CN101447579A - Circular fuel processor and method thereof - Google Patents

Abstract

The invention relates to a circular fuel processor and method thereof, in particular a method for producing hydrogen in a fuel processor. The fuel processor (15) comprises a reformer (32) and a heater (30). The reformer (32) includes a catalyst that facilitates the production of hydrogen. A large-scale reformer increases hydrogen from given fuel processor size by increasing volume of the catalyst in the reformer. The heater provides heat to the reformer. One or more buners can surround a plurality of edges of the reformer to increase heat transmission. A dewar container further increases heat management of the fuel processor (15) and efficiency of the burner. The dewar container includes one or a plurality of dewar containers for receiving the air before the burner receives inlet air (31). The air can be preheated in the dewar container chamber by heat generated by the burner (30).

Description

Annular fuel processor and method

The application divides an application as the application number 200480024619.0 of enjoying June 25 2004 applying date and title " annular fuel processor and method ".

Technical field

The present invention relates to fuel cell technology.Particularly, the present invention relates to produce hydrogen and be applicable to fuel processor in the portable application situation.

Background technology

Fuel cell electrochemically in conjunction with hydrogen and oxygen to produce.Surrounding air is easy to supply oxygen.Yet providing of hydrogen needs practical feeding mechanism.Gaseous Hydrogen has low energy densities, has reduced the operability as portable fuel thus.Liquified hydrogen with suitable energy density must store under extremely low temperature and condition of high voltage, this make liquified hydrogen storage and transport pretty troublesome.

The reformer hydrogen feeding mechanism is by handling fuels sources to produce hydrogen.Fuels sources is as hydrogen carrier.The hydrocarbon fuel sources that can get comprises methyl alcohol, ethanol, gasoline, propane and natural gas at present.The liquid hydrocarbon fuels source provides high-energy-density and the ability that is easy to store and transport.Fuel processor is reformed to produce hydrogen to hydrocarbon fuel.

The development of fuel cell has concentrated on the generator of large-scale application situation as the industrial size that is used for power supply stand-by so far.Current lithium ion battery and the similar battery technology of depending on of consumption electronic product and other portable electrical power applications.The fuel processor that is used for portable application situation such as electronic installation is desirable but also can't obtains commercial.In addition, the technology of minimizing fuel processor size or increase fuel processor efficient will be highly useful.

Summary of the invention

This aspect relates to a kind of fuel processor that is produced hydrogen by fuels sources.Described fuel processor comprises reformer and burner.Described reformer includes and is beneficial to the catalyst that is produced hydrogen by described fuels sources.Providing has increased the amount that can be used for the catalyst in the reformer and has increased the big volume reformer chamber design of exporting for the hydrogen of given fuel processor size.Described burner offers described reformer with heat.Thereby one or more burners can be configured to increase the heat transmission of carrying out to described reformer around reformer on many limits.

Also described by reducing thermal loss and increasing the Dewar type container (dewar) that combustor efficiency is improved the heat management of fuel processor.Dewar type container is included in reactor and receives the one or more Dewar type containers chamber that receives them before entry process gas or the liquid.Described Dewar type container is arranged such that by the entry process gas of described Dewar type container chamber or liquid and blocked the heat that produces in the described burner before heat is overflowed described fuel processor.Make entry process gas or liquid carry out three kinds of functions by the Dewar type container chamber by this way: the heat that a) produces in burner initiatively cools off and the dissipation heat before arriving described fuel processor outside, and b) heated air before air is received by described burner, and c) absorbs heat and heat recirculation is returned into the interior efficient with the increase burner of burner.When described burner relied on catalytic combustion to produce heat, the heat that produces in the described burner warmed the cooling procedure gas in the described burner according to the temperature of described process gas or liquid.This has stolen heat, reduced the efficiency of heating surface of burner and has caused greater amount ground to consume described fuels sources usually from described reformer.Therefore described Dewar type container carries out preheating so that described burner makes less heat arrive described process gas or liquid to it before arriving burner introducing process gas or liquid, described heat otherwise will be passed to described reformer.

In one aspect, the present invention relates to a kind of fuel processor that is used for producing hydrogen by fuels sources.Described fuel processor comprises and is configured to receive described fuels sources, is configured to export hydrogen and includes the reformer that is beneficial to the catalyst that produces hydrogen.Described fuel processor also comprises the boiling device that is configured to the described fuels sources of heating before described reformer receives described fuels sources.Described fuel processor further comprises and is configured to that heat offered described reformer and is arranged at least one burner around the described reformer annularly.Described fuel processor also can comprise the boiling device of the feed fluid fuel that heats described burner.

In one aspect of the method, the present invention relates to a kind of fuel processor that is used for producing hydrogen by fuels sources.Described fuel processor comprises and is configured to receive described fuels sources, is configured to export hydrogen and includes the reformer that is beneficial to the catalyst that produces hydrogen.Described reformer also comprises having greater than about 0.1 cubic centimetre and less than the reformer chamber of about 50 cubic centimetres volume and be characterised in that cross-sectional width and greater than the cross-sectional height of 1/3rd described cross-sectional width.Described fuel processor also comprises the boiling device that is configured to the described fuels sources of heating before described reformer receives described fuels sources.Described fuel processor further comprises at least one burner that is configured to heat is offered described reformer.

In a further aspect, the present invention relates to a kind of fuel processor that is used for producing hydrogen by fuels sources.Described fuel processor comprises and is configured to receive described hydrogen fuel source, is configured to export hydrogen and includes the reformer that is beneficial to the catalyst that produces hydrogen.Described fuel processor also comprises the burner that is configured to heat is offered described reformer.Described fuel processor further comprises and comprises described reformer and described burner at least in part and comprise and form the one group of Dewar type container wall that is configured to receive the Dewar type container chamber of described entry process gas or liquid before described burner receives entry process gas or liquid.Described fuel processor additionally comprises housing, and described housing comprises the one group of shell wall that comprises described Dewar type container at least in part and the exterior mechanical protection is provided for described reformer and described burner.

In aspect another, the present invention relates to a kind of method that is used for managing the heat of fuel processor.Described fuel processor comprises burner, reformer and comprises the Dewar type container of described burner at least in part.Described method is included in the described burner and produces heat.Described method also comprises makes entry process gas or liquid by the Dewar type container chamber.Described method comprises that further the heat that produces in the described burner of use heats described entry process gas or the liquid in the described Dewar type container chamber.

In one aspect of the method, the present invention relates to a kind of method that is used for producing hydrogen at fuel processor.Described fuel processor comprises burner, reformer and comprises the Dewar type container of described burner and described reformer at least in part.Described method is included in the described burner and produces heat.Described method also comprises makes entry process gas or liquid by the Dewar type container chamber.Described method comprises that further the heat that produces in the described burner of use heats described entry process gas or the liquid in the described Dewar type container chamber.Described method additionally is included in described entry process gas or liquid and it is supplied to described burner after being heated in described Dewar type container chamber.Described method comprises that also the heat transferred that will produce in the described burner is to described reformer.Described method further comprises reforms to produce hydrogen to fuels sources.

In one aspect, the present invention relates to a kind of fuel processor that is used for producing hydrogen by fuels sources.Described fuel processor comprises reformer, and described reformer comprises the one group of reformer channels that is arranged in first substrate.Described reformer also includes and is beneficial to the reformer catalyst that is produced hydrogen by described fuels sources.Described fuel processor further comprises boiling device, and described boiling device comprises the one group of passage that is arranged in second substrate and is configured to the described fuels sources of heating before described reformer receives described reformer.Described fuel processor also comprises the burner that is configured to that heat offered described reformer and is configured to heat is offered described boiling device.Described fuel processor additionally comprise be configured to by apply pass a part described first substrate and a part described second substrate submissive fastening force to keep the depressed place portion of described reformer and the position of described boiling device in described fuel processor.

In one aspect of the method, the present invention relates to a kind of fuel processor that is used for producing hydrogen by fuels sources.Described fuel processor comprises reformer, and described reformer comprises the one group of reformer channels that is arranged in first substrate.Described reformer also includes and is beneficial to the reformer catalyst that is produced hydrogen by described fuels sources.Described fuel processor further comprises boiling device, and described boiling device comprises the one group of passage that is arranged in second substrate and is configured to the described fuels sources of heating before described reformer receives described fuels sources.Described fuel processor also comprises catalytic burner, and described catalytic burner includes and be beneficial to the catalyst that uses described fuels sources to produce heat, be configured to that heat offered described first substrate and described second substrate and comprise one group of passage in one that is arranged in described first substrate and described second substrate.

In a further aspect, the present invention relates to a kind of fuel processor that is used for producing hydrogen by fuels sources.Described fuel processor comprises reformer, and described reformer comprises the one group of reformer channels that is arranged in first substrate.Described reformer also includes and is beneficial to the reformer catalyst that is produced hydrogen by described fuels sources.Described fuel processor further comprises the burner that is configured to heat is offered described reformer.Described fuel processor also comprises the Dewar type container that comprises described reformer and described burner and comprises that formation is configured to receive one group of Dewar type container wall of the Dewar type container chamber of described fuels sources or oxygen before described reformer receives described fuels sources or oxygen.

In following description of the present invention and relevant drawings, will be described these and further feature of the present invention and advantage.

Description of drawings

Figure 1A shows the fuel cell system that is used to produce electric energy according to an embodiment of the invention;

Figure 1B shows the schematic operation according to the fuel cell system shown in Figure 1A of a specific embodiment of the present invention;

Fig. 1 C shows and makes hydrogen move to an embodiment of the fuel cell system shown in the Figure 1A of the burner the fuel processor by route from the anode outlet of fuel cell;

Fig. 2 A shows the sectional view of the fuel processor of the fuel cell system shown in the Figure 1A of being used for according to an embodiment of the invention;

Fig. 2 B shows along the front cross sectional view of the fuel processor that is used for the fuel cell system shown in Figure 1A of the midplane intercepting of fuel processor;

Fig. 3 A shows the front cross sectional view of the monolithic construction that adopts in the fuel processor shown in Fig. 2 A according to an embodiment of the invention;

Fig. 3 B shows the cross sectional arrangement figure of the tubular design that is used for fuel processor according to another embodiment of the invention;

Fig. 3 C shows the front cross sectional view of the monolithic construction in the fuel processor according to an embodiment of the invention, and described monolithic construction comprises the single burner with " O shape ", and described single burner is fully around the reformer chamber;

Fig. 3 D shows the external view of the end plate that uses in the fuel processor shown in Fig. 2 A;

Fig. 3 E shows fuel processor 15 according to another embodiment of the invention;

Fig. 4 A shows the sectional view of the fuel processor shown in Fig. 2 A and the air that produced by Dewar type container according to an embodiment of the invention moves;

Fig. 4 B shows the front cross sectional view of the fuel processor shown in Fig. 2 A and has confirmed the heat management advantage that Dewar type container obtains;

Fig. 4 C shows the thermal map of the hot path that is produced by the Dewar type container wall that is used for the fuel processor shown in Fig. 2 A;

Fig. 4 D show according to another embodiment of the invention increase air flow through the cutaway view of fuel processor in the convection current path of Dewar type container wall;

Fig. 4 E shows Dewar type container according to another embodiment of the invention;

Fig. 4 F and Fig. 4 G show the cutaway view of the fuel processor that comprises monolithic construction and multichannel Dewar type container according to another embodiment of the invention;

Fig. 4 H shows the spiral Dewar type container of the expansion form that is in according to another embodiment of the invention in the initial construction process;

Fig. 4 I and Fig. 4 J show according to the carrier coating in the burner wall portion of two embodiment of the present invention (wash coating);

Fig. 5 shows the technological process that is used for producing at fuel processor according to an embodiment of the invention hydrogen;

Fig. 6 A shows the top view of fuel processor according to an embodiment of the invention;

Fig. 6 B shows the sectional view of the fuel processor shown in Fig. 6 A of K-K along the line intercepting;

Fig. 6 C shows the sectional view of the fuel processor shown in Fig. 6 A of L-L along the line intercepting;

Fig. 6 D shows the sectional view of the fuel processor shown in Fig. 6 A of A-A along the line intercepting;

Fig. 6 E shows the sectional view of the fuel processor shown in Fig. 6 A of M-M along the line intercepting;

Fig. 6 F shows the sectional view of the fuel processor shown in Fig. 6 A of N-N along the line intercepting;

Fig. 6 G shows the front cross sectional view of the fuel processor shown in Fig. 6 A of B-B along the line intercepting;

Fig. 6 H shows the front cross sectional view of the fuel processor shown in Fig. 6 A of C-C along the line intercepting;

Fig. 6 I shows the front cross sectional view of the fuel processor shown in Fig. 6 A of D-D along the line intercepting; With

Fig. 6 J shows the enlarged drawing of the part shown in Fig. 6 G.

Embodiment

A plurality of preferred embodiments in conjunction with the accompanying drawings describe the present invention.In the following description, in order to help comprehensive understanding of the present invention a lot of concrete details have been disclosed.Yet,, it is apparent that do not have some or all detail also can implement the present invention to those skilled in the art.In other example,, be not described in detail for known process steps and/or structure for fear of unnecessarily having blured the present invention.

Figure 1A shows the fuel cell system 10 that is used to produce electric energy according to an embodiment of the invention.Fuel cell system 10 comprises storage device 16, fuel processor 15 and fuel cell 20.

