MXPA98008429A - Thermally better compact reformer - Google Patents

Abstract

A natural gas reformer (10) comprising a stack of thermally conductive plates (12) interdispersed (12) with catalyst plates (14) and provided with internal or external manifolds or manifolds for reagents. The catalyst plate is in intimate thermal contact with the conductive plates in such a way that its temperature closely follows the temperature of the thermally conductive plate, which can be designed to reach an almost isothermal state in plane to the plate. One or more catalysts, distributed over the direction of flow, can be employed in plan to the thermally conductive plate in a variety of optional embodiments. The reformer can be operated as a steam reformer or as a partial oxidation reformer. When operating as a steam reformer, thermal energy is externally provided for the steam reforming reaction (endothermic), by radiation and / or conduction to the thermally conductive plates. This produces carbon monoxide, hydrogen, vapor and carbon dioxide. When operating as a partial oxidation reformer, a fraction of natural gas is oxidized assisted by the presence of a combustion catalyst and a reforming catalyst. This produces carbon monoxide, hydrogen, vapor and carbon dioxide. Because of the intimate thermal contact between the catalyst plate and the conductive plates, excessive temperature can not develop within the stack structure. Plate design details can be varied to fit a variety of manifold or manifold modes, by providing one or more inlet and outlet gates, to introduce preheat and discharge of reactive

Description

THERMALLY IMPROVED COMPACT REFORMER BACKGROUND OF THE INVENTION The present invention relates to reformers and particularly to reforming apparatuses that reform fuels in fuel species suitable for use by electrochemical converters. In particular, it relates to a plate-type reformer, suitable either for steam reforming or reforming with partial oxidation. The use of conventional hydrocarbon fuels as a combustible reagent for fuel cells is well known in the art. Hydrocarbon fuels are typically pre-processed and reformed into simpler reagents before introduction to the electrochemical converter. Conventionally, the fuel is pre-processed by passing the hydrocarbon fuel first through a desulfurization unit, then through a reformer, and a displacement or change reactor (for a fuel cell supplied with H2 only), to produce a convenient combustible material. Conventional steam reformers currently in wide commercial use comprise a reforming section consisting of a catalyst material that promotes the reforming reaction and a burner to supply heat for the endothermic reforming reaction. A steam source is typically connected to the reforming section to provide steam. The burner typically operates at temperatures well above those required by the reforming reaction and well above the operating temperatures of conventional fuel cells, for example solid oxide fuel cells. Because of this, the burner must operate as a separate unit independent of the fuel cell and as such contributes considerable volume, weight, cost and complexity to the total energy system. In addition, the burner is not uniquely adaptable to utilize the waste heat generally available from the fuel cell. Furthermore, the consumption of extra fuel by the burner limits the efficiency of the energy system. A typical tubular reformer contains multiple tubes, which are normally produced from refractory metal alloys. Each tube contains a packed pelletized or granular material having a convenient reforming catalyst as a surface coating. The tube diameter typically varies between 9 and 16 cm, and the pre-heated heated tube length usually between 6 and 12 meters. A combustion zone is provided external to the tube and is typically formed in the burner. The temperature on the surface of the tube is maintained by the burner in the range of 900 ° C to ensure that the hydrocarbon fuel circulating inside the tube is suitably catalyzed with steam at a temperature between 500 ° C and 700 ° C. This traditional tube reformer is based on thermal transfer by conduction and convex inside the tube to distribute heat to reform. Plate-type reformers are known in the art, an example of which is illustrated and described in US Pat. No. 5,015,444 to Koga et al. The described reformer has alternating planar gap spaces for fuel / vapor mixture flow and fuel / air mixture flow. The combustion of the air / fuel stream within the spaces provides the heat to reform the fuel / vapor mixture stream. A disadvantage of this design is that the reformer relies on the thermal transfer between the adjacent flat separation spaces to promote the process of reforming the fuel. The U.S. Patent No. 5,470,670 of Yas? oto et al. describes an integrated reformer / fuel cell structure, having alternating layers of fuel cells and reformer plates. The thermal transfer from the exothermic fuel cell to the endothermic reformer occurs through the thickness of the separation plates. A disadvantage of this design is that they are difficult to reach, if in fact, temperature uniformities in this fuel cell / reformer structure, and that is essential in compact and efficient electrochemical or chemical device designs. This fuel cell / reformer structure also requires multiple reagents for complex, problematic reagents to interconnect the reagent streams between the alternating fuel cell layers and the reformer layers. Electrochemical converters such as fuel cells have known as systems for converting chemical energy derived from fuel materials, directly into electrical energy through electrochemical reaction. One type of fuel cell typically used in fuel cell based power generation systems is a solid oxide fuel cell. The solid oxide fuel cell generates electricity and releases waste heat at a temperature of approximately 1000 ° C. A typical fuel cell consists primarily of a series of electrolyte units in which oxidant and fuel electrodes are connected, and a similar series of interconnects disposed between the electrolyte units provide electrical connections in series. Electricity is generated between the electrodes through the electrolyte by an electrochemical reaction that is fired with a fuel, such as hydrogen, is introduced into the fuel electrode and an oxidant, for example oxygen, is introduced into the oxidizing electrode. Typically, the electrolyte is an iconic conductor having low ionic strength, thereby allowing transport of an ionic species from an electrode-electrolyte interface to the opposite electrode-electrolyte interface under the operating conditions of the converter. The electrical current can be derived from external load from the interconnector plates. The conventional solid oxide fuel cell also includes, in addition to the features listed above, an electrolyte having an oxidizing electrode material and porous fuel applied on opposite sides of the electrolyte. The electrolyte is typically an oxygen ion conducting material, such as stabilized zirconium oxide. The oxidizing electrode, which is typically kept in an oxidizing atmosphere is usually a high electrical conductivity perovskite such as lanthanum manganite, adulterated with strontium (LaMn03 (Sr).) The fuel electrode is typically maintained in a fuel-rich or reducing atmosphere and usually It is a cer et such as zirconium oxide and nickel oxide (Zr02 / Ni) .The interconnecting plate of the solid oxide fuel cell is typically made from an electronic conductive material that is stable in both an oxidizing and receiving atmosphere. There is still a need in the art for a plate utilizing the waste heat generated by the fuel cell for reforming use In particular, there is a need to employ a reformer design in close association with the electrochemical converters. It will be described below in connection with certain preferred modalities, however it should be clear that Various changes and modifications can be practiced by those skilled in the art without departing from the spirit and scope of the invention. SUMMARY OF THE INVENTION It is an object of the present invention to provide a plate type reformer having excellent thermal performance characteristics and allowing effective thermal integration with a fuel cell.

The invention also relates to a plate-type reformer that can be operated either as a steam reformer or as a partial oxidation reformer. When operated as a steam reformer, it receives heat from a source such as a fuel cell, and receives steam from a source such as the exhaust from a fuel cell. The steam can be supplied externally from any conventional source, such as a steam boiler, or it can be supplied by multiple distribution of the exhaust from a conventional fuel cell to the reformer. The thermal source can also be a combustion reactor. When operated as a partial oxidation reformer, it burns a relatively small portion, for example about 25% of the incoming reactant gas, to provide heat for the endothermic reforming reaction. The reformer is preferably able to operate at a balanced autothermal condition, which does not require any other power (heat source) or steam supply. It is also capable of operating at a partial oxidation condition that is capable of utilizing waste heat from a fuel cell. Another object of the present invention is to provide a plate-type reformer wherein the catalyst is in intimate thermal contact with thermally conductive plates, oriented, for example elongated in the direction of gas flow, such that a plate temperature in The average plane is maintained to allow an effective reforming reaction, as well as to eliminate or reduce the occurrence of hot spots that would be harmful to the catalytic materials or the structure of the reformer. The term "in plane" is meant to mean the flat surfaces or side of the plate. Still another object of the invention is to provide a plate-type reformer that is capable of utilizing the waste heat that is provided by the fuel cell for its endothermic reactions, either in steam reforming or in partial oxidation reforming. Still another object of the invention is to provide a plate-type reformer that preheats incoming reagents to a suitable temperature for reforming. Another object of the invention is to provide a plate-type reformer wherein input manifolds are provided, such that reagents can be introduced to the reformer separately, and then mixed thoroughly into the reformer, before entering the section of oxidation and the reformer section. The reformer of the present invention employs a thermal improvement feature that promotes efficient fuel reforming. According to one aspect, the reformer includes a planar catalyst configuration having thermally interleaved conductive plates. This last feature greatly improves the thermal characteristics of the reformer, resulting in a relatively compact reformer design. Therefore, the reformer can be thermally and physically integrated with an electrochemical converter to efficiently reform hydrocarbon fuel and generate electricity. The invention overcomes the size disadvantages of conventional reformers by using the above efficient thermal transfer techniques, to achieve uniformity in temperature (isothermal surfaces) and energy balance in the system. This uniformity of temperature reduces the amount of reforming material needed to reform the input reagents. In addition, the thermal energy required by the endothermic reforming reactions is derived from the waste heat of the thermally integrated electrochemical converter. For example, under normal operating conditions, the converter generates waste heat or excess heat, which is used to withstand an operating temperature consistent with that required for reforming (in the range of between about 500 ° C and about 700 ° C). Compactness and simplicity of distribution are essential to provide a basis for system integration and economic reformer construction.

