CN1941483A - Fuel reformer - Google Patents
Fuel reformer Download PDFInfo
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- CN1941483A CN1941483A CNA2006101278931A CN200610127893A CN1941483A CN 1941483 A CN1941483 A CN 1941483A CN A2006101278931 A CNA2006101278931 A CN A2006101278931A CN 200610127893 A CN200610127893 A CN 200610127893A CN 1941483 A CN1941483 A CN 1941483A
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- fuel reformer
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
- C01B2203/067—Integration with other chemical processes with fuel cells the reforming process taking place in the fuel cell
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Fuel Cell (AREA)
Abstract
The present invention discloses a fuel reformer including: a first pipe; a second pipe which is disposed in the first pipe; a main heat source, which includes an oxidation catalyst, filling the second pipe adapted to generate thermal energy with a predetermined temperature range through an oxidation reaction of a fuel using the oxidation catalyst; an auxiliary heat source which includes a torch connected to the second pipe to ignite and burn the gaseous fuel, thereby preheating the oxidation catalyst to a reaction starting temperature range; and a reforming reaction unit which includes a reforming catalyst filling a space between the first and second pipes to generate a reforming gas containing hydrogen through the reforming reaction of the fuel using the reforming catalyst by using the thermal energy generated by the main heat source.
Description
Technical field
The present invention relates to a kind of fuel reformer, more specifically, relate to a kind of fuel reformer that produces heat energy by the fuel oxidation reaction.
Background technology
As everyone knows, fuel cell constitutes a kind of system that uses fuel to produce electric energy.
In fuel cell, polymer dielectric film fuel cell (polymer electrolyte membranefuel cell) has good output characteristic, low operating temperature, the characteristic that starts and respond fast.In addition, polymer dielectric film fuel cell helps having the scope of application widely, comprises in the portable power source that is used in vehicle, is used in the distributed power source in dwelling house or the building, and is used in the Miniature Power Unit of electronic instrument.
Use the fuel cell system of polymer dielectric film fuel cell to comprise: the fuel battery main body (for convenience following, as to be called " heap ") that is called heap; Fuel reformer, this reformer fuel reforming to be generating hydrogeneous reformed gas, and this reformed gas is offered fuel battery main body; Provide the oxidant gas of oxidant gas that the unit is provided to heap.
Therefore, the polymer dielectric film fuel cell system produces electric energy by the electrochemical reaction between reformed gas and the oxidant gas, and described reformed gas is from the fuel reformer in the heap, and described oxidant gas provides the unit to provide by oxidant gas.
Fuel cell reformer comprises: heat source unit, and it uses the method by oxidation catalyst oxidizes fuel to produce heat energy; The reforming reaction unit, it uses described heat energy to make fuel generation reforming reaction generate reformed gas.
At this moment, the liquid fuel that thermal source can be by oxidation such as methyl alcohol and ethanol or produce heat energy such as the method for the gaseous fuel of LPG and LNG.Especially, use the thermal source of liquid fuel to react, can in predetermined temperature range, produce heat energy, under the condition of using oxidation catalyst, even at room temperature produce heat energy by fuel oxidation.
On the other hand, when the thermal source that fuel reformer comprised of routine uses the method for oxidizing gas fuel, because described thermal source can not at room temperature use oxidation catalyst that the oxidation reaction of gaseous fuel takes place, therefore need an additional preheater that oxidation catalyst is preheating to a predetermined temperature, make gaseous fuel that oxidation reaction can take place.
In addition, when the thermal source that fuel reformer comprised of routine uses the method for igniting and combustion of liquid fuel, because the energy efficiency of fuel reformer changes with the position of thermal source, then thermal source is by flame oxidation, therefore the durability of thermal source is damaged, and the new thermal source of the frequent substitution of having to, and then the useful life of reducing fuel reformer.
Summary of the invention
The invention provides a kind of fuel reformer, it can come the preheating oxidation catalyst by lighting with combustion fuel when fuel cell system begins to drive, and uses the oxidation catalyst generation oxidation reaction of preheating to produce heat energy.
According to an aspect of the present invention, provide a kind of fuel reformer, it comprises: first pipe; Place second pipe of described first pipe; Main heat source, it comprises the oxidation catalyst that is filled in described second pipe, and uses described oxidation catalyst to make fuel generation oxidation reaction have the heat energy of predetermined temperature range with generation; Auxiliary thermal source, it comprises the igniter that is connected with described second pipe, this igniter is lighted and the described gaseous fuel that burns, and therefore described oxidation catalyst is preheating to reaction start-up temperature scope; And reforming reaction unit, it comprises the reforming catalyst in the space that is filled between described second pipe and described first pipe, and the heat energy that uses described reforming catalyst and described main heat source to produce, make described fuel generation reforming reaction generate hydrogeneous reformed gas.
Of the present invention above-mentioned aspect in, described fuel reformer comprises that further carbon monoxide reduces the unit, and its structure is used for filling water gas converting catalyst to reduce the concentration of the carbon monoxide that contains in the described reformed gas in the space between described first pipe and described second pipe.
In addition, described fuel reformer further comprises the dividing plate that places between described first pipe and described second pipe, and this dividing plate is divided into a zone and a zone that is filled with water gas converting catalyst that is filled with reforming catalyst with the space between described first pipe and described second pipe.
In addition, described dividing plate has netted profile.
In addition, the reaction start-up temperature scope of described oxidation catalyst is from 150 ℃ to 300 ℃.