" reformation " hydrogen supply device is handled to produce hydrogen fuels sources.As shown in the figure, the reformer hydrogen feeding mechanism comprises fuel processor 15 and fuels sources storage device 16.Storage device 16 stores fuel source 17, and can comprise propellant bottle portable and/or that can dispose.The tube that can dispose provides the function that moment recharges for the user.In one embodiment, tube is included in the scalable capsule in the duroplasts distributor sheath body.Independent petrolift control usually comes the fuels sources 17 of self-storing mechanism 16 to flow.If system 10 is load trackings, control system metering fuel source 17 is so that be delivered to processor 15 with the flow velocity of being determined by the power demand horizontal output of fuel cell 20 with fuels sources 17 so.

Fuels sources 17 is used as the carrier of hydrogen and can be subjected to handling with separating hydrogen gas.Fuels sources 17 can comprise any year hydrogen fuel stream, hydrocarbon fuel or other hydrogen fuel source such as ammonia.Be suitable for for example comprising gasoline, C with the hydrocarbon fuel sources that can get at present 17 that the present invention uses ₁To C ₄Hydrocarbon, its oxidation analog and/or its combination.Multiple hydrocarbon and ammonolysis product also can produce suitable fuels sources 17.Liquid fuel source 17 provides high-energy-density and the ability that is easy to store and transport.Storage device 16 can comprise fuel mixture.When fuel processor 15 comprised steam reformer, storage device 16 can comprise the fuel mixture of hydrocarbon fuel sources and water.Hydrocarbon fuel source/water fuel mixtures is illustrated as the percentage fuels sources in the water usually.In one embodiment, fuels sources 17 comprises methyl alcohol or the ethanol of concentration in 1% to 99.9% scope in the water.Other liquid fuel such as butane, propane, gasoline, army grade " JP8 " etc. also can be comprised in the storage device 16 and in the water concentration in 5 to 100% scope.In specific embodiment, fuels sources 17 comprises that percent by volume is 67% methyl alcohol.

Hydrogen is handled and exported to 15 pairs of hydrocarbon fuel sources 17 of fuel processor.Hydrocarbon fuel processor 15 exists under the situation of catalyst heating and processing hydrocarbons fuels sources 17 with generation hydrogen.Fuel processor 15 comprises reformer, and described reformer is the catalytic unit that liquid or gaseous hydrocarbon fuel source 17 is changed into hydrogen and carbon dioxide.When using this term at this, reforming refers to the process that is produced hydrogen by fuels sources.Fuel processor 15 exportable pure hydrogens or year hydrogen stream.Below fuel processor 15 is described in further detail.

Fuel cell 20 is with hydrogen and oxygen electrochemically changes into water and produce electricity and heat in this process.Surrounding air is generally fuel cell 20 supply oxygens.Pure or direct source of oxygen also can be used for carrying out oxygen supply.Water forms steam usually, and this depends on the temperature of fuel cell 20 parts.For a lot of fuel cells, electrochemical reaction also can produce carbon dioxide as accessory substance.

In one embodiment, fuel cell 20 is to be suitable for low volume polymer dielectric film (PEM) fuel cell that uses with electronic installation with portable application situation such as consumer.Polymer dielectric film fuel cell comprises the membrane electrode assembly 40 of the electrochemical reaction of implementing the generation electric energy.Membrane electrode assembly 40 comprises hydrogen catalyst, oxygen catalyst and ion-conductive membranes, and described ion-conductive membranes is optionally proton conducting and b a)) hydrogen catalyst and oxygen catalyst electricity are kept apart.Hydrogen gas distribution layer comprises hydrogen catalyst and allows hydrogen to diffuse through wherein.Oxygen gas distribution layer comprises oxygen catalyst and permission oxygen and hydrogen diffusion of protons and passes through wherein.Ion-conductive membranes is separated hydrogen and oxygen gas distribution layer.In the technical terms of chemistry, anode comprises hydrogen gas distribution layer and hydrogen catalyst, and negative electrode comprises oxygen gas distribution layer and oxygen catalyst.

Polymer dielectric film fuel cell generally includes the fuel cell pack with one group of bipolar plates.Membrane electrode assembly is set between two bipolar plates.Hydrogen distributes 43 by the generation of the passage area on the plate, and oxygen distributes 45 passage area of passing through on second block of subtend plate to take place.Particularly, the first passage zone is dispensed to hydrogen gas distribution layer with hydrogen, and the second channel zone is dispensed to oxygen gas distribution layer with oxygen.Term " bipolar " is clipped in two bipolar plates (no matter comprising a plate or two boards) between the membrane electrode assembly layer referring on the electricity.In this case, bipolar plates is as the negative terminal of an adjacent membranes electrode assemblie be arranged in the positive terminal of second adjacent membranes electrode assemblie on the opposite face of bipolar plates.

In electrical terms, anode comprises hydrogen gas distribution layer, hydrogen catalyst and bipolar plates.The electronics that anode is discharged by hydrogen molecule as the negative electrode of fuel cell 20 and conduction so that they can externally use as powering as external circuit.In fuel cell pack, bipolar plates polyphone connects the current potential that obtains in the heap that adds up every layer.In electrical terms, negative electrode comprises oxygen gas distribution layer, oxygen catalyst and bipolar plates.Negative electrode is represented the positive electrode of fuel cell 20 and electronics is conducted back oxygen catalyst from external circuit, can combine again to form water with hydrogen ion and oxygen at described oxygen catalyst place electronics.

Hydrogen catalyst becomes proton and electronics with Hydrogen Separation.The ion-conductive membranes block electrons, and chemical anode (hydrogen gas distribution layer and hydrogen catalyst) and chemical cathodic electricity are kept apart.Ion-conductive membranes is the ion of conduction band positive electricity optionally also.Anode with the electronics conductivity to load (generation) or battery (storage power).Simultaneously, proton move through ion-conductive membranes with combination with oxygen.Proton and used electronics on cathode side, meet subsequently and with combination with oxygen to form water.Oxygen catalyst in the oxygen gas distribution layer helps this reaction.A kind of general oxygen catalyst comprises the platinum powder end that is coated to as thin as a wafer on carbon paper or the cloth.Multiple design adopts coarse and catalyst porous to be exposed to the surface area of the platinum of hydrogen and oxygen with increase.

In one embodiment, fuel cell 20 comprises one group of bipolar plates, and described bipolar plates is included in the distribution hydrogen on the opposite face and the passage area of oxygen respectively.Article one, passage area is distributed hydrogen and passage area on the opposite face is distributed oxygen.The polylith bipolar plates can be stacked to produce " fuel cell pack ", and wherein membrane electrode assembly is set between every pair of adjacent bipolar plates.Because the living electric process in the fuel cell 20 is heat release, so fuel cell 20 can be implemented heat management system to dissipate from the heat of fuel cell.Fuel cell 20 also can adopt a plurality of humidifying plates (HP) with the moisture level in the management fuel cell.In the patent application of common all common pending trials that exercise question is applied for for the inventor and in the date identical with present patent application for " micro fuel cell structure " and name Ian Kaye, comprise further describing to the fuel cell that is suitable for using with the present invention.This application is introduced into for your guidance thus.

Although the conjugated polymer dielectric film fuel cell is mainly described the present invention, should be appreciated that and to implement the present invention by other fuel cell configurations.Main difference between the fuel cell configurations is the type of used ion-conductive membranes.In one embodiment, fuel cell 20 is the phosphoric acid fuel cells that adopt liquid phosphoric acid to carry out ion-exchange.Solid Oxide Fuel Cell adopts hard atresia ceramic compound to carry out ion-exchange and can be suitable for using with the present invention.Usually, any fuel battery structure can be benefited from fuel processor improvement described herein.Other this fuel cell configurations comprises direct methyl alcohol, alkalescence and molten carbonate fuel cell.

Fuel cell 20 produces the direct voltage that can be used in the multiple applicable cases.For example, electric availablely think that motor or lamp power by what fuel cell 20 produced.In one embodiment, the invention provides " little " fuel cell of the power (clean or total) that is designed to export less than 200 watts.The fuel cell of this size generally is known as " micro fuel cell " and is suitable for using with portable electronic equipment very much.In one embodiment, fuel cell 20 is configured to produce about 1 milliwatt to about 200 watts power.In another embodiment, fuel cell 20 produce about 3 watts to about 20 watts power.Fuel cell 20 can also be a fuel cell independently, and described fuel cell is the individual unit that produces power, as long as it has a) oxygen and b) hydrogen or hydrocarbon fuel feeding mechanism.Export about 40 watts and be very suitable for being the laptop computer power supply to about 100 watts fuel cell 20.

Figure 1B shows the schematic operation of fuel cell system 10 according to a particular embodiment of the invention.As shown in the figure, fuel cell system 10 comprises fuel container 16, hydrogen fuel source 17, fuel processor 15, fuel cell 20, many pumps 21 and blower fan 35, burning line and gas line and one or more valve 23.Although will mainly describe the present invention in conjunction with the methyl alcohol in the source of acting as a fuel 17 now, should be appreciated that a kind of fuels sources that the present invention can adopt another kind of fuels sources 17 as provide above.

Fuel container 16 stores methyl alcohol as hydrogen fuel source 17.The outlet 26 of fuel container 16 provides methyl alcohol 17 to enter hydrogen fuel pipeline 25.As shown in the figure, pipeline 25 is divided into two pipelines: methyl alcohol 17 is transported to fuel processor 15 burner 30 first pipeline 17 and methyl alcohol 17 is transported to second pipeline 29 of the reformer 32 in the fuel processor 15. Pipeline 25,27 and 29 for example can comprise plastic duct system.Being respectively pipeline 27 and 29 provides independent pump 21a and 21b pipeline is pressurizeed and then transmit fuels sources with speed independently if desired.By Plymouth Meeting, the model that the Instech of PA provides is that the pump of P625 is suitable for transmitting the liquid methanol that is used for system 10 and is applicable to present embodiment.Amount at the flow sensor on the pipeline 29 between storage device 16 and the fuel processor 18 or valve 23 detections and reception and registration methyl alcohol 17 of transmission between storage device 16 and reformer 32.Combined sensor or valve 23 and suitably control as by carrying out digital control that processor from the instruction of storing software applies, pump 21b regulates methyl alcohol 17 supplies of 16 pairs of reformers 32 of storage device.

Blower fan 35a carries the regenerator 36 that arrives fuel processor 15 by pipeline 31 with oxygen and air from environment space.Blower fan 35b carries the regenerator 36 that arrives fuel processor 15 by pipeline 33 with oxygen and air from environment space.In the present embodiment, the model that is provided by the Adda USA of California is that the blower fan of AD2005DX-K70 is suitable for transmitting oxygen and the air that is used for fuel cell system 10.Blower fan 37 is blown over fuel cell 20 and heat transfer annex 46 thereof with cooling air.

Fuel processor 15 receives the methyl alcohol 17 and the output hydrogen of self-storing mechanism 16.Fuel processor 15 comprises burner 30, reformer 32, boiling device 34 and Dewar type container 150.Burner 30 comprises that reception is from the inlet of the methyl alcohol 17 of pipeline 27 with at the catalyst that has generation heat under the situation of methyl alcohol.In one embodiment, burner 30 comprises the outlet that heated air is expelled to pipeline 41, and described pipeline transmitted heated air the warm-up time of heat transfer annex 46 fuel cell carried out preheating and need to have accelerated of fuel cell 20 when initially opening fuel cell 20.The outlet of burner 30 also can be discharged heated air and be entered in the environment space.

Boiling device 34 comprises the inlet of reception from the methyl alcohol 17 of pipeline 29.The structure of boiling device 34 allows heat methyl alcohol 17 in the heating boiling device 34 before reformer 32 receives methyl alcohol 17 of generation in the burner 30.Boiling device 34 comprises the outlet that heating methanol 17 is offered reformer 32.

Reformer 32 comprises the inlet of reception from the heating methanol 17 of boiling device 34.Catalyst in the reformer 32 and methyl alcohol 17 reactions and generation hydrogen and carbon dioxide.This reaction be absorb heat slightly and from burner 30 draw heat.The hydrogen outlet of reformer 32 exports hydrogen to pipeline 39.In one embodiment, fuel processor 15 also comprises discharge hydrogen that blocks reformer 32 and the preferential oxidizer that reduces the CO content in the effluent.Preferential oxidizer adopt from air intake arrive preferential oxidizer oxygen and for carbon monoxide than carbon dioxide more preferably for example based on the catalyst of ruthenium or platinum.

Dewar type container 150 carried out preheating to process gas or liquid before air enters burner 30.Dewar type container 150 is also introduced process liquids or gas by heating before heat effusion fuel processor 15 and is reduced thermal loss from fuel cell 15.On a kind of meaning, Dewar type container 150 is as using used heat in the fuel processor 15 with the heat management that increases fuel processor and the regenerator of the heat efficiency.Particularly, thereby can reduce the heat that is passed to the air in the burner in order to the introducing air that offers burner 30 is carried out preheating, so that more heat is passed to reformer 32 from the used heat of boiling device 30.Below Dewar type container 150 is described in further detail.

Pipeline 39 is transported to fuel cell 20 with hydrogen from fuel processor 15. Gas delivery pipeline 31,33,39 for example can comprise polymer or metal piping system.Also hydrogen flowing quantity transducer (not shown) can be added on the pipeline 39 to detect and to pass on the amounts of hydrogen that is delivered to fuel cell 20.In conjunction with hydrogen flowing quantity transducer and suitably control as by carrying out digital control that processor from the instruction of storing software applies, the hydrogen of fuel processor 15 fuel metering batteries 20 provides.