Other general and more specific objectives of the invention will be evident in part and in part will be obvious from the drawings and description that follow. BRIEF DESCRIPTION OF THE DRAWINGS The foregoing and other objects, features and advantages of the invention will be apparent from the following description and apparent from the accompanying drawings in which like reference characters refer to the same parts through the different views. The drawings illustrate principles of the invention and although not to scale, show relative dimensions. Figure 1 is a cross-sectional view of an embodiment of an external fuel reformer according to the present invention; Figures 2A-2C are cross-sectional views of various embodiments of the reformer and catalyst plates of Figure 1; Figure 3 is an isometric view of an assembled electrochemical converter with internal reforming capability. Figure 4 is a more detailed isometric view of the electrolyte component and the interconnector component of an electrochemical converter allowing internal reforming; Figure 5 is an assembled cross-sectional view of the electrolyte component and interconnector component according to the invention illustrating the flow of externally distributed through reactants; and Figure 6 illustrates graphically that the interconnector plates provide the thermal transfer function between the endothermic reforming strip and the exothermic combustion strip and the exothermic fuel cell strip resulting in an isothermal plane temperature. DESCRIPTION OF ILLUSTRATED MODALITIES Figure 1 is a cross-sectional view of the reformer 10 of the present invention. The reformer 10 includes a number of thermally conductive plates 12 and reformer plates 14 that are stacked alternately together to form a stacked reforming structure 13 extending over the axis 28. The reformer includes a fluid conduit 16 that is in fluid communication with the inner portions 12a, 14a and plates 12, 14. The reformer 10 is preferably located within a gas tight enclosure 20. The illustrated reformer can be employed to perform both oxidation and steam reforming. The heat necessary for the reforming process can be supplied internally by partial oxidation of hydrocarbon fuel or supplied externally by the remote heat source, as illustrated by the corrugated lines 26, to the reformer 10 by radiation, conduction or convection. The reagent to be reformed by the reformer 10 is introduced to the apparatus through the axial fluid manifold 16. The reactant preferably comprises a mixture of hydrocarbon fuel and a reforming agent, such as air, oxygen, water or C02, which is pre-prepared. -mix either before introduction to manifold 16 or within the reformer. The illustrated reformer 10 includes at least one manifold that supplies a reformer / fuel agent mixture to the reformer, rather than providing separate feed manifolds for each gas constituent. The introduction of pre-mixed reagents to the reformer 10 provides a simple relative design. The mixture of reagents 22 is introduced to the manifold 16 by any suitable means such as fluid conduits. The mixture 22 enters the interior portions of the reformer through the reagent passages 24 that form between the adjacent conductive plates 12 and the reforming plates 14. The passages may comprise any surface indentations or projections, which may be formed upon enhancement and constitute a substantially continuous fluid passageway extending from the manifold 16 to the peripheral surface 13a of the stacked reforming structure 13. The passages are also formed by using reforming or conductive plates that are made from a porous material or have a material energy reforming catalyst coated or formed there, thus allowing the reagent to pass through the reformer. Examples of these various plate structures and configurations are illustrated in Figures 2a-2c. Figure 2a illustrates the stacked structure of the reformer plates 14 and conductive plates 12. The reformer plates preferably have formed a reformed catalyst material 36 which intimately contacts the conductive plate 12. The illustrated conductive plate 12 is embossed to form flow channels of reagents The mixture 22 is introduced to the axial manifold 16 and enters the reagent channels, where it exits the plate reformer stacked at its peripheral edges. The reforming catalyst material may be composed of a solid or porous material. Figure 2b illustrates the mixing flow through the reformer 10 when a porous reforming material is used. The use of a porous reforming material relaxes the enhancement requirements of the illustrated reformer. In another embodiment, as illustrated in Figure 2c, the reformer 10 includes a plurality of stacked plates 38 or simply a column structure that is formed of a composite of thermally conductive material and a reforming material. This composite plate 38 can be achieved by interdispersing a suitable thermally conductive material in admixture with a suitable reforming material. The resulting stacked structure operates superficially in identical fashion to the stacked reforming structure 3 illustrated in Figures 1, 2c and 2b and described above. Those with ordinary dexterity will recognize that other reforming modalities 10 exist, such as when the reformer plates 14 are composed of a porous material and have a reforming catalyst material disposed there or coated. The use of porous materials is one of the advantages of the present external reformer since it relaxes the gas tightness requirements of the reforming system without sacrificing efficiency. The reagent mixture is reformed within the stacked reforming structure 10 as the reagent passes through the reagent passages and over or through the reforming plates 14. The catalyst material associated with reforming plates 14 promotes reforming of hydrocarbon fuel in simpler reaction species. The stream of reagent mixtures introduced into manifold 16 may comprise H20, 02 and C02, in addition to a hydrocarbon fuel. For example, methane (CH4) can be reformed catalytically in a mixture of hydrogen, water, carbon monoxide and carbon dioxide. When the reformer is operated as a steam reformer, it receives a mixture of reactive gases containing natural gas (or methane) and steam. The steam reforming catalyst can be formed in a circumferential band. The thermal energy of the reforming reaction is preferably conducted radially inward from the gas-tight enclosure by the conductive plates 12. The reactor and thermal conductivity of the conductive plates are chosen to provide sufficient thermal flow radially (or in plan) to provide heat to the endothermic reforming reaction. The conductive plate may include an integral extension projecting into the axial reagent manifold 16 for preheating the reagent reagents as described in more detail below. When operating, the reformer, as a partial oxidation reformer, receives a mixture of reactive gases containing natural gas (or methane) and air or oxygen. One or more types of the reforming catalyst material can be distributed in circumferential bands of the reforming plate. According to one aspect, the plate may include an inner band containing a combustion catalyst 92, and a radially outer band 90 containing catalyst to promote reforming of methane by steam (reforming with steam) and by carbon dioxide. The thermal energy for these endothermic reforming reactions is conducted radially from the combustion band to the reforming band by plate 12. Catalysts for other reactions, such as conventional displacement reactions that convert CO in the presence of or H20 to form H2 and C02, can also be incorporated. The thickness and thermal conductivity of the conductive plates 12 are chosen to provide sufficient thermal flow radially between the inner combustion band and the outer reforming band to supply thermal energy for the endothermic reforming reactions. The conductive plates 12 also provide enough and heat radially from the combustion band to preheat the incoming reagents in the inlet passages 24, at almost operational temperatures, for example -300 ° C. The thermal energy of the system is preferably transferred from the external source to the reformer 10 through the gas tight enclosure 20. The illustrated reformer 10 can be used to reform reagents such as alkanes (paraffinic hydrocarbons), hydrocarbons bound with alcohols (hydroxyls) , hydrocarbons bonded with carboxyls, hydrocarbons bonded with carbonyls, hydrocarbons bonded with alkenes (olefin hydrocarbons), hydrocarbons bound with ethers, hydrocarbons bound with esters, hydrocarbons bonded with amines, hydrocarbons bound with aromatic derivatives and hydrocarbons linked with other derived bodies. The reforming material web of the reformer 10 can be located and mixed in varying proportions to maximize the production of reformed gas. The reformer plate 14 can be composed of any suitable reformed catalytic material which operates at temperatures in the range between about 200 ° C and about 800 ° C. Examples of the types of materials that may be employed include platinum, palladium, chromium, chromium oxide, nickel, nickel oxide, nickel-containing compounds and other suitable transition metals and their oxides. The reforming plate 14 may further include a ceramic support plate having a coated reforming material, as illustrated in Figures 2A and 2B. In this way, the reformer plate 14 of the present invention can include any reformed plate structure or multiple piles including convenient reforming catalysts that promote the reformation of a hydrocarbon fuel into suitable reaction species.

