In the figure, 4a is a shift reaction portion, 3 a steam superheating portion, 38 a shift catalyst, and 27 a heat-transfer fin. The cost of the PdAg membrane and its susceptibility to damage by temperature changes provide obstacles to adoption.
For this reason, the high-temperature recovery portion 7b and the catalytic combustion portion 6a are provided on both sides of the steam superheating portion 3 as heating sources.
For non-stationary However, traditional reactors with randomly packed catalytic operations of the reactor, this feature is essential. The feed section for the total staked together in the housing Fig.
This structure is capable of reducing the size of the apparatus compared with the aforementioned conventional apparatuses, also suppressing the thermal loss of the heat-source gases generated in the combustion portion 84, and making efficient use of heat.
As reported nitude higher compared to traditional chemical reactors. The fuel reforming apparatus as set forth in claim 1, wherein said catalytic combustion portion is divided into a plurality of portions and inserted between the reforming portion and the steam superheating portion and wherein a fuel portion of said catalytic combustion portion and the reforming portion are stacked in contact with each other.
This reactor consisted of a hollow ceramic tube within a ceramic test-tube shaped well, with both the inside and outside surfaces of the hollow tube coated with similar or different metal catalyst films.
Below the reformed-gas exhaust tube 12, there are provided both the OFF-gas supply tube 13 for supplying Off-gases from the exterior of the upper end plate 23 to the interior and the Off-gas supply manifold Field of the Invention The present invention relates to a fuel reforming apparatus which is employed, for example, for generating hydrogen necessary for portable fuel cells for general power supply or necessary for fuel cells to be mounted in electric automobiles and converts alcohol material or hydrocarbon material to hydrogen-rich, reformed gases.
The heat produced by catalytic oxidation of fuel in the first channel is transferred to the second channel where a catalytic reforming reaction takes place. The resulting product in the reforming gas, primarily a mixture of hydrogen and carbon dioxide, is then discharged through an outlet conduit.
The reformed gases emerging from the reforming portion 4 are introduced into a shift reaction porion 4a, and, after water and carbon monoxide have been converted to carbon dioxide and hydrogen, the reformed gases are guided to the CO oxidization portion 5, in which the remaining CO is converted to CO2 by oxidization.
Since the response factor of the mass spectrometer ing reactors exists. The catalyst was micro-milled 3.
Yan [ 8 ] used nickel-chromium alloy as the material of a micro heater and nickel as the material for a temperature sensor.
Different cata- state and the dynamic reactor behavior. The cylindrical housing 18 of the tubular reactor 17 is connected at the end faces to the connecting line 5 and the outlet conduit.
Therefore, the reactor should be designed so that an optimum heat transfer from a heat transfer medium supplied to the reformed gas and the catalyst material is ensured.
Stokes, Hydrogen production by steam reforming of methanol  J. Also, with the symmetrical plane between the first and second stacked bodies as a boundary, the second stacked body is constituted by flat plate elements:.
The methanol steam reforming (MSR) catalyst was inserted in a serpentine channel of the cellular reformer, separated from the membrane electrode assembly (MEA) of the fuel cell by highly permeable and selective Pd-Ag membrane.
Sensors11 1. Introduction Methanol is a more feasible liquid fuel for use in a reformer owing to its high safety of storage and transport, high carbon/hydrogen ratio, high power density and low reforming temperature.
A methanol reformer is a device used in chemical engineering, especially in the area of fuel cell technology, which can produce pure hydrogen gas and carbon dioxide by reacting a.
A numerical study is performed to examine the characteristics of heat and mass transfer and the performance of a plate methanol steam micro reformer with a methanol catalytic combustor. The next method of producing H2 gas from methanol is the steam reforming of methanol.
This involves the sum of reactions 1 & 2 combined into one step as given in eq. 3: 3 + ↔ + CH OH H O H CO 3 2 2 2 (3) SRM H kJ mol Catalytic Production of Hydrogen Gas by Methanol Reforming. In the middle of oxidation of methanol allows to switch between inert (nitro- the stack a special plate, designed for temperature measure- gen) and reactant feed consisting of methanol ( mol%), ments, is.Inserted plate coated of methanol steam reformer