Thereby fuel cell 20 comprises reception and is delivered to the hydrogen inlet port that the hydrogen inlet manifold is delivered to one or more bipolar plates and hydrogen distribution passage thereof from the hydrogen of pipeline 39 and with it.The oxygen inlet port of fuel cell 20 receives from the oxygen of pipeline 33 and with it and is delivered to the oxygen inlet manifold so that be delivered to one or more bipolar plates and oxygen distribution passage.The anode exhaust manifold collects to distribute the gas of passage and they are delivered to anode exhaust from hydrogen, and described anode exhaust will be discharged the gas discharge and be made it enter environment space.The cathode exhaust gas manifold collects to distribute the gas of passage and they are delivered to cathode exhaust vent from oxygen.

The schematic operation of the fuel cell system 10 shown in Figure 1B is typical and has expected other modification of fuel cell system design such as reactant and accessory substance pipe-line equipment.Except the parts shown in Figure 1B, system 10 can comprise that also those skilled in the art is known and for concise and to the point and help other element of the function of realization system 10 in this abridged, as system sensor, manifold, heat exchanger and the electronic interconnector device of electronic-controlled installation, complementary pump and valve, increase.

Fig. 1 C shows and makes untapped hydrogen move back to the embodiment of the fuel system 10 of burner 30 by route from fuel cell 20.Burner 30 comprises and the catalyst of untapped hydrogen reaction with the generation heat.Because the hydrogen consumption process in the fuel cell 20 is normally incomplete and the anode effluent generally includes untapped hydrogen, therefore makes the anode effluent change route and arrive burner 30 and allow fuel cell systems 10 to utilize hydrogen utilization rate and the efficient in hydrogen and the increase system 10 do not used in the fuel cell 20.As term as used herein, untapped hydrogen is commonly referred to as the hydrogen by fuel cell output.

Pipeline 51 is configured to untapped hydrogen is sent to from fuel cell 20 burner 30 of fuel processor 15.For Fig. 1 C, burner 30 comprises two inlets: the inlet 55 and the hydrogen that is configured to receive from pipeline 51 that are configured to receive hydrogen fuel source 17.Untapped hydrogen is collected and discharged to hydrogen from the anodic gas collection channel that fuel processor 15 is dispensed to each membrane electrode assembly layer.The inlet blower fan is to pressurizeing hydrogen from the pipeline 39 that the outlet of fuel processor 15 is delivered to the anode inlet of fuel cell 20.Inlet blower fan also antianode gas collection channel pressurizes to distribute the hydrogen in the fuel cell 20.The outlet place that the process of the material processor 15 that gas delivery is strile-backd that carries out in pipeline 51 in one embodiment, depends on the anode gas distribution passage is the pressure in the anode exhaust manifold for example.In another embodiment, extra blower fan is added into pipeline 51 pipeline 51 is pressurizeed and make untapped hydrogen return fuel processor 15.

Burner 30 also comprises the inlet 59 that is configured to receive from the oxygen of the oxygen discharger that comprises in the fuel cell 20.To collect and discharge untapped hydrogen from the oxygen and air distribution to the cathode gas collection channel of each membrane electrode assembly layer of environment space.Pipeline 61 is delivered to inlet 59 from collecting from the exhaust manifold of the oxygen of every cathode gas collection channel with untapped oxygen.Therefore burner 30 comprises two oxygen intakes: inlet 59 and be configured to receive the inlet 57 of described oxygen from the oxygen delivery of environment space after by Dewar type container 150.Because the hydrogen consumption process in the fuel cell 20 is normally incomplete and the negative electrode effluent comprises untapped hydrogen, therefore makes the negative electrode effluent change route and arrive burner 30 and allow fuel cell systems 10 to utilize hydrogen utilization rate and the efficient in hydrogen and the increase system 10 do not used in the fuel cell 20.

In one embodiment, fuel processor 15 is only to need steam to produce the steam reformer of hydrogen.Be applicable to that the polytype reformer in the fuel cell system 10 comprises steam reformer, automatic thermal reforming device (ATR) or catalyzing part oxidation device (CPOX).Automatic thermal reforming device or catalyzing part oxidation device reformer make air mix with fuel and vapour mixture.Automatic thermal reforming device or catalyzing part oxidation device system reform to fuel such as methyl alcohol, diesel oil, regular unleaded and other hydrocarbon.In specific embodiment, storage device 16 offers fuel processor 15 with methyl alcohol 17, and described fuel processor is reformed and allowed fuel cell system 10 to be used for temperature methyl alcohol under about 250 ℃ or lower temperature and wants minimized applicable cases.

Fig. 2 A shows the sectional view of fuel processor 15 according to an embodiment of the invention.Fig. 2 B shows along the front cross sectional view of the fuel processor 15 of the midplane intercepting of processor 15, also shows the feature of end plate 82 among the figure.15 pairs of methyl alcohol of fuel processor are reformed to produce hydrogen.Fuel processor 15 comprises monolithic construction 100, end plate 82 and 84, reformer 32, burner 30, boiling device 34, boiling device 108, Dewar type container 150 and housing 152.Although now will present invention is described in conjunction with the methanol consumption that is used to produce hydrogen, should be appreciated that fuel processor of the present invention can consume another kind of fuels sources, is to be appreciated that ground as those skilled in the art.

As term as used herein, " integral type " refers to and comprises the single overall structure that is used for a plurality of parts of fuel processor 15 to small part.As shown in the figure, monolithic construction 100 comprises reformer 32, burner 30, boiling device 34 and boiling device 108.Monolithic construction 100 also can comprise the pipe-line equipment entrance and exit that is associated that is used for reformer 32, burner 30 and boiling device 34.Monolithic construction 100 comprises the versatile material 141 that constitutes this structure.Versatile material 141 is included in the wall portion that limits reformer 32, burner 30 and boiling device 34 and 108.Particularly, wall portion 111,119,120,122,130,132,134 and 136 all comprises versatile material 141.Versatile material 141 can comprise metal, as copper, silicon, stainless steel, Yin Kenaier with demonstrate other metal/alloy of favourable thermal conductive property.Monolithic construction 100 and versatile material 141 have been simplified the manufacture process of fuel processor 15.For example, metal being used for versatile material 141 allows to form monolithic construction 100 by extruding or casting technique.In some cases, the cross sectional dimensions of monolithic construction 100 is consistent between end plate 82 and 84 and only is included in the copper that forms in the single extrusion.Versatile material 141 for example also can comprise pottery.Can form ceramic integral formula structure 100 by sintering.

Housing 152 provides mechanical protection for the internal part of fuel processor 15 such as burner 30 and reformer 32.Housing 152 also provides the function of isolating with the external environment condition of processor 15 and has comprised and make gas and liquid and fuel processor 15 inside and outside entering and outlet of being communicated with.Housing 152 comprises the one group of shell wall 161 that comprises Dewar type container 150 at least in part and the exterior mechanical protection is provided for the parts in the fuel processor 15.Wall portion 161 for example can comprise suitably hard material such as metal or rigid polymer.Dewar type container 150 has improved the heat management performance of fuel processor 15 and will describe in further detail in conjunction with Fig. 4 A.

Monolithic construction 100 and end plate 82 and 84 limit reformer 32, burner 30, boiling device 34 and boiling device 108 and corresponding chamber thereof together structurally.In order to illustrate purpose, Fig. 2 A shows monolithic construction 100 and end plate 82 and 84 separately, and Fig. 4 A shows them together.

Referring to Fig. 3 B, boiling device 34 is heating methanol before reformer 32 receives methyl alcohol.Boiling device 34 receives methyl alcohol by the fuels sources inlet 81 that is attached to the methyl alcohol supply line 27 shown in Figure 1B.Because the methanol recapitalization and the hydrogen that are undertaken by the catalyst in the reformer 32 102 produce the methanol temperature that needs rising usually, so fuel processor 15 carried out preheating by 34 pairs of methyl alcohol of boiling device before methyl alcohol is received by reformer 32.Boiling device 34 is set at the heat of position to produce in the reception burner 30 near burner 30.Heat is by arriving boiling device 34 from burner 30 conduction by monolithic construction and transmitting by carrying out convection current from boiling device 34 wall portions to the methyl alcohol by wherein.In one embodiment, boiling device 34 is configured so that the liquid methanol vaporization.Thereby boiling device 34 makes gas methyl alcohol produce the gas interaction by arriving reformer 32 with catalyst 102 subsequently.

Reformer 32 is configured to receive the methyl alcohol from boiling device 34.End wall 113 (Fig. 2 B) on wall portion 111 in the monolithic construction 100 (referring to the cross section among Fig. 3 A) and end plate 82 and 84 limits the size of reformer chamber 103.In one embodiment, end plate 82 and/or end plate 84 also comprise and make the heating methanol of discharging from boiling device 34 move into passage 95 (Fig. 2 A) in the reformer 32 by route.Heating methanol enters the reformer chamber 103 that is in monolithic construction 100 1 ends subsequently and arrives the other end, and the reformer effluent is disposed at the described other end.In another embodiment, be arranged on eyelet in the reformer 32 wall portions and receive inlet heating methanol from pipeline or other feeding mechanism.Enter in the suitable wall portion 111 or 113 that eyelet or aperture can be set at reformer 32.

Reformer 32 includes and is beneficial to the catalyst 102 that produces hydrogen.Catalyst 102 reacts with methyl alcohol 17 and helps producing hydrogen and carbon monoxide.In one embodiment, particle size is designed so that be exposed to the amount maximization of the surface area of introducing methyl alcohol.The particle diameter of scope in about 50 microns to about 1.5 millimeters is applicable to multiple applicable cases.Scope is suitable for using with reformer chamber 103 at about 300 microns particle diameters to about 1500 micrometer ranges.Particle size and filling also can change the pressure drop of passing reformer chamber 103 with control.In one embodiment, the number of pressure drops magnitude between the inlet of reformer chamber 103 and the outlet is suitable about 0.2 to about 5psi scope.For example when the particle diameter of increase of reformer chamber size and catalyst 102 can increase, particle size can change with respect to the cross sectional dimensions of reformer chamber 103.In one embodiment, particle diameter (d) can be about 0.0125 to about 1 scope with the ratio of cross-sectional height 117 (D).The D/d ratio also is applicable to multiple applicable cases about 5 to about 20 scope.Packing density also can be used as the filling feature of catalyst 102 in reformer chamber 103.For copper zinc catalyst 102, packing density is suitable at about 0.3 grams per milliliter to the scope of about 2 grams per milliliters.Packing density is applicable to the embodiment shown in Fig. 3 A at about 0.9 grams per milliliter to the scope of about 1.4 grams per milliliters.

When methyl alcohol was used as hydrocarbon fuel sources 17, a kind of suitable catalyst 102 can comprise the CuZn on the alumina particle.Other material that is applicable to catalyst 102 for example can be based on independent nickel, platinum, palladium or other noble metal catalyst or its combination.The particle of catalyst 102 is commercial can be obtained from the known multidigit seller of those skilled in the art.Beaded catalyst also can be set in the resistance barrier system that is provided with in the reformer chamber 103.Resistance barrier system comprises that the pilot fuel source is along one group of wall portion that nonlinear path is advanced.Resistance barrier system slows down and control gaseous methyl alcohol flowing to improve the interaction between gas methyl alcohol and the beaded catalyst 102 in chamber 103.Another kind of optional mode is that catalyst 102 can comprise the catalyst material of listing above that is coated on metal sponge or the metal foaming material.The technology that required Metal catalyst materials is washed in the wall portion that is layed onto reformer chamber 103 also can be used for reformer 32.

Reformer 32 is configured to export hydrogen and comprises and make in the reformer 32 hydrogen that forms and the outlet 87 of fuel processor 15 external communications.In fuel system 10, aperture 87 makes hydrogen be communicated to pipeline 39 so that carry out hydrogen distribution 43 in fuel cell 20.Aperture 87 is set in the wall portion of end plate 82 and comprises eyelet (referring to Fig. 2 B) by wall portion.Delivery port can be set on any suitable wall portion 111 or 113.

Hydrogen production process in the reformer 32 be absorb heat slightly and from burner 30 draw heat.Burner 30 produces heat and is configured to heat is offered reformer 32.Burner 30 is arranged on around the reformer 32 annularly, as below discussing ground in further detail.Shown in Fig. 2 B, burner 30 comprises two burners (or burner part) 30a and 30b and centers on the corresponding combustor 105a and the 105b of reformer 32.Burner 30 comprises by the inlet of the reception of the passage in the end plate in end plate 82 or 84 from the methyl alcohol 17 of boiling device 108.In one embodiment, burner inlet leads in the combustor 105a.Methyl alcohol marches to the passage that is arranged in the end plate 82 along the length 142 of combustor 105a subsequently, and described passage makes methyl alcohol move to combustor 105b from combustor 105a by route.Methyl alcohol is advanced subsequently backward by the length 142 arrival burner outlets 89 of combustor 105b.In another embodiment, burner inlet leads in chamber 105a and the 105b.Methyl alcohol marches to burner outlet 89 along the length 142 of chamber 105a and 105b subsequently.