The conductive plate 12 can be formed of any suitable thermally conductive material, including metals such as aluminum, copper, iron, steel alloys, nickel, nickel alloys, chromium, chromium alloys, platinum and non-metals such as silicon carbide and others. composite materials. The thickness of the conductive plate 12 can be selected to maintain a minimum plane temperature gradient of the plate 12 and to thereby provide an isothermal region for optimal reforming reaction and to relieve thermal stress in the refurbishing plates 14. conductive plate 12 preferably forms an almost isothermal plane condition of each plate 12. The isothermal surface formed by the conductive plate 12 improves the efficiency of the total reforming process by providing a substantially uniform temperature and supply of heat on the surface of the plate for reformed. In addition, the conductive plates form an isothermal condition on the stack axis (on the outer peripheral surface of the stacked reformer 13) by the uniform distribution of the reagent mixture through the reagent passages, thus preventing points from arising. hot or cold on the pile. This improves the thermal characteristics of the reformer 10 and improves the overall performance of the system. As used herein, the term "isothermal" condition or region is intended to include a substantially constant temperature that varies only slightly in an axial or plane direction. A variation in temperature of about 50 ° C is contemplated by the teachings of the present invention. The reaction or refurbished fuel species are discharged onto the peripheral portion 13A of the stacked reforming structure 13, as indicated by the wavy lines 30. Peripheral discharge of the reaction species, eg reformed fuel products allow relatively easy distribution of the reagents. The discharged fluid medium is then collected by the gas-tight housing 20 and discharged from and through outlet conduits 32. The gas-tight housing 20 thus serves as a peripheral manifold. In an alternate mode, the mixture of reagents 22 can be introduced to the peripheral manifold formed by the housing 20 and then to the stacked reforming structure 13 on the peripheral edge. The reagent flows radially inwardly through the reforming and conducting plates 14, 12, and is discharged through the axial manifold 16. The ability to vent the reformed reagent mixture to at least a substantial portion of the periphery of the stack , and preferably near the entire periphery, provides an exposed peripheral surface lacking a gas tight seal or insulating material. Therefore, the external reformer 10 of the present invention achieves a compact, simple, elegant external reforming design. The gas tight enclosure 20 is preferably composed of a thermally conductive material, such as metal. In the illustrated embodiment, the gas-tight enclosure 20 radiantly receives thermal energy from an external thermal source and also radiantly transfers this thermal energy to the stack 13 and thus to the conductive plates 12. The plates 12 supply the thermal energy necessary for the reforming reaction, by conductively transferring the heat from the outer peripheral surface 13A of the stack 13 inwards, to the reagent manifold 16. In another embodiment, the outer surface of the reforming structure 10 contacts the outer surface of the gas tight housing, which serves to conductively transfer the thermal energy to the conductive plates. The gas tight enclosure of cylindrical configuration is particularly convenient for operation of the pressure reformer. The pressure within the vessel is preferably between about ambient and about 50 atm. The technique for achieving uniformity in the axial flow distribution of reagents is as follows. The reagent flow passages 24 are designed to have the total reagent flow pressure drop in the reagent passages be significantly greater than the pressure drop of reactive streams in reagent manifold 16 dominates. More specifically, the flow resistance of the passages 24 is substantially greater than the flow resistance of the axial manifold 16. In accordance with the preferred practice, the reagent flow pressure within the passages 24 is approximately 10 times greater than the flow pressure of reagents within the manifold. This pressure differential ensures a uniform azimuthal and axial distribution of the reagent over the reagent manifold 16 and the reactive passages 24 and essentially from the top to the bottom of the reformer stack 13. The uniform flow distribution ensures a uniform temperature condition on the axis of the reforming structure 10. According to a preferred embodiment, the stacked reforming structure 13 is a column structure, and the plate has a diameter between approximately 2.54 cm (1 in) and approximately 50.8 cm (20"). ) and has a thickness between approximately .00508 cm (.002") and approximately .508 cm (.2") .The term column, as used herein, is intended to describe various geometric structures that we stack on a longitudinal axis and have at least one internal reagent manifold that serves as a conduit for the mixing of reagents, those with ordinary dexterity will appreciate that other geometric configurations can in use, such as rectangular or rectilinear forms with multiple internal or external. The plates have a rectangular configuration, can be stacked and integrated with multiple external connected for the supply and collection of resistances resulting from reforming and reagents. The relatively small dimensions of plates 12, 14 of the reformer provide a compact plate-type reformer that reforms a hydrocarbon fuel and a convenient reaction species, and that easily integrates with existing energy systems and structures. The illustrated reformer 10 can be thermally integrated with an electrochemical converter, such as a solid oxide fuel cell. In the special application where the reformed fuel is introduced to the fuel cell, the required heat of reaction is supplied from the waste heat generated by the fuel cell. In accordance with another practice of the present invention, the reformer structure of Figure 1 can also function as a plate type burner. Specifically, hydrocarbon fuel can be oxidized in the presence of air or other oxidants with or without a convenient catalyst material. The burner mode of the present invention includes a conductive plate 12, and a catalyst plate 14 that are alternately stacked together, as described above in relation to the reformer of Figure 1. The burner can employ a feed manifold 16 for enter the burner entry reagent. The entry reagents may comprise a hydrocarbon fuel and an oxidant, such as air. The hydrocarbon fuel and oxidant can be distributed manifold separately to the burner or can be pre-mixed. For example, if substantially gas-tight materials are used to form plates 12, 14, the reagents are pre-mixed either before introduction to the burner or into the feed manifold. On the contrary, if any plate is formed of a porous material, the reagents can be distributed separately. Reagents that pass through the porous material of the plate then pass and mix with the other reagent within the reagent passages. The oxidized or burned reagent is then discharged around the periphery of the burner stack. The oxidized reagent or the resulting species include C02, H20 and other stable combustion products depending on the type of fuel. The conductive plate of the burner is identical to that of the reformer and functions to conductively transfer heat in plane from the plate to form an isothermal surface. The thickness of the conductive plate is designed to maintain a minimum temperature gradient in plane of the plate to provide an isothermal region for optimal combustion reaction to produce reduced NOx, if air is used as the oxidant and to relieve thermal stress in the catalyst plates 14. In addition, the isothermal condition can be maintained by the uniform distribution of reagents on the stack axis, thus avoiding hot and cold spots of any development on the pile. This improves the overall thermal characteristics of the burner and improves the overall operational performance of the burner. The illustrated burner further includes passages for reagent flow 24, as set forth above in conjunction with the reformer 10. The passages for reagent 24 are designed to ensure that the total reagent flow pressure drop in the reagent passages 24 is significantly greater than the pressure drop of the reagent stream in the reagent manifold 16. More specifically, the flow resistance of the passages 24 is substantially greater than the flow resistance in the axial manifold 16. This pressure differential ensures a distribution axial and azimuthal uniform reagents through the axial length of the burner. The oxidized reagent can be discharged relative to the peripheral portion of the burner. The fluid media discharged can be captured by a gas-tight housing 20 surrounding the burner. In an alternate embodiment, the burner may include a plurality of stacked plates that are formed of a composite of thermally conductive material and a catalyst material. This composite plate can be achieved by interdispersing a suitable thermally conductive material in admixture with a suitable catalytic material. The resulting stacked structure operates substantially identically to the stacked reforming structure 13 which is illustrated in Figure 1 and described above. In an alternate embodiment, the burner may include a cylindrical column which is formed of a composite of the thermally conductive material and a catalyst material by interdispersing a suitable thermally conductive material in admixture with a suitable catalytic material. The resulting reforming structure operates substantially identically to the stacked reforming structure 13 shown in Figure 1 and described above. All other features discussed above in relation to the reformer are equally applicable to the burner. Figure 3 shows an isometric view of a built-in reformer internal to an electrochemical converter, according to a preferred embodiment of the invention. The internal reforming electrochemical converter 40 is illustrated as consisting of alternating layers of an electrolyte plate 50 and an interconnecting plate 60. The interconnector plate is typically a good thermal and electrical conductor. Orifices or manifolds formed in the structure provide conduits for combustible gases and oxidants, for example reagent feed. Passages for flow of reagents formed in the interconnection plates, Figure 4, facilitate the distribution and collection of these gases. The plates 50, 60 of the internal reforming electrochemical converter 40 are held in compression by a spring-loaded connecting rod structure 42. The connecting rod structure 42 includes a connecting rod member 44 seated within a multiple oxidant. central 47, as illustrated in Figure 4, which includes an assembly nut 44A. A pair of end plates 46 mounted on either end of the internal reforming electrochemical converter 40, provide uniform clamping action on the stack of alternate electrolyte and interconnect plates 50, 60 and maintain electrical contact between the plates and provide gas sealing in appropriate places within the structure. Figures 3 to 5 illustrate