Distributed hydrogen for the hydrogen economy will require new catalysts and processes. Existing large‐scale hydrogen plants can not simply be reduced in size to meet the economic, safety, and frequent duty cycle requirements for applications for fuel cells, hydrogen fueling stations, and industrial uses such as hydrogenation reactions, gas turbine cooling, metal processing, etc 1 2. Consequently, there is a need to completely reassess how hydrogen can be made for the emerging hydrogen economy. This article presents some of the technological advantages of precious metal monoliths over traditional base metal particulate catalysts for reforming hydrocarbons, such as natural gas, for the generation of distributed hydrogen.

/pdf/precious-metal-catalysts-supported-on-ceramic-and-metal-3l10nlkg3h.pdf

Precious Metal Catalysts Supported on Ceramic and Metal Monolithic Structures for the Hydrogen Economy

A method and apparatus (212) selectively oxidizes, within the fuel cell assembly (210), the carbon monoxide present in a fuel stream (222) fed to the assembly. A quantity of catalyst is contained within at least a portion of a fuel stream passageway within the stack. The carbon monoxide is selectively oxidized by the catalyst to carbon dioxide, and carbon monoxide produced by the reverse water-shift reaction is also oxidized.

Electrochemical fuel cell assembly with integral selective oxidizer

The invention pertains to the preparation and use of catalytic materials and catalyst members for the selective oxidation of carbon monoxide in a gas stream that contains hydrogen. One such catalyst member may be produced by depositing by electric arc spraying a metal feedstock onto a metal substrate to provide a metal anchor layer on the substrate, and depositing a catalytic material comprising platinum and iron dispersed on a refractory inorganic oxide support material onto the metal substrate. The catalytic material may optionally be produced by wetting the support material, especially a particulate support material, with a platinum group metal solution and iron solution and drying and calcining the wetted support material in air at a temperature in the range of from 200° C. to 300° C., preferably using a solution containing bivalent platinum ion species. The catalyst member may be used by flowing the gas stream therethrough at a temperature at about 90° C. with a O 2 :CO ratio of about 1:1 and a space velocity of about 20,000/hr or, alternatively, at a temperature of about 150° C. with a O 2 :CO ratio of about 1.5:1 and a space velocity of about 80,000/hr.

Method for preparation of catalytic material for selective oxidation and catalyst members thereof

A process and apparatus are disclosed for the operation of a fuel cell to generate electric power from a feed stream comprising a hydrocarbon or an alcohol. The fuel cell comprises a proton exchange membrane which produces electric power from a hydrogen product stream which comprises essentially no carbon monoxide. The hydrogen product stream is produced from the feed stream in a novel steam reforming zone containing a steam reforming catalyst disposed in a bell-shaped catalyst zone. The bell-shaped catalyst zone is disposed over a combustion zone such that the exhaust gas from the combustion flows around the bell-shaped catalyst zone to heat the catalyst from the inside and the outside of the catalyst zone. Furthermore, the bell-shaped catalyst zone maintains a high inlet and a high outlet temperature to avoid methane slippage in the steam reforming zone. Heat for the steam reforming zone is provided by a fuel stream and at least a portion of the anode waste gas stream from the fuel cell.

Process for the generation of pure hydrogen for use with fuel cells

A method and apparatus oxidizes the carbon monoxide present in an incoming reactant fuel stream and/or carbon monoxide produced by the reverse water-shift reaction to carbon dioxide in a reactant stream introduced to an electrochemical fuel cell. The reactant stream comprises hydrogen, carbon dioxide and carbon monoxide. A first oxygen-containing gas stream is introduced into the reactant stream through a first port disposed between the reactant stream inlet (214) and the reactant stream outlet (218). A further oxygen-containing gas stream is introduced into the reactant stream through at least one secondary port (234) located between the first port and the reactant stream outlet (218).

Method and apparatus for oxidizing carbon monoxide in the reactant stream of an electrochemical fuel cell

AN IMPROVED PROCESS FOR THE SELECTIVE OXIDATION OF CARBON MONOXIDE CONTAINED IN FEED GASES FROM A STEAM REFORMER-CONVERTER WHEREIN THE FEED GASES IN ADMIXTURE WITH OXYGEN ARE CONTACTED WITH A PLATINUM GROUP METAL CATALYST AND THE ACTIVITY OF THE CATALYST FOR THE SELECTIVE OXIDATION REACTION IS MAINTAINED BY PERIODICALLY TREATING DEACTIVATED CATALYST WITH THE SELECTED OXIDATION REACTION EFFUENT GASES CONTAINING LESS THAN 50 P.P.M. CARBON MONOXIDE AT A TEMPERATURE OF 75* TO 200*C.

Process for oxidation of carbon monoxide

1299666 Carbon dioxide ENGELHARD MINERALS & CHEMICALS CORP 3 April 1970 [4 April 1969] 16031/70 Heading C1A [Also in Division B1] Carbon monoxide is removed from a feed containing 0A01 to 3% vol carbon monoxide, 50 to 99% vol hydrogen, 0 to 5% vol carbon dioxide and the remainder, if any, inert gas by oxidation of the carbon monoxide to carbon dioxide over a supported platinum group metal catalyst Oxygen is mixed with the feed gas to give an O 2 : CO ratio of 0A5 : 1 to 3 : 1 and conditions used are an inlet temperature of 20-100‹ C and a pressure of atmosphere to 500 psig In the Figure, a scheme is shown for producing a gas of low carbon monoxide content from a mixture of steam, air and natural gas which is fed in at line 1 The mixture is heated in furnace 2, heat exchanged in exchanger 4 then saturated with water vapour in vessel 6 The saturated gases pass by way of heat exchanger 4 to shift converter 8 in which CO is reacted with water vapour to produce CO 2 and H 2  The effluent gases are cooled by water in tower 10 and then passed through monoethanolamine absorber 12 to remove carbon dioxide The mixture at this stage typically comprises 0A1% CO 2 , 0A5% CO; 0A4% methane and 0A3% argon The mixture is finally passed over the supported platinum metal catalyst in vessel 16 to remove the last traces of carbon monoxide, and then through CO 2 absorber 20 and gas cooler 22 to use, eg in ammonia synthesis Lines 24 and 26 are provided so that the flow of the gas mixture over the catalyst may be reversed when the catalyst becomes deactivated so as to regenerate it without interrupting flow

Cohn Johann Gunther E

Papers

Process for oxidation of carbon monoxide

Process for the reactivation of a catalyst