In one embodiment, burner 30 adopts catalytic combustion to produce heat.The catalyst 104 that is arranged in each combustor 105 helps to produce heat by the burner fuel of chamber.In one embodiment, methyl alcohol produces heat and catalyst 104 and helps methyl alcohol and produce heat in burner 30.In another embodiment, the useless hydrogen from fuel cell 20 produces heat under the situation that has catalyst 104.Suitable burner catalyst 104 for example can comprise platinum or the palladium that is coated on suitable carrier or the alumina particle.Other material that is applicable to catalyst 104 comprises iron, tin oxide, other noble metal catalyst, reducible oxide and composition thereof.Catalyst 104 can obtain from the known multidigit seller of those skilled in the art commercial as granule.Particle can be filled in the combustor 105 to form the porous bedding or otherwise suitably to be packed in the combustion chamber volume.Catalyst 104 particle sizes can change with respect to the cross sectional dimensions of combustor 105.Catalyst 104 also can comprise and is coated on metal sponge or the metal foaming material or washes the catalyst material of listing above in the wall portion that is layed onto combustor 105.Burner outlet 89 (Fig. 2 A) makes the effluent of formation in the burner 30 and the external communications of fuel processor 15.

Some fuels sources produce additional heat in burner 30, or more effectively produce heat, and elevate the temperature.Fuel processor 15 is included in burner 30 and receives the fuels sources boiling device 108 of heating methanol before.In this case, boiling device 108 receives methyl alcohol by fuels sources inlet 85.Boiling device 108 is set at the heat of position to produce in the reception burner 30 near burner 30.Heat is by arriving boiling device 108 from burner 30 conduction by monolithic construction and transmitting by carrying out convection current from boiling device 108 wall portions to the methyl alcohol by wherein.

The air that comprises oxygen enters fuel processor 15 by air inlet port 91.Burner 30 uses oxygen so that methyl alcohol is carried out catalytic combustion.As further going through ground below in conjunction with Fig. 4 A and Fig. 4 B, air before by the hole in the Dewar type container at first along the outside of Dewar type container 150 by and pass through along the inside of Dewar type container 150.This is heated air before the air inlet port 93 by burner 30 receives.

Fig. 3 A shows the front cross sectional view of the monolithic construction 100 along midplane 121 intercepting according to an embodiment of the invention.Monolithic construction 100 extends to end plate 84 from end plate 82.The cross section of the monolithic construction 100 shown in Fig. 3 A extends to the other end of the structure 100 at end plate 84 places from an end of the structure 100 of end plate 82.Monolithic construction 100 comprises reformer 32, burner 30, boiling device 34 and the boiling device 108 between end plate 82 and 84.

Reformer 32 comprises reformer chamber 103, and described reformer chamber is the big volume space in the fuel processor 15, and described big volume space comprises reforming catalyst 102, leads to fuels sources inlet (from the boiling device 34 of fuel processor 15) and leads to hydrogen outlet 87.Sidewall 111 limits the non-planar transverse cross-section shape of reformer 32 and reformer chamber 103 thereof.Wall portion 113 on the end plate 82 and 84 seals reformer chamber 103 and comprises entering and outlet of chamber 103 on arbitrary end of chamber 103.

Reformer 103 comprises the on-plane surface volume.As term as used herein, on-plane surface reformer chamber 103 refers to non-flat substantially or nonlinear shape of cross section.Cross section refers to the plane lamina of cutting fuel processor or parts.For the cross section that comprises a plurality of fuel processor parts (for example burner 30 and reformer 32), cross section comprises all two parts.For the vertical and preceding cross section 121 shown in Fig. 3 A, the cross sectional dimensions of shown monolithic construction 100 is consistent in 84 the scope from end plate 82 to end plate, and to locate at each cross section 121 (Fig. 2 A) be consistent.

Quadrangle or non-quadrangular cross section shape can be adopted in reformer 32 and reformer chamber 103 thereof.It is tetragonal reformer chamber 103 that four edges limits cross section.Article four, vertical substantially margin is made rectangle and square quadrangle reformer 32.Non-quadrangle reformer 32 can adopt has more or less cross sectional dimensions, elliptical shape (referring to Fig. 3 B) and the more complicated shape of cross section on bar limit.As shown in Figure 3A, reformer 32 comprises the hexagon cross section " P shape " with chamfering.A bight of removing reformer 32 from monolithic construction 100 is to allow boiling device 34 near burner 30.

Reformer burner 103 has the feature of cross-sectional width 115 and cross-sectional height 117.The edge is across the quantity of the maximum linear between the inwall 111 of the chamber 103 of the direction of reformer chamber 103 cross sections apart from expression cross-sectional width 155.Maximum linear between the inwall 111 of the chamber 103 vertical with width 115 is apart from the quantity of expression cross-sectional height 117.As shown in the figure, cross-sectional height 117 is greater than 1/3rd of cross-sectional width 115.This height/width relation has increased the volume for the reformer chamber 103 of given fuel processor 15.In one embodiment, cross-sectional height 117 is greater than half of cross-sectional width 115.In another embodiment, cross-sectional height 117 is greater than cross-sectional width 115.

Return the A referring to Fig. 2, reformer chamber 103 comprises the length 142 (perpendicular to width 115 and height 117) of the other end that extends to the structure 100 at end plate 84 places from an end of the monolithic construction 100 of end plate 82.In one embodiment, reformer chamber 103 has less than the length 142 of 20:1 and the ratio of width 115.In so not elongated design, reformer chamber 103 has less than the length 142 of 10:1 and the ratio of width 115.

Reformer 32 provides the reformer chamber 103 of big volume.This three-dimensional structure of reformer chamber 103 and the design of little fuel processor form contrast, and in described little fuel processor design, combustor 103 is etched into the microchannel on the planar substrates.The on-plane surface size of reformer chamber 103 allows reformer 32 to have bigger volume and allows the fuel processor 15 of intended size to have more multi-catalyst 102.This has increased the amount of the methyl alcohol that can be handled and has increased hydrogen output for the size of concrete fuel processor 15.Therefore reformer 32 has improved applicability and the performance of fuel processor 15 in the portable application situation, and in described portable application situation, the fuel processor size is important or is restricted.In other words, although owing to increase the volume of reformer chamber 103 but the size of the entrance and exit pipe-line equipment and the mouth of pipe changes hardly, so this allows fuel processor 15 to increase hydrogen output and has increased the power density that is used for the portable application situation to keep the size of the pipe-line equipment that is associated relative with weight constant simultaneously.In one embodiment, reformer chamber 103 comprises greater than about 0.1 cubic centimetre and less than about 50 cubic centimetres volume.In certain embodiments, reformer 32 volumes are applicable to the applicable cases of laptop computer between about 0.5 cubic centimetre and about 2.5 cubic centimetres.

Fuel processor 15 comprises at least one burner 30.Each burner 30 comprises combustor 105.For catalytic burner 30, combustor 105 is the big volume spaces that comprise catalyst 104 in fuel processor 15.For being communicated with or burner reactant and product arrive and leave for the process of combustor 105, combustor 105 can directly or indirectly lead to fuels sources inlet (from the boiling device 108 of fuel processor 15), leads to air intake 93 and lead to burner outlet 89.

The quantity of burner 30 and combustor 105 can change according to design.Monolithic construction 100 shown in Fig. 3 A comprises double burner 30a and 30b design, and described double burner design has the discontinuous chamber that two combustor 105a and 105b and formation cross section center on reformer 32 substantially respectively.Burner 30a comprises the end wall 113 on sidewall 119a (Fig. 3 A) that comprises in the monolithic construction 100 and the end plate 82 and 84 that limits combustor 105a.Similarly, burner 30b comprises the end wall 113 on sidewall 119b (Fig. 3 A) that comprises in the monolithic construction 100 and the end plate 82 and 84 that limits combustor 105b.Monolithic construction 100 shown in Fig. 3 C comprises having the single burner 30c that centers on the single combustor 105c of reformer 32 fully.Tubulose shown in Fig. 3 B is arranged and is comprised 40 burners 204 that surpass that center on reformer 202 fully.Monolithic construction 452 shown in Fig. 4 F comprises the single burner that is divided into fully around 104 combustors of reformer 32.

Referring to Fig. 2 B, construct each burner 30 so that the heat transferred of generation is to reformer 32 in the burner 30 with respect to reformer 32.In one embodiment, one or more burners 30 are arranged on around the reformer 32 by ring-type.As term as used herein, at least one burner 30 refers to burner 30 with respect to the cyclic configuration of reformer 32 to be had continuous or discrete section or chamber 105 around reformer 32, is made or formed by described section or chamber by described section or chamber.Ring-type is closed and tied up on the cross section is clearly.Arrange for burner and reformer, meet boundary or adjacent so that heat can be sent to reformer 32 from burner 30 around referring to the circumference of burner 30 with reformer 32.Burner 30a and 30b can center on reformer 32 to change the degree based on design around the circumference of reformer 32.One or more burners 30 are at least around the cross sectional perimeter greater than 50% reformer 32.This comes fuel processor 15 and plane and dull and stereotyped design distinguished, and in plane and slab design, burner is coplanar with reformer and has similar size, and with regard to how much logics, and burner is adjacent with reformer circumference less than 50%.In one embodiment, one or more burners are around the cross sectional perimeter greater than 75% reformer 32.Increasing that burner increased around the degree of reformer 32 circumferences on cross section can be in order to the surface area of the reformer 32 by the heat heated reformate device volume that produces in the burner.For the design of some fuel processors 15, one or more burners 30 can be around the cross sectional perimeter that surpasses 90% reformer 32.For the embodiment shown in Fig. 3 B, burner 30 is around the cross sectional perimeter of whole reformer 32.

Present invention is described although will be arranged on reformer 32 burner 30 on every side in conjunction with ring-type now, should be appreciated that monolithic construction 100 can comprise opposite configuration.That is, reformer 32 can be arranged on around the burner 30 by ring-type.In this case, reformer 32 can comprise one or more continuous or discrete section or the chamber 103 around burner 30.

In one embodiment, each burner 30 and combustor 105 thereof have the non-planar transverse cross-section shape.On-plane surface burner 30 can adopt shape of cross section such as quadrangle, have more or less non-quadrangle geometry, ellipse (referring to circle/tube burner 30 of Fig. 3 B) or the more complicated shape of cross section on bar limit.As shown in Figure 3A, each burner 30 is included in reformer 32 crooked hexagonal cross-section " L " shape (having chamfering) of 90 degree on every side.

Each burner 30 therefore with the reformer 32 bilateral boundaries that connect.N side joint circle of this meaning refers to reformer 32 and count N with the limit that burner 30 (and combustor 105) meets the boundary on cross section.Therefore, the right and the base of burner 30b and reformer 32 meet the boundary, and the top margin and the left side of burner 30a and reformer 32 meet the boundary.Can adopt " U-shaped " burner 30 with on three limits with reformer 32 3 edge joints circle.Burner 30a and 30b together on the limit of all four vertical reformer 32 with reformer 32 4 edge joints circle.The reformer 32 that uses in the configuration shown in Fig. 3 B comprises a plurality of tube burners with reformer 32 4 edge joints circle.Fig. 3 C shows the front cross sectional view that comprises the monolithic construction 100 of the single burner 30c with the O shape that centers on combustor 103 fully according to an embodiment of the invention.Burner 30c be around the continuous chamber of reformer 32 circumferences and with reformer 32 4 edge joints circle.

The heat that produces in the burner 30 directly and/or indirect transfer to reformer 32.For the monolithic construction 100 shown in Fig. 3 A, the shared total wall of each burner 30 and reformer 32 portion 120 and 122 and each burner 30 in the heat that produces by conduction heat transfer by total wall portion 120 and 122 and directly be passed to reformer 32.Wall portion 120 has formed the boundary wall portion of burner 30b and the boundary wall portion of reformer 32.As shown in the figure, a side of wall portion 120 is led to combustor 105b and another part of wall portion leads to combustor 103.Therefore wall portion 120 allows to carry out direct conduction heat transfer between burner 30b and reformer 32.Similarly, wall portion 122 formed the boundary wall portion of burner 30a and reformer 32 boundary wall portion, lead to combustor 105a, lead to reformer chamber 103 and allow and between burner 30a and reformer 32, carry out direct conduction heat transfer.Wall portion 120 and 122 cross section all be on-plane surface and with many edge joints circle of reformer chamber 103, many limits of burner 30b and 30a and described reformer are adjacent.Therefore wall portion 120 provides the function of carrying out direct conduction heat transfer to reformer 32 from burner 30a along a plurality of vertical direction 128 and 129.Wall portion 122 similarly provides the function of carrying out direct conduction heat transfer from burner 30b to reformer 32 along the direction relative with 128 and 129.

Boiling device 34 comprises the end wall 113 (referring to Fig. 2 B) on cylindrical wall 143 that comprises in the monolithic construction 100 and the end plate 82 and 84 that limits boiling device chamber 147.The cross section of circle wall 143 has formed the cylindrical shape of boiling device 34, and described cylindrical shape extends to routing end 84 from routing end 82.Boiling device 34 is set near the position of burner 30a and 30b to receive the heat that produces in each burner 30.For monolithic construction 100, the shared total wall of boiling device 34 and burner 30a portion 130 and with the shared total wall of burner 30b portion 132. Total wall portion 130 and 132 allows to carry out direct conduction heat transfer from each burner 30 to boiling device 34.Boiling device 34 also is set between burner 30 and the reformer 32 to block the conduction heat that moves to heat absorption reformer 32 from high temperature and living heat combustor 30 all the time.

Thereby boiling device 108 is configured to receive the heat heating methanol before burner 30 receives methyl alcohol from burner 30.Boiling device 108 also comprises having the tubular form that extends through the circular cross section of monolithic construction 100 arrival end plates 84 from end plate 82.Boiling device 108 is set near the position of burner 30a and 30b to receive the heat that produces in each burner 30, and described heat is used to heating methanol.The shared total wall of boiling device 108 and burner 30a portion 134 and with the shared total wall of burner 30b portion 136. Total wall portion 134 and 136 allows to carry out direct conduction heat transfer from burner 30a and 30b to boiling device 108.