the basic cell unit of the electrochemical converter 40, which includes the electrolyte plate 50 and the interconnector plate 60. In one embodiment, the electrolyte plate 50 can be made from a ceramic material such as an electrode material. stabilized zirconium oxide Zr02 (Y203), an oxygen ion conductor and a porous oxidizing electrode material 50A, and a porous fuel electrode material 50B which are disposed thereon. Exemplary materials for the oxidizing electrode material are perovskite materials, such as LaMn03 (Sr). Exemplary materials for the fuel electrode material are cermets such as Zr02 / Ni and Zr02 / Ni0. The interconnector plate 60 is preferably made of a thermally and electrically conductive interconnector material. Suitable materials for interconnector fabrication include metals such as aluminum, copper, iron, steel alloys, nickel, nickel alloys, chromium, chromium alloys, platinum, platinum alloys and non-metals such as silicon carbide (La) MnCr03 , and other electrically conductive materials. The interconnector plate 60 serves as the electrical connector between adjacent electrolyte plates and as a spacing between the oxidant and fuel reactants. Additionally, the interconnect plate 60 conductively transfers heat in plane (across the surface) of the plate to form an isothermal surface, as described in more detail below. As best illustrated in Figure 4, the interconnect plate 60 has a central opening 62 and a set of concentric radially outward intermediate spaced apertures 64. A third outer aperture assembly 66 is disposed on the outer cylindrical portion or periphery of the plate 60. The interconnect plate 60 may have a textured surface. The textured surface 60A preferably has a series of depressions or slits formed, which are formed by known embossing techniques and with which a series of passages for flow of connecting reagents is formed. Preferably, both sides of the interconnecting plate have a surface with grooves therein formed. Although the intermediate and outer set of openings 64 and 66 respectively are illustrated with a selected number of openings, those with ordinary skill will recognize that any number of openings or distribution patterns can be employed, depending on the system and reagent flow and distribution requirements. Similarly, the electrolyte plate 50 has a central opening 52 and a set of intermediate and outer openings 54 and 56, which are formed at sites complementary to the openings 62, 64 and 66 respectively of the interconnecting plate 60. As illustrated in FIG. Figure 4, an element for reagent flow adjustment 80 can be sandwiched between the electrolyte plate 50 and the interconnector plate 60. The element for flow adjustment 80 serves as an impedance for fluid flow between plates 50, 60, which restricts the flow of reagents in the passages for reagent flow. In this way, the element for adjusting the flow 80 provides greater uniformity of flow. A preferred flow-adjusting element is a mesh or wire screen, but any convenient design can be employed as long as it serves to restrict the flow of the reactants at a selected and determinable rate.

With reference to Figure 4, the electrolyte plates 50 and the interconnector plates 60 are alternately stacked and aligned over their respective openings. The openings form multiple axial (with respect to the stack) that feed the cell unit with the feed reagents and discharges into the spent fuel. In particular, the central openings 52, 62, form the multiple feed oxidant 47, the concentric openings 54, 64 form the feed fuel manifold 48 and the aligned outer openings 52, 66 form the spent fuel manifold 49. The absence of a flange or other raised structure in the portion of the periphery of the interconnector plate, provides discharge gates communicating with the external environment. The passages for reagent flow fluidly connect the reagent feed manifolds 46 and 48 to the outer periphery of the reformer 40, thereby allowing reagents to be discharged externally to the converter. The internal reforming electrochemical converter is a structure of stacked plates of cylindrical configuration and at least one of the electrolyte plate and the conductive plate has a diameter between about 2.54 cm (1 in) and about 50.8 cm (20 in) and has a thickness between approximately .00508 cm (.002") and approximately .508 cm (.2"). The internal reforming electrochemical converter 40 of this invention has additional features incorporated as described below. The internal reforming operation when performed in the presence of steam receives a mixture of reactive gas containing natural gas (or methane) and steam. A steam reforming catalyst 90 (Figure 5) is distributed in a circumferential band that precedes the fuel electrode material 50B in the electrolyte plate 50. Thermal energy for the reforming reaction is conducted radially by the plate 60 to the band of reformed. The thickness and thermal conductivity of the plates are designed to provide sufficient thermal flow radially between the inner reforming band 90 and the outer fuel cell band (e.g., band 50B), to provide thermal energy for the endothermic reforming reaction and to preheat the entry reagents. The internal reforming can also be carried out by a partial oxidation reaction. In this mode, the illustrated converter 40 receives a mixture of reactive gases containing natural gas (or methane) and air or oxygen. One or more types of catalysts are distributed in circumferential bands that precede the fuel electrode 50B to the electrolyte plate 50. As illustrated in Figure 5, the electrolyte plate includes an inner band containing a combustion catalyst 92, a radially outer band 90 containing catalysts for promoting methane reforming by steam (reformed with steam) and by carbon dioxide. The thermal energy for these endothermic reforming reactions is conducted radially from the combustion band 92 to the reforming band 90. Catalysts for other reactions, for example displacement reactions, etc., can also be incorporated. The thickness and thermal conductivity of the conductive plates is designed to provide sufficient heat flow radially between the inner combustion band 90 and the radially reshaped outer band 90, to provide the energy of the endothermic reaction and to preheat the incoming reagents. Additional thermal energy can be obtained from the exothermic fuel cell reaction performed by the fuel electrode 50B illustrated as an outermost band on the diameter of the plate. In the illustrated electrochemical converter 40, the combustion catalyst 92, the reforming catalyst 90 and a displacement catalyst (which can also be applied as a radially outward band of reforming catalyst 80), they can also be applied in flow adjustment elements, which are located between the electrolyte plate and the conductive plate. The reformer can apply the catalysts that are mixed in proportional variants, radially to maximize the production of product gas. All the reforming characteristics discussed above in relation to the external reformer and band are equally applicable to this internal reforming electrochemical converter. For example, interconnector plates 60 may include extended lip portions 72a and 72b, any of which may be used to preheat incoming reagents. The internal reforming electrochemical converter 40 of the present invention can be a fuel cell, such as a solid oxide fuel cell, molten carbonate fuel cell, alkaline fuel cell, phosphoric acid fuel cell and fuel cell of proton membrane. The preferred fuel cell of the present invention is a solid oxide fuel cell. The internal reforming electrochemical converter 40 of the present invention preferably has an operating temperature above 600 ° C and preferably between about 900 ° C and 1,100 ° C and more preferably about 1000 ° C. Those of ordinary skill in the art will appreciate that the illustrated bands of combustion, reforming and fuel electrode are simply representative of relative sites of electrochemical operations that occur during use of the converter 40 as a reformer. In another embodiment of the invention, the internal reforming electrochemical converter 40 can have any convenient geometrical configuration, such as a rectilinear configuration. The structure stacked in this way can include rectangular electrolyte plates 50 and rectangular interconnector plates 60 with multiple connected external to the plates. The electrode and catalytic materials can be applied in strips to the electrolyte plates perpendicular to the flow direction of the reagent. As illustrated in Figure 5, the fuel flow 24 is perpendicular to the elongated bands 92, 90 and 50b. The interconnector plates 60 conductively transfer thermal energy to the endothermic reformed catalyst web 90, the exothermic combustion catalyst web 92, and the exothermic fuel external band 50b, resulting substantially under exothermic conditions in plane as illustrated in Figure 6. Figure 6 graphically illustrates the isothermal temperature condition of the input reagents, for example hydrocarbon fuel, and reforming fuel which are established by the thermally conductive plate 60 during its passage over the electrolyte plate 50. The fuel temperature during Operation is defined by the axis of the ordinates and fuel flow retention is defined by the abscissa. In a reforming structure that does not use a thermally conductive plate to transfer heat in plane during operation, the fuel temperature varies greatly in the direction of fuel flow, as denoted by the waveform 110. As illustrated, the fuel of intake is initially preheated, such as by the projecting surfaces 72a and 72b. This pre-heating step 112 corresponds to an increase in the fuel temperature as it approaches the operating temperature of the converter 40. During the combustion or exothermic partial oxidation stage 114, the fuel temperature is further increased until the flow of the fuel is increased. The fuel reaches the reforming stage 116. The endothermic reforming stage requires a significant amount of thermal energy to sustain the reforming operation. The fuel then circulates to the reaction stage in the fuel cell 118, where the fuel is again heated, for example by the relatively hot operating environment of the converter 40. This sinusoidal type temperature profile 110 of the fuel decreases the efficiency total operational of the converter, as well as exposes certain components (the electrolyte plate 50) to inconvenient thermal stresses. The introduction of the conductive plate (interconnector) into the converter 40, "smoothes" the temperature profile and creates a substantially isothermal temperature condition, in plane and axially on the converter stack, through all the operation stages as illustrated by the isothermal profile 120. According to one mode of operation, the internal reforming electrochemical converter catalytically reforms the hydrocarbon fuel with H20 to produce H2 and CO, which in turn proceed to the fuel cell portion (e.g. the fuel electrode 50b) for generating electricity. It produces discharge species H20 and C02. The heat of the reaction of the exothermic fuel cell is transferred conductively in plane to the conductive plates to sustain the endothermic reforming reaction.

