (E1) for supply of a hydrogenous first gas (G1) to a reaction space, a second inlet (E2) for supply of an oxygenous second gas (G2) to the reaction space and an outlet (A) for discharge of a third gas (G3), wherein there is a multitude of conduits (Kv) extending from the second inlet (E2) into the reaction space, each of which comprises at least one opening (O) for supply of the second gas (G2) to the reaction space.