Fig. 3 D shows the external view of end plate 82 according to an embodiment of the invention.End plate 82 comprises fuels sources inlet 81, fuels sources inlet 85, hydrogen outlet 87 and burner air inlet 93.Fuels sources inlet 81 is included in eyelet or the aperture in the end wall 113 of end plate 82, and described eyelet or aperture make and be communicated with heating methanol before reformer 32 reception methyl alcohol from the methyl alcohol of outside methyl alcohol feeding mechanism (usually as liquid) thereby with boiling device 34.Methanol fuel source inlet 85 is included in eyelet or the aperture in the end wall 113 of end plate 82, and described eyelet or aperture make and be communicated with heating methanol before burner 30 receives methyl alcohol from the methyl alcohol of outside methyl alcohol feeding mechanism (usually as liquid) thereby with boiling device 108.Burner air inlet 93 is included in eyelet or the aperture in the end wall 113 of end plate 82, and described eyelet or aperture make from the air of environment space and oxygen and inwardly be communicated with after the preheating in Dewar type container 150.Hydrogen outlet 87 makes from the gaseous hydrogen of reformer chamber 103 and fuel processor 15 external communications.

Bolt hole 153 is set in the alar part 145 of monolithic construction 100.Bolt hole 153 allows bolt to pass through wherein and allows fastening structure 100 and end plate 82 and 84.

Fig. 3 B shows the cross sectional arrangement figure of the tubular design that is used for fuel processor 15 200 of replacement monolithic construction 100 according to another embodiment of the invention.Structure 200 comprises reformer 202, burner 204, boiling device 206 and boiling device 208.

In the whole cylindrical length range of Cross-section Design 200 shown in Fig. 3 B between the end plate (not shown) is consistent, and described end plate comprises and is used for the gas supply and is expelled to entering and outlet of design 200 parts.Reformer 202.Combustor 212, boiling device 206 and boiling device 208 round-shaped so between end plate, extend whole cylindrical length.End plate also can be responsible for making gas between the single pipeline as move by route between tube burner 234.

Reformer 202 comprises and limits the cylindrical wall 203 of circular cross section substantially.Therefore reformer 232 is reassembled into hollow circular cylinder on three-dimensional, described hollow circular cylinder limits tubulose reformer chamber 210.Usually, reformer 202 can comprise be applicable to any elliptical shape (circular expression has the ellipse of the vertical dimension that approximately equates) that comprises catalyst 102, makes methyl alcohol flow through reformer chamber 210, produces hydrogen and hydrogen is flowed in reformer chamber 210 in reformer chamber 210.As shown in the figure, reformer chamber 210 by the cross-sectional width that equates substantially and cross-sectional height limits and so reformer 202 comprise the cross-sectional aspect ratio of 1:1.

Burner 204 comprises the one group of cylindrical wall 214 that limits tube burner chamber 212 respectively.As shown in the figure, tubular design 200 comprises fully 40 the tube burner chambers 212 that surpass around the cross sectional perimeter of reformer 32.Each tube burner 212 comprises the circular substantially cross section that is limited by cylindrical wall 214.Each tube burner 212 includes and is beneficial to the catalyst 104 that is produced heat by methyl alcohol.Burner 204 can comprise about two to about 200 cylindrical wall 214 and tube burner chamber 212.Some designs can comprise about ten to about 60 tube burner chambers 212.In one embodiment, each cylindrical wall 214 comprises metal and is squeezed into its required size.In specific embodiment, cylindrical wall 214 comprises nickel.Can form nickel wall 214 by nickel being electroplated onto on suitable matrix such as zinc or the aluminium, described matrix is etched subsequently to be gone out to stay the nickel pipe.Other material that can form nickel wall 214 thereon comprises zinc, tin, lead, wax or plastics.Except nickel, wall portion 214 can comprise gold, silver, copper, stainless steel, pottery and at the material that does not cause showing under the complicated situation of burner catalyst 104 suitable thermal property.

As shown in the figure, burner 204 complete ring-types are around the cross sectional perimeter of reformer 202.In this case, burner 204 comprises three circular layers 216,218 and 220 that circularly are arranged on around the reformer 202 and are in the pipeline 214 at three different radii places.Pipeline 214 in every layer 216,218 and 220 limits the circular scope of reformer 202.The heat that produces in each tubular chamber 212 of burner 30 passes through mulitpath: a) the heat conduction arrives the wall portion of reformer 202 by the pipeline in the layer 216 214; B) heat conducts by the pipeline 214 in the 214 arrival layers 216 of the pipeline in the skin 218 and 220 and the wall portion of arrival reformer 202; And/or c) carries out thermal radiation between pipeline 214 in outer 218 and 220 and the pipeline 214 and inwardly conduct to reformer 202 subsequently and be passed to reformer 202 directly or indirectly.

Boiling device 206 is configured to heating methanol before reformer 202 receives methyl alcohol.Boiling device 206 receives from the heat of burner 204 and comprises the cylindrical wall 207 of the tubular form that limits boiling device.Boiling device 206 is set near the position of burner tubes 214 to receive the heat that produces in each combustor 212.Particularly, boiling device 206 is set in second circular layer 218 and the heat of the adjacent combustor 212 in receiving layer 216,218 and 220.Burner 204 offers boiling device 206 by the wall portion of every adjacent channel 214 and by wall portion 207 with heat by conduction.

Boiling device 208 is configured to heating methanol before burner 204 receives methyl alcohol.Boiling device 208 receives from the heat of burner 204 and also comprises the cylindrical wall 209 of the tubular form that limits boiling device.With boiling device 206 similarly, boiling device 208 is set in second circular layer 218 and receives the heat from the adjacent combustor 212 in layer 216,218 and 220.

In one embodiment, integral type fuel processor 15 comprises a plurality of sections that are linked together and connect at cross-section line 121 places along the gas flow in the reformer chamber 103.Each section has total profile as shown in Figure 3A and can comprise metal or the ceramic component that carries out combination or brazing perpendicular to gas flow.Another kind of optional mode is that fuel processor 15 can comprise the integrated part of the single length of the boundary that limits all reformers 32, burner 30, boiling device 34 and boiling device 108 except the zone that is limited boundary by end piece 82 and 84.

In another embodiment, fuel processor 15 is included in a plurality of parts that are linked together on the cross section.Fig. 3 E shows fuel processor 15 according to another embodiment of the invention.In this case, fuel processor 15 comprises three parts: lower member 280, intermediate member 282 and head components 284.Lower member 280 and intermediate member 282 are attached to form reformer 32 and two combustors 30.Head components 284 and intermediate member 282 are attached to form boiling device 34 and 108.Each parts 208,282 and 284 comprises versatile material and can be extruded or be cast as appropriate size.Attached between the parts for example can comprise chemical bond.

Fig. 4 A shows the sectional view of fuel processor 15 and the air that produced by Dewar type container according to an embodiment of the invention 150 moves.Fig. 4 B shows the front cross sectional view of fuel processor 15 and has confirmed the heat management advantage that Dewar type container 150 obtains.Although thermal management technology described herein will be described to the fuel processor parts now, person of skill in the art will appreciate that to the present invention includes the thermal management algorithm that is used for widespread usage.

Burner 30 in the fuel processor 15 produces heat and operation at elevated temperatures usually.The operating temperature of burner 30 is general greater than 200 degrees centigrade.The standard of making electronic installation has been stipulated the maximum surface temperature of device usually.Electronic installation such as laptop computer generally include cooling device such as blower fan or cooling water pipe with management and dissipation internal heat.The cooling system of the fuel processor claimed apparatus of the electronic installation inside in the loses heat access to plant is handled the heat of loss.

In one embodiment, fuel processor 15 comprises that Dewar type container 150 is to improve the heat management performance of fuel processor 15.Dewar type container 150 makes the parts of housing 152 inside such as burner 30 heat keep apart and comprise heat in the fuel processor 15 at least in part.Dewar type container 150 has reduced from the temperature gradient between the outer surface of the thermal loss of fuel processor 15 and help burner 30 and housing 152.And as will be described below, Dewar type container 150 also carried out preheating to air before burner 30 admission of airs.

Dewar type container 150 comprises burner 30 and reformer 32 at least in part, and comprises the one group of Dewar type container wall 154 that helps to form Dewar type container chamber 156 and chamber 158.In certain embodiments, Dewar type container 150 centers on burner 30 and reformer 32 fully on viewgraph of cross-section and in the end of burner 30 and reformer 32.Still less comprising that Dewar type container 150 provides also is suitable for providing hot advantage described herein.Multichannel Dewar type container 300 shown in Fig. 4 E is only partly sealed burner 30 and reformer 32 on cross section.In some cases, Dewar type container 150 does not extend fully and provides incomplete along the length of monolithic construction 100 and comprises.

Shown in Fig. 4 B, Dewar type container 150 centers on burner 30 annularly on cross section.Wall portion group 154 comprises with roof and diapire 154b and 154d and combining to form the sidewall 154a and the 154c of the rectangular cross section shown in Fig. 4 B; And comprise two the end wall 154e and the 154f that combine with roof and diapire 154b and 154d to form the rectangular cross section shown in Fig. 4 A.End wall 154f comprises and allows to enter and the holes of outlet 85,87 and 89 by wherein.

In Dewar type container wall 154, form Dewar type container chamber 156 and described Dewar type container chamber comprise in the Dewar type container wall 154 not by monolithic construction 100 occupy have living space.Shown in Fig. 4 B, Dewar type container chamber 156 is around monolithic construction 100.Shown in Fig. 4 B, chamber 156 comprises the conduit between the wall portion 154 on all four sides of monolithic construction 100 and Dewar type container chamber 150.In addition, chamber 156 comprises end plate 82 on the two ends of the end wall of Dewar type container 150 and monolithic construction 100 and the air pocket (Fig. 4 A) between 84 the outer surface.

At Dewar type container wall 154 outside and between Dewar type container 150 and housing 152 formation chamber 158.Chamber 158 comprise in the housing 152 not by Dewar type container 150 occupy have living space.Shown in Fig. 4 B, housing 152 is sealed Dewar type container 150 and further inner monolithic construction 100.Chamber 158 comprises wall portion 154 on all four sides of Dewar type container 150 and the conduit between the housing 152.In addition, chamber 158 is at the air pocket 167 that comprises on the two ends between Dewar type container 150 and the housing 152, and described air pocket prevents contacting and conduction heat transfer (Fig. 4 A) between Dewar type container 150 and the housing 152.

Dewar type container 150 is configured so that by the process gas of Dewar type container chamber 156 or liquid and receives the heat that produces in the burner 30.Process gas or liquid for example can comprise any reactant such as oxygen, air or the fuels sources of using in the fuel processor 17.Therefore Dewar type container 150 provides two kinds of functions for fuel processor 15: a) it allows initiatively to cool off the parts in the fuel processor 15 before heat arrives the fuel processor outside, and b) air of going to burner 30 is carried out preheating.For reformer, air moves through fuel processor 15 and passes the wall portion 154 of Dewar type container 150 so that colder air absorbs heat from the parts of hotter fuel processor 15.

Shown in Fig. 4 A, housing 152 comprises and allows air inlet port 91 or the eyelet of air in external shell 152 inlet chambers 158.Blower fan directly offers air fuel processor 15 usually and the air by aperture 91 is pressurizeed.Roof and diapire 154b and 154d comprise air inlet port or the eyelet 172 that allows air arrival Dewar type container chambers 156 158 from the chamber.Air stream by fuel processor 15 is subsequently: in air inlet port 91, flow, along the length of Dewar type container 150 flow through chamber 158, by the eyelet 172 among the 154b of wall portion and the 154d, refluxing by chamber 156 with length and entering the air inlet port 176 that allows air to enter burner 30 by the relative direction upper edge Dewar type container 150 in chamber 158.In chamber 158, air a) move through the outer surface of Dewar type container wall 154 and from Dewar type container wall 154 convection current ground absorb heat, and b) move through the inner surface of housing 152 and from housing 152 wall portions convection current ground absorb heat (when housing 152 is in the temperature that is higher than air).In chamber 156, air a) move through the outer surface of monolithic construction 100 and from the wall portion of monolithic construction 100 convection current ground absorb heat, and b) move through the inner surface of Dewar type container 150 and from Dewar type container wall 154 convection current ground absorb heat.

Therefore Dewar type container 150 is configured so that the air by Dewar type container carries out the heat that direct convective heat transfer receives generation in the burner 30 by the wall portion the monolithic construction from the outside of burner 30 100 to the air by Dewar type container chamber 156.Dewar type container 150 is configured so that also the air by chamber 156 receives heat indirectly from burner 30.The heat that referring to indirectly on this meaning produces in the burner 30 moved to another structure in the fuel processor 15 before being received by air.

Fig. 4 C shows the thermal map by the hot path of wall portion 154 generations of Dewar type container 150.Heat conduction from burner 30 arrives the surface that leads to the structure 100 in the Dewar type container chamber 156 by monolithic construction 100.From here, heat a) conducts in the air that enters by Dewar type container chamber 156, thus heated air; B) be radiated to the inwall 155 of Dewar type container wall 154, enter air by Dewar type container chamber 156 from the convection current of described inwall heat; C) inwall 155, conduction that is radiated to Dewar type container wall 154 arrives the outer surface 157 of Dewar type container walls 154 by wall portion 154, enter air from the convection current of described outer surface heat by Dewar type container chamber 158 in; And d) inwall 155, conduction that is radiated to Dewar type container wall 154 by wall portion 154 arrive Dewar type container walls 154 outer surface 157, be radiated to the wall portion of housing 152, enter air from the heat convection current of described wall portion by Dewar type container chamber 158 in.