According to another mode of operation, the internal reforming electrochemical converter catalytically oxidizes the hydrocarbon fuel to produce H2 and CO, which proceeds to the fuel cell section for generating electricity. It produces the discharge species H20 and C02. The heat of the exothermic fuel cell reaction is preferred and transferred in conductive form to the conductive plates 70 to support the reforming reaction with slightly exothermic partial oxidation. The internal reforming electrochemical converter can be placed in an enclosure designed for pressurized operation. Another significant feature of the present invention is that the projecting heating surfaces 72D and 72C heat the reactants supplied from the oxidant and external fuel manifolds 47 and 48 to the operating temperature of the converter. Specifically, the extended surface 72D projecting to the oxidant manifold 47, heats the oxidizing reagent and the projecting surface 72C projecting to the fuel manifold 48 heats the fuel reagent. The highly conductive thermal interconnecting plate 60, facilitates the heating of the feed reagents by conductively transferring the heat from the fuel cell strip to the projecting surfaces or lip portions, thereby heating the feed reagents to the temperature operative The projecting surfaces in this way function as a thermal fin. This reagent heating structure provides a compact converter that is capable of thermally integrating into an energy system to achieve extraordinary system efficiency. The illustrated electrochemical converter 40 of the Figures 3 to 5, is also capable of chemical production and transformation, while concomitantly producing electricity in a co-production operation. According to this embodiment, the electrochemical converter 40 is adapted to receive electricity from a power source, which initiates an electrochemical reaction within the converter and reduces selected contaminants contained within the reactant of entry into benign species. Therefore, for example the electrochemical converter 40 can be coupled to a discharge source containing selected contaminants including NOx, and hydrocarbon species. The converter 40 catalytically reduces contaminants in benign species including, N2, 02 and C02.

From this it will be seen that the invention efficiently achieves the objectives set forth above, between those apparent from the preceding description. Since certain changes can be practiced in the above constructions without departing from the scope of the invention, it is intended that all matter contained in the above description or illustrated in the accompanying drawings, be interpreted as illustrative and not in a limiting sense. It is also understood that the following claims will cover all the generic and specific characteristics of the invention described herein, and all the declarations of the scope of the invention which, as a matter of language, could be said to fall between them. Having described the invention, what is claimed is:

Claims (127)

1. CLAIMS 1.- A plaque-type reformer for reforming a reactant in reaction species during operation, the reformer is characterized in that it comprises: a plurality of catalyst plates, having one or more catalyst materials associated to promote reforming and a plurality of conductive plates formed of a thermally conductive material, the catalyst plates and the conductive plates are stacked alternately to form a reforming structure, the conductive plates conductively transfer thermal energy in plane to sustain the reforming process.
2. 2. The reformer according to claim 1, characterized in that the reforming process includes one or more reforming reactions, the reforming reactions include a catalytically assisted chemical reaction between two or more reaction species, and a catalytically assisted thermal dissociation. of a single species. 3. - The reformer according to claim 1, characterized in that the reforming structure includes at least one axial manifold for introducing the reagent and at least one manifold to allow the reaction species to leave the reforming structure. 4. - The reformer according to claim 1, characterized in that the reforming structure has an exposed peripheral surface for exchanging thermal energy with an external environment. 5. - The reformer according to claim 1, characterized in that the reforming structure includes at least one axial reagent manifold for introducing the reactant and a peripheral discharge means, for discharging the reaction species from a peripheral portion of the structure of reformed. 6. - The reformer according to claim 1, characterized in that it further comprises a gas-tight, thermally conductive housing disposed with respect to the stacked reforming structure to form a peripheral axial manifold and means for allowing the reaction species to enter the manifold peripheral axial, where the reaction species are captured by the gas-tight housing. 7. - The reformer according to claim 1, characterized in that it also includes a gas-tight, thermally conductive housing that has means for exchanging thermal energy with the external environment and the conductive plate for one of radiation, conduction and convection. 8. - The reformer according to claim 1, characterized in that an outer surface of the reforming structure contacts an inner surface of a gas-tight housing, the gas-tight housing is capable of conductively transferring thermal energy to the conductive plates. 9. - The reformer according to claim 1, characterized in that it also comprises a gas-tight enclosure, of cylindrical configuration to allow operation of reformer under pressure. 10. - The reformer according to claim 1, characterized in that the conductive plate includes means for providing a generally isothermal condition, in plane of the conductive plate. 11. - The reformer according to claim 1, characterized in that the reforming structure includes at least one axial reagent manifold for introducing the reagent, and wherein the conductive plates include tension means integrally formed and extending in the manifold of axial reagent to preheat an entry reagent. 12. - The reformer according to claim 1, characterized in that at least one of the conductive plate and the catalyst plate includes a plane surface having passage means to allow the reagent to circulate on the surface of the plate. 13. - The reformer according to claim 1, characterized in that it also includes an axial manifold formed within the reforming structure, passage means formed between the conductive plate and the catalyst plate, and means for generating a reagent flow pressure drop through the passage means between the conductive plate and the catalyst plate which is substantially greater than the drop of Reagent flow pressure within the axial manifold. 14. - The reformer according to claim 1, characterized in that it also includes passage means formed between the catalyst and conductive plates, to allow an entry reagent to pass over a surface of one of the plates, the passage means maintain a Substantially uniform pressure drop, to provide a substantially uniform flow of reagent onto an axis of the reforming structure. 15. - The reformer according to claim 1, characterized in that it includes means for producing a substantially uniform temperature condition on an axis of the reforming structure. 16. - The reformer according to claim 1, characterized in that the catalyst plate is formed of a porous catalyst material, the porous material forms passage means to allow an input reagent to pass through at least a portion of the plate. 17. - The reformer according to claim 1, characterized in that the thermally conductive plate is formed of a conductive porous material, the porous material forms passage means to allow an entry reagent to pass through the plate. 18. - The reformer according to claim 1, characterized in that the conductive plate is composed of at least one of a non-metal such as silicon carbide and a composite material. 19. - The reformer according to claim 1, characterized in that the conductive plate is composed of at least one metal such as aluminum, copper, iron, steel alloys, nickel, nickel alloys, chromium, chromium alloys, platinum and platinum alloys. 20. The reformer according to claim 1, characterized in that the catalyst plate is composed of a ceramic support plate having a coating of catalyst material. 21. The reformer according to claim 1, characterized in that the catalyst material is selected from the group consisting of platinum, palladium, nickel, nickel oxide, iron, chromium iron oxide, chromium oxide, cobalt oxide, copper , copper oxide, zinc, zinc oxide, molybdenum, molybdenum oxide and other suitable transition metals and their oxides. 22. The reformer according to claim 1, characterized in that the catalyst plate is composed of at least one of platinum, nickel, nickel oxide, chromium and chromium oxide. 23. - The reformer according to claim 1, characterized in that the reagent includes a hydrocarbon species and at least one of 02, H20 and C02. 24. - The reformer according to claim 1, characterized in that the reagent includes at least one of alkane, a hydroxyl, a hydrocarbon bonded with a carboxyl, a hydrocarbon bonded with a carbonyl, an hydrocarbon of olefin, a hydrocarbon bound with an ether , a hydrocarbon bonded with an ester, a hydrocarbon bonded with an amine, a hydrocarbon bonded with an aromatic derivative, and a hydrocarbon bonded with another derived organ. 25. - The reformer according to claim 1, characterized in that it also includes means for coupling the reaction species leaving the reformer to an external fuel cell. 26. The reformer according to claim 23, characterized in that the hydrocarbon fuel and at least one of H20 and C02 undergo an endothermic catalytic reforming to produce H20 and C02, the energy requirements for the endothermic reforming are supplied by energy produced by an external fuel cell, the energy is transferred from the fuel cell through the conductive plate through thermal conduction in plane. 27. The reformer according to claim 23, characterized in that the hydrocarbon fuel and 02 are subjected to catalytic combustion and reforming to produce H20 and C02, and at least one of exothermic combustion and an exothermic reaction of an external fuel cell that It supplements the energy requirements for the endothermic reforming through the thermal conduction in plane of the conductive plate. 28. The reformer according to claim 23 or 24, characterized in that the C02 and H20 are subjected to a catalytic displacement reaction to form C02 and H20. 29. The reformer according to claim 1, characterized in that the reforming structure has a substantially cylindrical shape. 30. The reformer according to claim 1, characterized in that the reforming structure is cylindrical and at least one of the catalyst plate and the conductive plate has a diameter between approximately 2.54 cm (1") and approximately 50.8 cm (20"). ) and has a thickness between approximately .00508 cm (.002") and approximately .508 cm (.2"). 31. The reformer according to claim 1, characterized in that the reforming structure has a substantially rectangular shape. 32.- The reformer for a reactive reaction species during operation, the reformer is characterized in that it comprises: a porous and thermally conductive material interdispersed with one or more catalyst materials to form a reforming structure, the thermally conductive material transfers thermal energy to sustain or support the reforming process. 33.- A plate type reformer for reforming a reactive species during operation, the reformer is characterized in that it comprises: a plurality of plates composed of a thermally conductive material interspersed with one or catalytic materials to promote the reforming process; plates are stacked together to form a reforming structure, the plates conductively transfer thermal energy in plane of the plates to sustain the reforming process. 34. - A reformer according to claim 32 or 33, characterized in that the reforming structure includes at least one axial manifold for introducing the reagent and at least one manifold to allow the reaction species to leave the reforming structure. The reformer according to claim 32 or 33, characterized in that the reforming structure has an exposed peripheral surface for exchanging thermal energy with an external environment. 36.- The reformer according to claim 32 or 33, characterized in that the reforming structure includes at least one axial reagent manifold for introducing the reagent and peripheral discharging means for the reaction species from a peripheral portion of the structure of the reagent. reformed. The reformer according to claim 32 or 33, characterized in that it further comprises a gas-tight, thermally conductive housing disposed with respect to the reforming structure to form a peripheral axial manifold and means for allowing the reaction species to enter to the peripheral axial manifold, wherein the reaction species are captured by the gas-tight housing. 38.- The reformer according to claim 32 or 33, characterized in that it also includes a gas-tight, thermally conductive housing that has means for exchanging thermal energy with the external environment and the reforming structure for one of radiation, conduction and convection . 39.- The reformer according to claim 32 or 33, characterized in that an outer surface of the reforming structure contacts an inner surface of a gas-tight housing, the gas-tight housing is capable of conductively transferring thermal energy to the reformed structure. 40.- The reformer according to claim 32 or 33, characterized in that it also comprises a gas tight enclosure of cylindrical configuration to allow operation of a reformer under pressure. 41. The reformer according to claim 32 or 33, characterized in that the reforming structure includes means for providing a generally isothermal condition through the reforming structure. 42. - The reformer according to claim 32 or 33, characterized in that the reforming structure includes at least one axial reagent manifold for introducing reactants, and wherein the reforming structure includes integrally formed tension means and extending in the axial reagent manifold to pre-heat the reagent. 43.- The reformer according to claim 32 or 33, characterized in that the reforming structure includes passage means to allow the reagent to circulate through the structure. 44. - The reformer according to claim 32 or 33, characterized in that it also includes an axial manifold formed within the reforming structure, reactive passage means for allowing a reagent to circulate in the plane of the reforming structure, and means for generating a reactive flow pressure drop through the passage means that are substantially greater than the reactive flow pressure drop within of the axial manifold. 45. - The reformer according to claim 43, characterized in that the passage means maintain a substantially uniform pressure drop to provide substantially uniform flow of reagents on an axis of the reforming structure. 46.- The reformer according to claim 32 or 33, characterized in that it also includes means for producing a substantially uniform temperature condition on an axis of the reforming structure. 47. - The reformer according to claim 32 or 33, characterized in that the conductive material is composed of a non-metal such as silicon carbide and a composite material. 48. The reformer according to claim 32 or 33, characterized in that the conductive material is composed of at least one metal such as aluminum, copper, iron, steel alloys, nickel, nickel alloys, chromium, chromium alloys, platinum and platinum alloys. 49. - The reformer according to claim 32 or 33, characterized in that the catalyst material is selected from the group consisting of platinum, palladium, nickel, nickel oxide, iron, iron oxide chromium, chromium oxide, cobalt oxide , copper, copper oxide, zinc, zinc oxide, molybdenum, molybdenum oxide, other suitable transition metals and their oxides. 50. - The reformer according to claim 32 or 33, characterized in that the reagent includes a hydrocarbon species and at least one of 02, H20 and C02. 51.- The reformer according to claim 32 or 33, characterized in that it also includes means for coupling the reaction species leaving the reformer to an external fuel cell. 52. - The reformer according to claim 32 or 33, characterized in that the reagent includes a hydrocarbon fuel and at least one of H20 and C02, which undergo catalytic reforming to produce H2, CO, H20 and C02, and where an exothermic reaction of an external fuel cell, supplements the energy requirements for the endothermic reforming reaction of the reforming structure through the thermally conductive material. 53. - The reformer according to claim 32 or 33, characterized in that the reagent includes a hydrocarbon fuel and at least one of H20 and C02, which are subjected to catalytic combustion and reformed to produce H2, CO, H20 and C02, and at least one of an exothermic combustion and an exothermic reaction of an external fuel cell, supplements the energy requirements for the endothermic reforming reaction of the reforming structure through the thermally conductive material. 54. - The reformer according to claim 32 or 33, characterized in that the reforming structure has a substantially cylindrical shape. 55. - The reformer according to claim 32 or 33, characterized in that the reforming structure is cylindrical and has a diameter between approximately 2.54 cm (1 in) and approximately 50.8 cm (20 in). 56.- The reformer according to claim 32 or 33, characterized in that the reforming structure has a substantially rectangular shape. 57.- A burner for oxidizing a hydrocarbon fuel to produce thermal energy, the burner is characterized in that it comprises: a plurality of conductive plates formed of a thermally conductive material and a plurality of catalyst plates having one or more oxidizing catalyst materials, the plates catalysts and conductive plates are stacked alternately to form a burner structure, wherein the catalyst material of the catalyst plate promotes the oxidation of the hydrocarbon fuel to form a resultant species, and wherein the conductive plates are capable of transferring thermal energy produced during the oxidation process to the surrounding medium by one of radiation, conduction and convection. 58. - The burner according to claim 57, characterized in that the burner structure has an exposed peripheral surface for exchanging thermal energy with an external environment. 59. - The burner according to claim 57, characterized in that the burner structure includes at least one of an axial reagent manifold for introducing the reagent and peripheral discharging means for discharging the reaction species from a peripheral portion of the structure of burner. 60. - The burner according to claim 57, characterized in that it also includes a thermally conductive housing arranged with respect to the burner structure and having means for exchanging thermal energy with the external environment and the conductive plate for radiation, conduction and convexion 61.- The burner according to claim 57, characterized in that an outer surface of the burner structure contacts an inner surface of a thermally conductive housing disposed with respect to the burner structure, the housing conductively transfers the thermal energy from the burners. conductive plates during operation. 62. - The burner according to claim 57, characterized in that the conductive plate includes means for providing a generally isothermal condition in the plane of the conductive plate. 