Therefore Dewar type container 150 provides two heat loss through convection streams of the heat effusion fuel processor that prevents generation in the burner 30 (or other internal part of fuel processor 15) and has activated air cooling stream in volume 156 and 158.

Reflect heat returned reduced from the heat loss amount of fuel processor 150 in the chamber 156 and increased heating the air by chamber 156.In order further to improve the radiance in the reflected back chamber 156, the inner surface of Dewar type container wall 154 can comprise that radiating layer 160 goes into heat (referring to Fig. 4 B or Fig. 4 C) in the wall portion 154 to reduce radiant transfer.Radiating layer 160 is set on the inner surface 155 in the one or more wall portion 154 to increase the reflect radiation heat of inner surface 155.Usually, the material that is used for radiating layer 160 has the emissivity lower than the material that is used for wall portion 154.The material that the wall portion 154 with Dewar type container 150 that is suitable for uses for example comprises nickel or pottery.Radiating layer 160 can comprise that gold, platinum, silver, palladium, nickel and metal can be coated on the inner surface 155 by sputter.Radiating layer 160 also can comprise low thermal conductivity.In this case, radiating layer 160 for example can comprise pottery.

When Dewar type container 150 complete closed monolithic constructions 100, Dewar type container has then limited the thermal loss of coming self-structure and reduced the heat that runs off from Dewar type container 150 and housing 152.The fuel processor of fuel processor 15 shown in Fig. 4 A and 4B is suitable for comprising heat in the housing 152 and the management heat transmission from fuel processor very much.In one embodiment, burner operation and hull outside under greater than about 200 degrees centigrade temperature keeps less than about 50 degrees centigrade temperature.At the embodiment that is used for the portable application situation, wherein fuel processor 15 occupies little volume, and volume 156 is relative with 158 less and comprise slype and conduit.In some cases, the channel height in the volume 156 and 158 is no more than 10 millimeters in housing 152 wall portions less than the wall portion of the burner 30 on 5 millimeters and the monolithic construction.

Also allow to use the combustion fuel of higher temperature as the fuels sources that produces hydrogen, as methyl alcohol and gasoline by the hot advantage of using Dewar type container 150 to obtain.In one embodiment, allow reformer 32 so that the carbon monoxide that produces in the burner 32 is reduced under the temperature of the amount that does not need preferential oxidizer methyl alcohol being handled under the temperature far above 100 degrees centigrade and at enough height by the heat management advantage of using Dewar type container 150 to obtain.

As the top ground of mentioning, Dewar type container 150 provides second kind of function by the air of going to burner is carried out preheating for fuel processor 15.Burner 30 relies on catalytic combustion to produce heat.The airborne oxygen that offers burner 30 is consumed as the partial combustion process.The heat that produces in the burner 30 will heat cold introducing air according to air themperature.This problem that thermal loss give is introduced cold air has reduced the heat efficiency of burner 30, and causes greater amount ground to consume methyl alcohol usually.In order to increase the efficiency of heating surface of burner 30, the present invention heats the introducing air and introduces in the air so that the heat that produces in the burner still less enters.In other words, the chamber and the air stream that are formed by Dewar type container 150 allow before air arrives burner air to be carried out preheating from the used heat of burner, therefore are used as the regenerator of fuel cell 15.

Although the fuel processor 15 shown in Fig. 4 A and Fig. 4 B shows sealing monolithic construction 100 Dewar type containers 150, the present invention also can adopt other structure of Dewar type container 150 and implement the burner 30 of one or two above-mentioned Dewar type container function or the relation between reformer 32 and the Dewar type container 150.Fig. 4 D show according to another embodiment of the invention prolongation cold air flow through the cross-sectional view of fuel processor 15 in the convection current path of hotter Dewar type container wall 254.Fuel processor 15 comprises the tubular design of burner 30 and reformer 32.

Dewar type container 250 makes cold introducing air pass elongated heat-transfer path by route.Dewar type container 250 comprises that cross section is a spiral wall portion 254, and described spiral wall portion is around burner 30 and reformer 32.Spiral wall portion 254 limits spiral Dewar type container chamber 256.Cold air enters Dewar type container chamber 256 at Dewar type container import 252 places.The penetralia 257 of wall portion 154 is attached on the outer wall 258 of burner 30.Heat from burner 30 directly conducts by spiral wall portion 254.Therefore, inner 257 is the warmest parts of wall portion 154, and the wall portion 254 at 252 places that enter the mouth is normally the coldest.Air warms in the process of advancing by Dewar type container chamber 256 gradually.When air was inwardly advanced, the temperature of wall portion 254 rose, and the heat that can be used for being passed to air rises equally.Instantaneous temperature according to air.Heat loss amount from wall portion 154 also can the inwardly preceding and then increase along with air.

Spiral Dewar type container 250 has prolonged the introducing cold air and has been interacted by the convection current between the wall portion of burner heating.Dewar type container 250 has also increased along given wall portion and the tropospheric quantity radially by the fuel processor center.Shown in Fig. 4 D, Dewar type container 250 is along given 4-5 wall portion and the troposphere of radially comprising, this depends on the position of number of computations.Wall portion radially and tropospheric quantity can change according to design.In one embodiment, spiral Dewar type container 250 is configured along radially having 1 layer to about 50 wall portions and troposphere by the given of fuel processor center.3 layers to 20 layers are applicable to multiple applicable cases.Channel width 260 limits the conduit space between the adjacent wall portion 254.In one embodiment, channel width 260 about 1/4 millimeter to about 5 millimeters scope.

Can remove layer as constructing spiral Dewar type container 250 on aluminium or the zinc by nickel is electroplated onto.Fig. 4 H shows the spiral Dewar type container 250 of the expansion form that is in according to another embodiment of the invention in the initial construction process.Initial aluminum or zinc layer 262 are added with control channel width 260 in the operation of rolling.Can remove layer 262 electroplates together with the selected material such as the nickel of wall portion 214 subsequently.After described process, thereby the employing galvanoplastics etches aluminium or therefore the zinc layer stays spiral Dewar type container 250.

Spiral Dewar type container 250 shown in Fig. 4 H also adopts and is wound on reformer 32 relief or folding burner structure 264 on every side.Fig. 4 I and Fig. 4 J show the carrier coating 266 in the wall portion 268 of burner 30 according to two embodiment of the present invention.For the folding burner structure 264 shown in Fig. 4 I, will comprise on the both sides of carrier coating 266 paint wall portions 268 of burner catalyst 104.

Fig. 4 J shows the planomural 270 that is applicable in the spiral Dewar type container 250.Planomural 270 comprises along its surface etching or otherwise the passage 272 that is provided with.The carrier coating 266 that comprises burner catalyst 104 is added on the surface of planomural 270 and passage 272 subsequently.

The fuel processor of fuel processor 15 shown in Fig. 4 D is suitable for comprising the inner heat that produces very much.In one embodiment, burner 30 operation and hull outside under greater than about 350 degrees centigrade temperature keeps less than about 75 degrees centigrade.Fuels sources such as methyl alcohol and propane burning that this for example helps using higher temperature to make burning in the device 30.

Dewar type container shown in Fig. 4 A and 4D can be considered to " multichannel ", this be because introduce air on a plurality of surfaces by between warmer surface and colder air, to carry out convective heat transfer.Embodiment shown in Fig. 4 A shows two-channel system, and air passes through two Dewar type container chambers in described system, and the embodiment shown in Fig. 4 D shows the N channel system, and wherein N is the quantity of edge by the given Dewar type container wall radially at fuel processor center.

Fig. 4 E shows the cross-sectional view of multichannel Dewar type container 300 according to another embodiment of the invention.Dewar type container 300 comprises four Dewar type container wall 302a-d that are connected on the shell wall 304.Dewar type container 300 partly comprises monolithic construction 100.Dewar type container wall 302a and shell wall 304 synergies are to seal monolithic construction 100, and described monolithic construction comprises burner 30.Dewar type container wall 302b and shell wall 304 are sealed Dewar type container wall 302a and burner 30.Similarly, Dewar type container wall 302c and shell wall 304 are sealed Dewar type container wall 302b, and Dewar type container wall 302d and shell wall 304 are sealed Dewar type container wall 302c.Dewar type container wall 302a-d has formed four volumes, and air passes through in warmer wall portion and the reception heat so that introduce.Air enters Dewar type container inlet port 310 and flows through Dewar type container 308a and enter in the 308b of Dewar type container chamber by aperture 312 after advancing by whole chamber 308a substantially.Air entered to sequence before entering burner inlet 314 and subsequently by chamber 308c and 308d.

Fig. 4 F and Fig. 4 G show the cross section of the fuel processor 15 that comprises monolithic construction 452 and multichannel Dewar type container 450 according to another embodiment of the invention.Monolithic construction 452 comprises a plurality of reformers chamber 454 in the core that is arranged on structure 452.A plurality of combustors 456 around and with reformer chamber 454 4 edge joints circle.The boiling device 458 of reformer is disposed in the cross section of combustor 456, and the boiling device 460 of burner is disposed in the cross section outside.

Dewar type container 462 comprises four Dewar type container wall 462a-d.In the cross section shown in Fig. 4 F, Dewar type container wall 462a is around monolithic construction 452.Dewar type container wall 462b around and seal Dewar type container wall 462a.Dewar type container wall 462c centers on and seals Dewar type container wall 462b, and Dewar type container wall 462d centers on and seal Dewar type container wall 462c.Dewar type container wall 462a-d has formed four Dewar type container volumes so that the introducing air is passed through and the reception heat.Shown in Fig. 4 G, air enters Dewar type container inlet port 464 and flows through Dewar type container chamber 468a and enter in the 468b of Dewar type container chamber after advancing by whole chamber 468a substantially along the length of monolithic construction 452.Air led to chamber 468c and chamber 468d from chamber 468b to sequence subsequently before entering burner inlet 40.

Fig. 6 A-6J shows fuel processor 615 according to another embodiment of the invention.Fig. 6 A shows the top view of fuel processor.Fig. 6 B-Fig. 6 F shows along the sectional view of the fuel processor 615 of a plurality of profile interceptings.Fig. 6 G-Fig. 6 J shows along the front cross sectional view of the fuel processor 615 of a plurality of profile interceptings.Fig. 6 J shows the extension side cutaway view of the part of the fuel processor 615 shown in Fig. 6 G.

Fuel processor 615 comprises reformer 632, burner 630, boiling device 634, depressed place portion 638, shell portion 675, preferential oxidizer 650 and plate 641,649 and 653 (Fig. 6 J).Although now will present invention is described in conjunction with the methanol consumption that is used to produce hydrogen, should be appreciated that fuel processor of the present invention can consume another kind of fuels sources, as those skilled in the art will recognize ground.

Fuel processor 615 comprises substrate 640,642 and 644.Every substrate 640,642 and 644 is included in two flat substantially faces on the opposite side of substrate.In one embodiment, every substrate 640,642 and 644 comprises that silicon and substrate in batch 640,642 and 644 are known as " chipset ".In the face of substrate 640,642 and 644, form passage to form reformer 632, burner 630, boiling device 634 and preferential oxidizer 650.Passage refers to the conduit that forms in substrate.Every channel lead moves by gas and liquid wherein.Silicon substrate 640,642 and 644 allows to use semiconductor fabrication with structure fuel processor 615.In specific embodiment, use etch process such as Deep Reaction ion(ic) etching (DRIE etch) and wet etching (wet etch) technology in silicon substrate, to form reformer channels 637, burner channel 631 and/or boiling device passage 635.In another embodiment, every substrate 640,642 and 644 comprises silicon alloy, carborundum and metal such as stainless steel, titanium or Yin Kenaier.Metal helps heat and is transmitting between burner 632 and the reformer 630 and between burner 632 and boiling device 634.Microelectromechanical systems (MEMs) manufacturing technology such as stratification and etching technique also can be in order to make substrate 640,642 and 644 and be arranged on wherein passage.

Referring to Fig. 6 B, Fig. 6 G and Fig. 6 J, boiling device 634 is heating methanol before reformer 632 receives methyl alcohol.Boiling device 634 comprises one group of boiling device passage 635 among the face 640a that is arranged on substrate 640.Plate 641 is attached to the open side that face 640a went up and covered every passage 635.Boiling device 634 comprises the volume of being determined by the accumulated size of the boiling device passage 635 in the channel group.

Boiling device 634 is set at the heat of position to produce in the reception burner 630 near burner 630.In an illustrated embodiment, boiling device passage 635 is set on the face 640a with the face 640b opposing substrates 640 of substrate 640, and described 640b comprises burner channel 631 (Fig. 6 J).Heat subsequently 1) by from burner 630 conduction by substrate 640 arrival boiling devices 634 and 2) transmit by carrying out convection current to the methyl alcohol by wherein from the wall portion of boiling device passage 635.In one embodiment, boiling device 634 is configured so that the liquid methanol vaporization.The gas methyl alcohol that flows out boiling device 634 arrives soon after reformer 632 so that carry out the gas interaction with catalyst 702.