63. - The burner according to claim 57, characterized in that the burner structure includes at least one axial reagent manifold for introducing the reagent, and wherein the conductive plates include tension means integrally formed and extending to the axial reagent manifold for preheating the hydrocarbon fuel. 64. - The burner according to claim 57, characterized in that a plane surface of at least one of the conductive plate and the catalyst plate includes passage means for allowing the hydrocarbon fuel to flow on the surface of the plate. The burner according to claim 57, characterized in that it also includes an axial manifold formed within the burner structure, passage means formed on a plane surface of one of the conductive plate and the catalyst plate, to allow fuel circulates on the plate surface, and means for generating a reagent flow pressure drop across the passage means that is substantially greater than the reactive flow pressure drop within the axial manifold. 66. - The burner according to claim 64, characterized in that the passage means maintain a substantially uniform pressure drop to provide a substantially uniform flow of the reagent onto an axis of the burner structure. 67. - The burner according to claim 57, characterized in that it also includes means for producing a substantially uniform temperature condition on an exterior surface of the burner structure. The burner according to claim 64, characterized in that the catalyst plate is formed of a porous catalyst material, the porous material forms the passage means and allows the reagent to pass through the plate. 69.- The burner according to claim 64, characterized in that the thermally conductive plate is formed of a porous conductive material, the porous material forms the passage means and allows the reagent to pass through the plate. 70. - The burner according to claim 57, characterized in that the conductive plate is composed of silicon carbide. 71.- The burner according to claim 57, characterized in that the conductive plate is composed of at least one refractory material. 72. - The burner according to claim 57, characterized in that the catalyst plate is composed of a ceramic support plate having the coated catalyst material. 73. - The burner according to claim 72, characterized in that the catalyst coating is selected from the group consisting of at least one of platinum, nickel, nickel oxide, chromium and chromium oxide. 74. - The burner according to claim 57, characterized in that the catalyst plate is composed of at least one of platinum, nickel, nickel oxide, chromium and chromium oxide. The burner according to claim 57, characterized in that the hydrocarbon fuel is pre-mixed with an oxidizing reagent before introduction to or into the axial manifold. 76. - The burner according to claim 57, characterized in that the burner structure has a substantially cylindrical shape. The burner according to claim 57, characterized in that the burner structure is cylindrical and at least one of the catalyst plate and the conductive plate has a diameter between approximately 2.54 cm (1") and approximately 50.8 cm (20"). ) and has a thickness between approximately .00508 cm (.002") and approximately .508 cm (.2"). 78.- A burner for oxidizing a hydrocarbon fuel to produce thermal energy, the apparatus is characterized in that it comprises: a porous and thermally conductive material interspersed with one or more catalyst materials, to form a burner structure, wherein the catalyst material promotes the oxidation of the hydrocarbon fuel to form resulting species, and where the conductive material is capable of transferring thermal energy produced during the oxidation process to the surrounding medium, by radiation, conduction and convection. 79.- Burner for oxidizing a hydrocarbon fuel to produce thermal energy, the apparatus is characterized in that it comprises: a plurality of plates composed of a thermally conductive material interspersed with one or catalytic materials, the plates are stacked together to form a burner structure , wherein the catalyst material promotes the oxidation of the hydrocarbon compound to form the resulting species, and wherein the conductive material transfers thermal energy produced during the oxidation process to the surrounding medium by one of radiation, conduction and convection. 80. - An electrochemical converter, characterized in that it comprises: a plurality of gas-tight electrolyte plates, having reactive materials arranged on both sides, the plates have a fuel flow side and have the reactive material disposed selected from the group which consists of at least one of a combustion catalyst, a reforming catalyst, a displacement catalyst and a fuel electrode material, the plates have an oxidant flow having the reactive material disposed selected from the group consisting of a material of oxidizing electrode, a plurality of gas-tight conductive plates formed of a thermally conductive material; the electrolyte plates and conductive plates are stacked alternately to each other to form a stacked plate structure, and internal reforming means for pre-heating and reforming a hydrocarbon fuel on the fuel flow side of the electrolyte plate within the Stacked plate structure, reforming is aided by conductive plates that are capable of conductively transferring heat from a fuel cell reaction portion of the stacked plate structure. 81.- The electrochemical converter according to claim 80, characterized in that the electrolyte plate forms a means for an electrolytic ion transfer action. 82. - The electrochemical converter according to claim 80, characterized in that the converter performs chemical transformation and production while consuming oxygen to produce electricity. 83. The electrochemical converter according to claim 80, characterized in that one side of the conductive plate faces the fuel flow side having at least one of the combustion catalyst, the reforming catalyst and the displacement catalyst disposed. 84. - The electrochemical converter according to claim 80, characterized in that at least one of the combustion catalyst, the reforming catalyst and the displacement catalyst, can be applied in a flow adjusting element, the flow adjustment element is placed between the electrolyte plate and the conductive plate. 85.- The electrochemical converter according to claim 80, characterized in that it also comprises a plurality of axial multiples formed in the stacked plate structure, at least one of the multiple is adapted to receive a hydrocarbon fuel reagent and to allow the fuel circulate on a surface of the electrolyte plate and exit at an outer edge of the plates; and at least one of the multiples is adapted to receive an oxidant reagent and allow the oxidant to flow on the other side of the reagent plate and exit at the outer edge of the plates. 86.- The electrochemical converter according to claim 80, characterized in that the stacked plate structure has a rectangular configuration with an edge that is adapted to receive a hydrocarbon fuel reagent, the reagent circulates within the space on a surface of the plates of electrolyte and leaves an opposite plate edge; and a third plate edge is adapted to receive an oxidizing reagent that circulates within a space on the other surface of the electrolyte plate and exits from a fourth plate edge. 87. The electrochemical converter according to claim 80, characterized in that the conductive plates include means for regulating the flat temperature distribution of the stacked plate structure to achieve a substantially flat isothermal condition. 88.- The electrochemical converter according to claim 85, characterized in that the manifolds provide means for regulating the distribution of uniform flow within the spaces between the plates on the axis of the stacked structure, to provide an axially isothermal condition. 89.- The electrochemical converter according to claim 80, characterized in that the thermally and electrically conductive material of the interconnector plate is composed of at least one non-metal. 90. The electrochemical converter according to claim 80, characterized in that the thermally and electrically conductive material of the interconnector plates is composed of at least one of nickel, nickel alloys, chromium, chromium alloys, platinum and platinum alloys. 91.- The electrochemical converter according to claim 80, characterized in that the thermally and electrically conductive material of the interconnector plate is composed of at least one of aluminum, copper and steel alloys. 92. - The electrochemical converter according to claim 80, characterized in that the fuel electrode is composed of at least one of nickel, a compound containing nickel, chromium and a compound containing chromium. The electrochemical converter according to claim 80, characterized in that the fuel catalyst is composed of at least one of platinum, composed of platinum, nickel and nickel compound. 94. The electrochemical converter according to claim 80, characterized in that the reforming catalyst is composed of at least one of nickel, a compound containing nickel, chromium and a chromium-containing compound. 95. The electrochemical converter according to claim 80, characterized in that the reforming catalyst is composed of at least one of platinum, palladium, nickel, nickel oxide, iron, iron oxide, chromium, chromium oxide, cobalt, Cobalt oxide, copper, copper oxide, zinc, zinc oxide, molybdenum and molybdenum oxide. 96. The electrochemical converter according to claim 80, characterized in that partial oxidation occurs on the combustion catalyst formed on a surface of at least one of the electrolyte plate and the conductive plate. 97. The electrochemical converter according to claim 80, characterized in that the internal reforming reaction occurs on the reforming catalyst on a surface of the electrolyte plate and the conductive plate. 98. The electrochemical converter according to claim 80, characterized in that the fuel cell reaction occurs on the reaction material of the electrolyte plate. 