Boiling device 634 receives methyl alcohol by fuels sources inlet 681 (Fig. 6 B), and described fuels sources inlet is attached to the methyl alcohol supply line 27 shown in Figure 1B.Inlet 681 comprises among the 728b of wall portion that is arranged on depressed place portion 638 and is configured to receive the socket 682 that methyl alcohol is transported to the pipeline 27 of fuel processor 615.Inlet manifold 684 is transported to reformer channels 635 substrate 640 and the substrate 640 with liquid methanol from socket 682.Manifold 684 comprises by submissive material 710, substrate 640 and 642 and the eyelet or the hole of plate 641.By 726 pairs of materials 710 of bolt, substrate 640 and 642 and plate 641 be compressed in sealing manifold 684 between the parts.

Reformer 632 comprises one group of reformer channels 637 among the face 642b that is arranged on substrate 642.Plate 649 is attached to the open side that face 642b went up and covered every passage 637.Reformer 632 comprises the volume of being determined by the cumulative volume of the reformer channels in the channel group 637 and size.More specifically, reformer 632 comprises the segmentation volume, and described segmentation volume comprises the contribution from many passages 637.In one embodiment, the cross section of passage 637 is substantially rectangle.The width 637b of passage 637 is applicable to multiple applicable cases about 20 between about 400 microns.In specific embodiment, passage 637 comprises about 100 microns width 637b.Also can use the size characteristic of one or more aspect ratios as passage 637.Length 637c and the ratio of width 637b have been described the area of plane of the passage 637 on the face of substrate.Have about 10000:1 and be applicable to multiple applicable cases to the passage 637 of the interior length-width ratio of about 200:1 scope.In specific embodiment, passage 637 comprises the length-width ratio of about 200:1.Degree of depth 637a has described the cross sectional dimensions of passage 637 along its length 637c with the ratio of width 637b.Be included in about 2:1 and be applicable to multiple applicable cases to the passage 637 of the interior depth over width ratio of about 100:1 scope.In specific embodiment, passage 637 comprises the depth over width ratio of about 630:1.Channel group comprises at least one passage.But the required hydrogen output of the quantity of the passage 637 of reformer 632 and size based on fuel processor 615 changes as the production capacity based on fuels sources and reformer catalyst 702.

Reformer 632 is configured to receive methyl alcohol after methyl alcohol is by boiling device 634.Reformer 632 receives methyl alcohol by pipeline 671, and described pipeline will be exported methyl alcohol is transported to reformer 632 from the passage 635 of boiling device 634 passage 637 (Fig. 2 B).More specifically, pipeline 671 makes methyl alcohol outwards be communicated with, cross substrate 640 and 642 and lead to passage 637 on the face 642b of substrate 642 from the face 640a of substrate 640.

Catalyst 702 in the reformer 632 helps producing hydrogen.Catalyst 702 is with methyl alcohol 17 reactions and help producing hydrogen and carbon dioxide.In one embodiment, catalyst 702 comprises the carrier coating that is arranged on every passage 637.The carrier coating of required catalyst can or spray on the substrate and carries out deep etch to keep flat surperficial 642b by sputter.Catalyst 702 forms in the wall portion of every passage 637 as thin layer subsequently.When methyl alcohol was used as hydrocarbon fuel sources, a kind of suitable catalyst 702 comprised CuZn.Other material that is applicable to catalyst 702 for example comprises platinum, palladium, platinum/palladium mixture and other noble metal catalyst.The combination of following material also can be used in the catalyst 702: Cu, Zn, Pt, Ru, Rh, aluminium oxide, calcium oxide, silica and/or iridium.

Preferential oxidizer 650 has been blocked the discharge hydrogen of reformer 632 and has been reduced the amount of carbon monoxide in the effluent (Fig. 2 G).Preferential oxidizer 650 comprises the one group of oxidator passage 651 (Fig. 2 J) among the face 644b that is arranged on substrate 644.Plate 653 is attached to the open side that face 644b went up and covered every oxidator passage 651.Preferential oxidizer 650 comprises the volume of being determined by the accumulated size of the boiling device passage 651 in the channel group.The oxygen (Fig. 2 C) that preferential oxidizer 650 adopts from air intake 707.

Air intake 707 receives from the air of environment space and comprises socket 711 and manifold 712.Socket 711 is set among the 728b of wall portion of depressed place portion 638 and has certain size to receive the pipeline that air is transported to fuel processor 615.Socket 711 leads to the manifold 712 that air is transported to the passage 651 in the substrate 633.More specifically, manifold 712 cross submissive material 710, by plate 640, by substrate 642 and 640, by plate 649, by spacing body 730 and by substrate 644 to lead to passage 651.Catalyst 714 is washed in the wall portion that is layed onto passage 651 and can be comprised a kind of in the following material or combination: Cu, Zn, Pt, Ru, Rh, aluminium oxide, calcium oxide, silica, iridium and/or for carbon monoxide comparison carbon dioxide another kind of catalyst more preferably.

Outlet 87 makes hydrogen and fuel processor 615 external communications (Fig. 2 E) that form in the reformer 632.In the fuel cell system shown in Figure 1B 10, aperture 87 makes hydrogen be communicated to pipeline 39 hydrogen is offered fuel cell 20.Aperture 87 is set in the wall portion of depressed place portion 638 and comprises socket 701 and the manifold of opening by wall portion 728 703.Socket 701 have certain size with the metal that receives pipeline 39 or plastic conduit so that hydrogen self-ignition material processor 615 outwards is communicated with.Binding agent can be fixed to pipeline on the inwall of socket 701.Another kind of optional mode is that metallic conduit can be brazed on the inwall of socket 701.When fuel processor 615 comprises preferential oxidizer 650 as shown in the figure, manifold 703 with hydrogen from preferential oxidizer, transport out, by substrate 644, by spacing body 730, by plate 649, by substrate 642 and 640, by plate 640, by submissive material 710 and arrive socket 701 (Fig. 6 B).

In another embodiment, preferential oxidizer 650 is not used for fuel processor 615 and reformer 632 is configured to hydrogen is directly come out from fuel processor 615.In this case, the passage 637 in the reformer 632 provides to manifold 703 gas so that hydrogen self-ignition material processor 615 outwards is communicated with.When fuel processor 615 does not comprise preferential oxidizer, manifold 703 with the reformer channels 637 of hydrogen from substrate 642 transport out, by substrate 642 and 640, by plate 640, by submissive material 710 and arrive socket 701.

Hydrogen production process in the reformer 632 be absorb heat slightly and from burner 630 draw heat.Burner 630 produces heat and is configured to heat is offered reformer 632.Burner 630 comprises two groups of burner channel 631: be arranged on first group of passage 631a among the face 642a of substrate 642 and be arranged on second group of passage 631b among the face 640b of substrate 640. Substrate 640 and 642 is placed with attached so that passage 631a on opposite face 642a and the 640b and 631b lead to each other.Burner 630 comprises the volume of being determined by the accumulated size of burner channel 631a and passage 631b.

Burner 630, boiling device 634 and preferential oxidizer 650 comprise the volume of being determined by the cumulative volume of the passage in its corresponding channel group and size respectively.The channel size of describing in conjunction with reformer channels 637 also can be used for the passage 635 of boiling device 634, the passage 631 of burner 630 and the passage 651 of preferential oxidizer 650 above.Therefore, above-described channel width, passage length width ratio and the channel depth width of passage 637 of being used for is than also being applicable to passage 635, passage 631 and passage 651.

In one embodiment, burner 630 adopts catalytic combustion to produce heat.Catalyst 704 in the burner 630 helps to produce heat by the burner fuel of chamber.In one embodiment, methyl alcohol produces heat and catalyst 704 and helps using methyl alcohol to produce heat in burner 630.Suitable methyl alcohol burner catalyst 704 can comprise platinum, palladium, iron, tin oxide, other noble metal catalyst and reducible oxide.Other suitable catalyst 704 materials comprise a kind of or combination in the following material: Cu, Zn, Pt, Ru, Rh, aluminium oxide, calcium oxide, silica and/or iridium.In another embodiment, the useless hydrogen from fuel cell 20 produces heat under the situation that has catalyst 704.Catalyst 704 can obtain from the known multidigit seller of those skilled in the art commercial.In one embodiment, catalyst 704 comprises the carrier coating that is arranged on every passage 631.Can use well-known mixing, injection, vaporization and method of reducing that the carrier coating of required catalyst 704 is injected in the microchannel.Catalyst 704 forms the layer of thin porous and high surface subsequently in the wall portion of every passage 631.

Burner 630 comprises the inlet 714 (Fig. 6 F) that receives methyl alcohol 17.Burner inlet 714 comprises among the 728b of wall portion that is arranged in the depressed place portion 638 and is configured to receive the socket 716 that methyl alcohol is transported to the pipeline 27 (Figure 1B) of fuel processor 615.Methanol inlet manifold 718 is transported to burner channel 631 substrate 640 and 642 with methyl alcohol from socket 716.

The air that comprises oxygen enters depressed place portion 638 by air inlet port 691 (Fig. 6 F).Burner 630 uses oxygen so that methyl alcohol is carried out catalytic combustion.Burner outlet 720 (Fig. 6 D) makes the effluent of formation in the burner 630 and the external communications of fuel processor 615.Burner outlet 720 comprises in the wall portion that is arranged on depressed place portion 638 and is configured to receive effluent is transported socket 722 away from the pipeline of fuel processor 615.Burner outlet manifold 124 is transported to socket 716 with effluent from passage 631.

Some fuels sources produce additional heat in burner 630, or more effectively produce heat, have the temperature of rising.In one embodiment, fuel processor 615 is included in burner 630 and receives the fuels sources boiling device of heating methanol before.In this case, boiling device receives methyl alcohol by fuels sources inlet 714.Boiling device is set at the heat of position to produce in the reception burner 630 near burner 630.

Burner 630 is configured to heat offered reformer 632 and be configured to heat is offered boiling device 634.The heat that produces among every burner channel 631a of one group of burner channel 631a permission is set in substrate 642 to be transmitted by the passage 637 that substrate 642 arrives reformers 632 and reformer 632 by conduction.Heat enters in the catalyst 702 near 642 conduction of the substrate every passage 637 subsequently.But heat is convection current admission passage 637 interior and heating methanol also.The heat that produces among every passage 631b of one group of burner channel 631b permission is set in substrate 640 to be transmitted by the passage 635 that substrate 640 arrives boiling devices 634 and boiling device 634 by conduction.Be placed on burner 630 and reformer 632 on the identical chip and permission heat closer to each other directly directly flows through thin independent substrate 642 and enters in the reformer catalyst 702 from burner catalyst 704.Because heat is transmitted conduction and is left a catalyst structure, enters next catalyst micro-structural by thin solid, so fuel processor 615 does not need big heat transfer zone so that heat is passed to reformer 632 from burner 630.This has reduced the total measurement (volume) of fuel processor 615.Burner 630 does not need to comprise burner channel 631 in substrate 640 and substrate 642.If only there is a substrate to comprise one group of burner channel 631, heat can conduct to another piece substrate from the substrate with described burner channel group and conduct to boiling device 634 subsequently or reformer 632 so.

Although be described so far, should be appreciated that some embodiments of the present invention can adopt the electric burner 630 that is configured to that heat offered reformer and is configured to heat is offered boiling device in conjunction with 632 pairs of fuel processors 615 of catalytic burner.Electricity burner 630 comprises the stratie that produces heat in response to input current.Electricity burner 630 can be set at thinks between substrate 640 and the substrate 642 that two substrates 640 and 642 provide conduction heat transfer.

The opening portion of the passage in the adjacent substrate of plate 641,649 and 653 coverings and sealing and every block of plate.Every block of plate 641,649 and 653 has also increased the mechanical strength of chipset.Every block of plate 641,649 and 653 for example can use suitable binding agent attached and be bonded to substrate.In specific embodiment, plate 641,649 and 653 comprises glass, and described glass is compared the total thermal loss that has low heat conductivity and reduced fuel processor 615 with silicon.

The reformer 632 in the depressed place portion 638 maintenance fuel processors 615 and the position of boiling device 634.Depressed place portion comprises bolt 726, one group of dock wall 728, spacing body 730, submissive material 710 and is used for process gas or liquid transport are arrived and leave the socket 684,711,722,701 and 716 of reformer 632, burner 630 and boiling device 634.Dock wall 728 comprises the fastening wall 728a of portion, the wall portion 728b relative with the fastening wall 728a of portion and the one or more sidewall 728c (Fig. 6 C) that extend between fastening wall 728a of portion and the 728b of wall portion.The fastening wall 728a of portion comprises the screwed hole that is used to receive bolt 726.Also available spring is replaced bolt 716 chipset is pushed against in submissive material 710 and the depressed place portion 638.Dock wall 728 combinations are to form the case of part around the part of reformer 632, boiling device 634 and burner 630.Dock wall 728 for example can comprise glass bonded mica, pottery, glass filling polyester or metal such as copper.

Depressed place portion 638 applies the submissive fastening force by a part of substrate 640 and a part of substrate 642.Bolt 726 spirals are by the fastening wall 728a of portion, or length of spring compressed is applied to compression stress on the plate 653 until it.This compression stress with substrate 640 and 642 and plate 641,649 and 653 be locked in the appropriate position, and prevent their dislocations in processing procedure.Where relative the 728b of wall portion and the fastening wall 728a of portion several and when its translation during by the parts in the heap therebetween, and the resistance of the compression stress that bolt 726 is provided is provided.The position and the line 732 between the wall portion 728 that run into plate 653 at bolt 726 can be in order to describe the compression stress path (Fig. 6 G) between bolt 726 and the 728b of wall portion roughly.Compression stress produces in the screw thread of bolt 726, near the position that transmission is met by plate 653 and bolt 726 a part of plate 653, transmit by near a part of substrate 644 the line 732, by near a part of spacing body 730 the line 732, by near a part of substrate 649 the line 732, by near a part of substrate 642 the line 732, by near a part of substrate 640 the line 732, by near a part of plate 641 the line 732, by near submissive material 710 of a part the line 732 and the arrival wall 728b of portion.In this case, be subjected to the substrate 640 of effects of compressive of bolt 726 and 642 part and comprise that compression stress propagates by near the end the position of substrate.In one embodiment, substrate 640 and 642 and the compression stress that applies by bolt 726 (or spring) of plate 641,649 and 653 re-assembly cantilever beam and it is kept together and be in the appropriate position.

The fastening force that submissive material 710 obstruction bolts 726 provide and the upper limit that produces submissive fastening force.Shown in Fig. 6 D, submissive material 710 be set between plate 641 and the 728b of wall portion and extreme plate 641 and the 728b of wall portion between fastening force.Submissive material 710 comprises that known material and the compression stress that applies for bolt 726 set the predetermined compliance of the upper limit.In one embodiment, material 710 comprises less than the rigidity of substrate 640 or 642 or the rigidity or the modulus of elasticity of modulus of elasticity.Submissive material 710 allows to be applied to Stress Transfer on substrate 640 and 642 subsequently to material 710.This has reduced the local stress on the substrate 640 and 642 and has set the upper limit for the stress on the substrate 640 and 642.When substrate 640 and 642 comprised fragile material such as silicon, material 710 prevented from the function of fuel processor 615 is produced infringement by machinery obstruction and the protective capability that increases substrate 640 and 642 pairs of external stresses.By provide to be applied to substrate 640 and 642 and plate 641 and 649 on the machinery of power hinder, submissive material 710 has reduced mechanical stress in substrate 640 or 642 and be attached at transmission between the pipeline in the socket in the depressed place portion 638.The distortion of submissive material 710 also can reduce near the material 710 substrate 640 and the pressure in 642 the part changes.Submissive material 710 also reduced owing to the thermal expansion of each parts and contraction cause substrate 640 and 642 and plate 641 and 649 between the stress that brings out, therefore cause producing the firmer mechanical structure of reformer 632, boiling device 634 and burner 630 and the protection of increase.Be suitable for the material that submissive material 710 uses comprise high temperature silicone, Teflon or have suitable compliance and reply fuel processor 615 in any other material of ability of used elevated temperature.In specific embodiment, submissive material 710 comprises the Grafoil that the Graftech International of WilmingtonDE provides.

In one embodiment, submissive material 710 is as the packing ring with outlet of entering between the inside of sealing plate 640 and the 728b of wall portion.Except seal gas flow, this packing ring also makes chipset and depressed place portion 638 and Dewar type container 150 heat keep apart (vide infra), has reduced the thermal loss from fuel processor 615 thus.

The isolation that spacing body 730 keeps between substrate 642 and the substrate 644.This has reduced from substrate 642 to heat transfer that colder substrate 644 carries out and allow more heat to remain on the substrate 642 and be passed to reformer 632 (as the methyl alcohol in catalyst 702 or the passage 637).In one embodiment, spacing body 730 comprises rigidity and low Heat Conduction Material such as pottery.Another kind of optional mode is, spacing body 730 can comprise that the submissive material 710 of another layer is with the power in the further control fuel processor 615 and protective substrate 640 and 642 and plate 641 and 649.

Dock wall 728 provides mechanical protection for internal part such as substrate 640 and 642, plate 641 and 649, reformer 632, burner 630 and the boiling device 634 of fuel processor 615.Shell portion 675 is attached in the depressed place portion 638 and also provides mechanical protection for the internal part of fuel processor 615.Shell portion 675 comprises the one group of wall portion 77 that comprises reformer 632, burner 630 and boiling device 634 to small part.Wall portion 77 for example comprises suitably hard material such as metal, pottery or rigidity polyester.Shell portion 675 can use binding agent or be attached in the depressed place portion 638 by one or more bolts.Shell portion 675 and depressed place portion 638 seal reformer 632, burner 630 and boiling device 634 together.As being described ground in conjunction with Dewar type container 150, shell portion 675 and depressed place portion 638 also can be fuel processor 615 the heat management advantage are provided.

Though fuel processor 615 comprise bolt 726 so that compression stress to be provided should envision other mechanical device can be in order to apply power to keep reformer and the position of boiling device in fuel processor.For example, available being configured to replaced bolt 726 with spring clip or pad that compression stress is provided on the chipset.

Depressed place portion 638 also comprises and is used to make gas and liquid and fuel processor 615 inside and outside entering and outlet of being communicated with.By above-mentioned aperture 681 and socket 682, depressed place portion 638 allows methyl alcohol is transported by the 728b of wall portion arrival reformer 632 from external fuel processor 615.Similarly, by above-mentioned aperture 87 and socket 701, depressed place portion 638 allows hydrogen is arrived the external fuel processor from the wall portion that reformer transports by comprising the portion of depressed place.Therefore depressed place portion 638 also provides gas and liquid interconnection performance for the parts that kept by depressed place portion 638.

Fig. 5 shows the technological process 500 that is used for producing at fuel processor according to an embodiment of the invention hydrogen.Fuel processor comprises burner, reformer and comprises the Dewar type container of burner and reformer at least in part.Although the present invention discusses Dewar type container in conjunction with ring-type reformer described herein and burner design so far, should expect that Dewar type container described herein also is useful for the heat in comprising other reformer and burner design.Multiple structure employing is arranged on burner top, plane and goes up or following plane reformer.The microchannel design of making in silicon is generally adopted this stacked planar configuration and will be benefited from Dewar type container described herein.

Technological process 500 begins (502) by produce heat in burner.The catalytic burner structure can comprise the microchannel design on above-described those structures or the silicon.Comprise further describing at exercise question for the inventor and in the patent application of common all common pending trials of the date application identical for " the little fuel processor in plane " and name Ian Kaye to the microchannel fuel processor that is suitable for using with the present invention with present patent application.This application is introduced into for your guidance for all purposes.Catalyst in the burner helps producing heat existing under the situation of heating fuel.Burner also can adopt and comprise the electric burner that produces the stratie of heat in response to input current.

Air enters the aperture of Dewar type container and passes through Dewar type container chamber (504).For the Dewar type container shown in Fig. 4 A, burner 30 passes through Dewar type container chamber 156 with air by the relative direction of the direction of combustor 105 at least in part with Dewar type container 150 common wall portions and air edge.

Use the heat that produces in the burner subsequently and in the Dewar type container chamber heated air (506).Heat marches to Dewar type container chamber 156 by conduction heat transfer from burner 30.Heat also can march to the Dewar type container chamber from burner by convection current and/or radiant heat transfer.In case be in the Dewar type container chamber, air is usually by being heated to the convective heat transfer that air carries out from the Dewar type container wall.In one embodiment, Dewar type container and burner common wall portion and use are from the air in the heat heating Dewar type container chamber of common wall portion.Also may continue to other wall portion in the Dewar type container and heat is passed to another non-shared Dewar type container wall from common wall portion after, heat air the Dewar type container chamber from the heat of burner wall portion.The heat of advancing between common wall portion and non-shared Dewar type container wall is by conducting between the connecting wall portion or transmitting towards radiation between the wall portion.

Technological process 500 will be warmed air supply to burner (508) subsequently after air is subjected to heating in the Dewar type container chamber.Usually, fuel processor comprises the outlet of Dewar type container chamber and the inlet of burner-and pipe-line equipment at any intermittence of allowing that heated air passes through betwixt.For the fuel processor shown in Fig. 2 A, be in the Dewar type container 150 at place, burner end and the space between the burner 30 and make air move to burner by route from Dewar type container.

Thereby air is used for burner subsequently produces heat to carry out catalytic combustion.The heat that produces is passed to reformer (510) from burner subsequently.In reformer, heat is used for fuels sources is reformed to produce hydrogen (512) subsequently.

Junior three element (502,504 or 506) of technological process 500 has also formed the method for the heat in the management fuel processor.In this case, the heat that produces in the burner (502) arrives the air (504) in the Dewar type container.Dewar type container 150 makes the parts such as the hot at least in part heat of keeping apart and comprising in the fuel processor of burner of fuel processor enclosure interior.Therefore Dewar type container has reduced from the temperature gradient between the thermal loss of fuel processor and help management burner and the housing outer surface.That Dewar type container also can comprise prolongation and/or a plurality of Dewar type containers chamber, air is by the heating of described Dewar type container chamber and the heat that is subjected to producing in the burner.Fig. 4 A shows the second Dewar type container chamber 158 that forms between the housing of Dewar type container and fuel processor.Air at first enters in the Dewar type container chamber 156 subsequently by chamber 158.Fig. 4 D shows the spiral Dewar type container of the Dewar type container chamber 408 that comprises prolongation.In this case, Dewar type container 250 comprises along with introducing air provides a wall portion of heat cumulatively near burner.Fig. 4 E shows the Dewar type container 300 that comprises four part Dewar type container chambers 308, and wherein the introducing air is heated successively along with introducing air in each Dewar type container chamber near burner.Fig. 4 F shows the Dewar type container that comprises four ring-types and concentric rectangle Dewar type container chamber 408, each described Dewar type container chamber along with introduce air to burner advance and successively heating introduce air.

Although invention has been described according to a plurality of preferred embodiments, exist to fall within the scope of the present invention and be concise and to the point cause abridged remodeling, displacement and equivalent.For example, although as shown in Figure 3A, reformer 32 comprises chamfering, and the present invention can adopt non-chamfering in reformer 32.In addition, although invention has been described according to the monolithic construction 100 that forms big volume reformer 32, the invention is not restricted to be arranged on the big volume reformer in the monolithic construction.Therefore expection should be determined scope of the present invention in conjunction with claims.

Claims (14)

1, a kind of method that is used for producing at fuel processor hydrogen, described fuel processor comprise burner, reformer and comprise the Dewar type container of described burner and reformer to small part that described method comprises:

In described burner, produce heat;

Make process gas or liquid by the Dewar type container chamber;

Use the heat that produces in the described burner to heat described process gas or liquid in the described Dewar type container chamber, wherein use the heat of the shared first wall portion of free described burner and described Dewar type container to heat described process gas or liquid, and wherein heat is passed to the wall of described Dewar type container from described burner after, just heat described process gas or liquid the described Dewar type container chamber;

After described process gas or liquid have been subjected to heating, it is supplied to described burner in described Dewar type container chamber;

With the heat transferred that produces in the described burner to described reformer, wherein said fuel processor comprises by described burner and the second shared wall portion of described Dewar type container, and described fuel processor is configured to allow to carry out conduction heat transfer from the burner catalyst by described wall portion and is communicated with; With

Fuels sources is reformed to produce hydrogen.

2, method according to claim 1, wherein said process gas or liquid are along passing through described Dewar type container chamber with described process gas or liquid by direction to the opposite direction of small part of described combustor.

3, method according to claim 1, wherein said Dewar type container chamber are included in the space that forms between one group of wall portion of the wall portion of described burner and described Dewar type container.

4, method according to claim 1, wherein said fuel processor comprises the housing that comprises described Dewar type container, form the second Dewar type container chamber with described housing and described Dewar type container, the described second Dewar type container chamber received described process gas or liquid before described Dewar type container chamber receives described process gas or liquid.

5, method according to claim 4 comprises that further the heat that produces in the described burner of use heats described process gas or the liquid in the described second Dewar type container chamber.

6, method according to claim 5 wherein heats described process gas or liquid and is included in and carries out convection current or radiant heat transfer between the shared wall portion of described burner and described Dewar type container.

7, method according to claim 6, wherein said Dewar type container comprise the radiating layer of the reflect radiation heat performance of the described inwall of improvement that is arranged on the described inwall.

8, a kind of method that is used for managing the heat of fuel processor, described fuel processor comprises burner, reformer and comprises the Dewar type container of described burner at least in part that described method comprises:

Produce heat in described burner, described burner has the combustor that comprises the burner catalyst;

Make process gas or liquid by the Dewar type container chamber; With

Use the heat that produces in the described burner to heat described process gas or liquid in the described Dewar type container chamber, wherein use the conduction or the radiant heat transfer of the shared wall portion of free described burner and described Dewar type container to heat described process gas or liquid.

9, method according to claim 8, wherein said process gas or liquid are along passing through described Dewar type container chamber with described process gas or liquid by direction to the opposite direction of small part of described combustor.

10, according to Claim 8 or 9 described methods, wherein said Dewar type container chamber is included in the space that forms between one group of wall portion of described burner wall portion and described Dewar type container.

11, according to Claim 8 or 9 described methods, wherein said fuel processor comprises the housing that comprises described Dewar type container, described housing and described Dewar type container form the second Dewar type container chamber, and the described second Dewar type container chamber received described process gas or liquid before described Dewar type container chamber receives described process gas or liquid.

12, method according to claim 11, further comprise and use the heat that produces in the described burner to heat described process gas or liquid in the described second Dewar type container chamber, wherein said burner under greater than about 200 degrees centigrade temperature, operate and the living thermal process of the outside in described burner of described housing in maintenance less than about 50 degrees centigrade.

13, according to Claim 8 or 9 described methods, wherein said Dewar type container is included on the cross section spiral around the wall portion of described burner.

14, according to Claim 8 or 9 described methods, wherein said Dewar type container is included in the wall portion around described burner of spiral on the cross section, wherein said Dewar type container comprises that a part of described spiral wall portion and described burner partly comprise the described spiral wall of second portion portion, and described second portion comprises described burner catalyst.

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