99. The electrochemical converter according to claim 80, characterized in that the reforming catalyst and the fuel electrode material are mixed on the surface of the electrolyte plate to substantially simultaneously reform the fuel and create the electrochemical reaction during operation. 100.- The electrochemical converter according to claim 80, characterized in that the combustion catalyst, the reforming catalyst and the fuel electrode material are mixed on the surface of the electrode plate to initiate in a substantially simultaneous form partial oxidation. and reforming a fuel reagent. 101.- The electrochemical converter according to claim 80, characterized in that a hydrocarbon fuel introduced to the converter catalytically reforms in the presence of H20, the fuel to produce H2 and CO, and the reformed fuel is subjected to a fuel cell reaction to form a kind of discharge that contains H20 and C02; wherein the heat of the reaction of the exothermic fuel cell is transferred in a conductive manner in plan to the conductive plates to sustain the endothermic reforming reaction. 102. - The electrochemical converter according to claim 80, characterized in that a hydrocarbon fuel introduced to the converter partially catalytically burns 02 to produce H2 and CO, and the partially burned fuel is subjected to an exothermic fuel cell reaction to form a kind of discharge that contains H20 and C02; wherein the heat generated from the reaction of the exothermic fuel cell is transferred conductively in plane to the conductive plates to provide a temperature sufficient to withstand the reforming reaction with slight exothermic partial oxidation. 103. The electrochemical converter according to claim 80, characterized in that the reagent includes at least one of alean hydroxyl, a hydrocarbon bonded with a carboxyl, a hydrocarbon bonded with a carbonyl, an hydrocarbon olefin, a hydrocarbon bound with an ether , a hydrocarbon bonded with an ester, a hydrocarbon bonded with an amine, a hydrocarbon bonded with an aromatic derivative, and a hydrocarbon bonded with other organ derivatives. 104.- The electrochemical converter according to claim 80, characterized in that the converter is a fuel cell selected from the group crue consisting of a solid oxide fuel cell, molten carbonate fuel cell, alkaline fuel cell, proton exchange membrane fuel and phosphoric acid fuel cell. 105. The electrochemical converter according to claim 80, characterized in that the electrolyte plate is composed of one of one of materials based on zirconium oxide and materials based on ceric oxide. 106. The electrochemical converter according to claim 80, characterized in that it also includes internal reactive heating means disposed within one of the manifolds for heating at least a portion of at least one of the reagents passing through the manifold. 107.- The electrochemical converter according to claim 106, characterized in that the internal reagent heating means comprise a thermally conductive and integrally formed surface of the conductive plate, which projects at least one of the multiple. 108. The electrochemical converter according to claim 107, characterized in that the reaction of the fuel cell generates waste heat that heats the reagents to approximately the operating temperature, and the waste heat is transferred in a conductive manner to the reactants by the interconnection plate and the extended surface. 109. The electrochemical converter according to claim 80, characterized in that it also includes peripheral discharge means for discharging the reformed fuel from a peripheral portion of the stacked plate structure. 110. The electrochemical converter according to claim 80, characterized in that at least one of the conductive plate and the electrolyte plate includes reactive passage means to allow the reagent to pass from the axial reagent manifold onto the surface of the plates. 111. The electrochemical converter according to claim 110, characterized in that the passage means include means for maintaining a substantially uniform pressure drop on at least one surface of the plates to provide a substantially uniform flow of reagent onto the plate surfaces. . 112. - The electrochemical converter according to claim 110, characterized in that the reagent coating of the electrolyte plate is porous "the porous coating forms the reagent passage means. 113. The electrochemical converter according to claim 80, characterized in that it also includes means for generating a reagent flow pressure drop through a space formed between the conductive plate and the opposite electrolyte plate which is substantially greater than the Reagent flow pressure drop within the axial manifold. 114. The electrochemical converter according to claim 80, characterized in that it further includes means for producing a substantially uniform radial flow distribution of reagents through the stacked plates. 115. - The electrochemical converter according to claim 80, characterized in that the stacked plate structure is cylindrical and at least one of the electrolyte plate and the conductive plate, has a diameter between approximately 2.54 cm (1") and approximately 50.8 cm (20") and has a thickness between approximately .00508 cm (.002") and approximately .508 cm (.2"). 116. - The electrochemical converter according to claim 80, characterized in that it also comprises a hermetic enclosure a gas, of cylindrical configuration, configured to surround the stacked plates to allow operation of reformer under pressure 117. The electrochemical converter according to claim 80, characterized in that the converter is an electrochemical catalytic converter that is adapted to receive electricity from a remote power source, electricity initiates an electrochemical reaction inside the converter that adapts to To reduce selected contaminants contained within the reagents of income in benign species. 118. - The electrochemical converter according to claim 116, characterized in that the catalytic converter further includes means for receiving an exhaust containing select pollutants, including NOx and hydrocarbon species, the catalytic converter includes means for reducing NOx and hydrocarbon species in benign species, including one of N2, 02 and C02. 119.- Catalytic converter, characterized in that it comprises: a plurality of gas-tight converter plates having on a first side of hydrocarbon gas, a reactive material consisting of one of a converter catalyst and a first electrode material; and disposed on a second side of buffer gas, a reactive material consisting of a second electrode material; a plurality of gas-tight conductive plates formed of a thermally conductive material; the converter plates and conductive plates are alternately stacked together to form a converter structure; means for introducing a hydrocarbon gas to the hydrocarbon gas side of the converter plate and introducing a buffer gas to the second side of the buffer gas of the converter plate; means for receiving electricity from a remote power source; and means to convert hydrocarbon gas into benign species. 120.- The converter according to claim 19, characterized in that the conductive plates include means for achieving a generally isothermal plane condition of the conductive plates. 121. The converter according to claim 19, characterized in that the converter plate is formed of a substantially gas-tight electrolyte material. 122. The converter according to claim 19, characterized in that the converter plate is a gas-tight ionic conductor. 123. The converter according to claim 19, characterized in that the electrode coatings of at least one side of the converter plate include nickel or a nickel-containing compound. 124. The converter according to claim 19, characterized in that the electrode coatings of at least one side of the converter plate include platinum. 125. The converter according to claim 19, characterized in that the electrode coating of at least one side of the converter plate includes palladium. 126. The converter according to claim 19, characterized in that the electricity received by the converter initiates an electrochemical reaction that reduces the selected contaminants within the hydrocarbon gas to benign species. 127.- The converter according to claim 19, characterized in that the structure is adapted to receive exhaust containing select pollutants, including NOx and hydrocarbon species, the catalytic converter further includes means for reducing NOx and hydrocarbon species to benign species. SUMMARY OF THE INVENTION A natural gas reformer (10) comprising a stack of thermally conductive plates (12) interdispersed 812) with catalyst plates (14) and provided with internal or external manifolds or manifolds for reagents. The catalyst plate is in intimate thermal contact with the conductive plates in such a way that its temperature closely follows the temperature of the thermally conductive plate, which can be designed to reach an almost isothermal state in-plane to the plate. One or more catalysts, distributed over the direction of flow, can be employed in plan to the thermally conductive plate in a variety of optional embodiments. The reformer can be operated as a steam reformer or as a partial oxidation reformer. When operating as a steam reformer, thermal energy is externally provided for the steam reforming reaction (endothermic), by radiation and / or conduction to the thermally conductive plates. This produces carbon monoxide, hydrogen, vapor and carbon dioxide. When operating as a partial oxidation reformer, a fraction of natural gas is oxidized assisted by the presence of a combustion catalyst and a reforming catalyst. This produces carbon monoxide, hydrogen, vapor and carbon dioxide. Due to the intimate thermal contact between the catalyst plate and the conductive plates, excessive temperature can not develop within the stack structure. Plate design details can be varied to fit a variety of manifold or manifold modes, by providing one or more inlet and outlet gates, to introduce preheat and reagent discharge. RS / frp / 31/16184