In addition, the temperature range of the described heat energy that is produced by main heat source is from 600 ℃ to 700 ℃.
According to a further aspect in the invention, provide a kind of fuel reformer, it comprises: the reactor block that comprises a plurality of reaction substrates, the oxidation reaction of first reactant of described reaction substrate by including a kind of fuel produces heat energy, and the reforming reaction of second reactant by including described fuel generates reformed gas; With the preheating unit that places described reactor block, its light and first reactant that burns so that the described reactor block of preheating.
Of the present invention above-mentioned aspect in, described preheating unit comprises: the shell that encapsulates described reactor block; Place the burner of described shell, it is used at the fired outside of described reactor block and burning first reactant.
According to a further aspect in the invention, provide a kind of fuel reformer, it comprises: one or more first reaction substrate, and it comprises first raceway groove that is used to allow include a kind of first reagent flow of fuel, layer of oxidation catalyst is formed on the surface of described first raceway groove therein; One or more second reaction substrate, it comprises second raceway groove that is used to allow include second reagent flow of described fuel, a reforming catalyst layer is formed on the surface of described second raceway groove therein; Reactor block by the bonding described first reaction substrate and the second reaction substrate formation; Preheating unit, it places described reactor block, to light and described first reactant that burns, so that described layer of oxidation catalyst is preheating to a reaction start-up temperature scope.
Of the present invention above-mentioned aspect in, described reactor block comprises by one or more cell cube with the described first reaction substrate and the second reaction substrate bonding formation.
In addition, described reactor block comprises the second reaction substrate bonding cover plate with described cell cube.
In addition, described reactor block is made of the mutual bonding described cell cube of order.
In addition, described reactor block comprises and the bonding cover plate of the second reaction substrate that places described reactor block top.
In addition, described preheating unit comprises: the shell that encapsulates described reactor block; Burner, it places described shell, is used for fired outside and burning first reactant at described reactor block.
In addition, described shell comprises: first, its flare and be positioned at described reactor block one end; Second portion, its flare and be positioned at the described reactor block other end; Third part, the part beyond the two ends of itself and described reactor block is bonding.
In addition, described reactor block comprises passage, this passage constitutes by the adhesive surface that uses described first raceway groove and the second reaction substrate, to allow first reactant to flow through, and described passage comprises a plurality of hand-holes that are formed on described reactor block one end place, and is formed on a plurality of discharge orifices that described reactor block other end place is connected with described hand-hole.
In addition, described preheating unit comprises: the shell that encapsulates described reactor block; And burner unit, it places described shell, is used to light and first reactant that burns, thereby injects flames in the described hand-hole.
In addition, described shell comprises: first, its flare and be positioned at described hand-hole side; Second portion, its flare and be positioned at described discharge orifice side; Third part, the part beyond the two ends of itself and described reactor block is bonding.
In addition, described burner places described first.
In addition, in described shell, in first, be formed with a hand-hole, it is used for first reactant is injected first, be formed with a discharge orifice in second portion, it is used to discharge burning gases that generated by described burner combustion first reactant and the reacting gas that is generated by described layer of oxidation catalyst oxidation first reactant.
In addition, the reaction start-up temperature scope of described layer of oxidation catalyst is from 150 ℃ to 300 ℃.
In addition, by the oxidation reaction of first reactant, the temperature range of the producible heat energy of the described first reaction substrate is from 600 ℃ to 700 ℃.
Description of drawings
Fig. 1 is the perspective view of describing according to the fuel reformer of the first embodiment of the present invention.
Fig. 2 is the cutaway view of fuel reformer shown in Figure 1.
Fig. 3 is the cutaway view of fuel reformer according to a second embodiment of the present invention.
Fig. 4 is a perspective view of describing the fuel reformer of a third embodiment in accordance with the invention.
Fig. 5 is the decomposition diagram of the reactor block of fuel reformer shown in Figure 4.
Fig. 6 is the perspective view that wherein is combined with the structure of reactor block shown in Figure 4.
Fig. 7 is the longitudinal sectional view of reactor block shown in Figure 6.
Fig. 8 is the transverse sectional view of fuel reformer shown in Figure 4.
Embodiment
In the following description, by way of example, show and specific exemplary embodiment of the present invention has been described.What those skilled in the art will recognize that is that described exemplary embodiment can be transformed in every way, but all must not exceed the spirit and scope of the present invention.Therefore, accompanying drawing and explanation should be considered to illustrative in fact, and are not intended to limit.
Fig. 1 is the perspective view of describing according to the fuel reformer of the first embodiment of the present invention.Fig. 2 is the cutaway view of fuel reformer shown in Figure 1.
See figures.1.and.2, fuel reformer 100 has a kind of structure according to an embodiment of the invention, this structure is used to burn such as the gaseous fuel of LPG or LNG or butagas producing heat energy, thereby and uses the heat energy that is produced to make fuel gas generation reforming reaction generate hydrogeneous reformed gas.
In the fuel reformer 100 according to present embodiment, main heat source 10 is used for producing the required heat energy of reforming reaction of reforming reaction unit 30, and the heat energy that produces is offered reforming reaction unit 30.Main heat source 10 produce temperature that heat energy are used for making the reforming reaction in the reforming reaction unit 30 remain on required from about 600 ℃ to about 700 ℃ temperature range.
In main heat source 10, an end of second pipe 52 is furnished with first hand-hole 13, and by first hand-hole 13, gaseous fuel and air are injected in second pipe.
In addition, in main heat source 10, second pipe, 52 the other end is furnished with first discharge orifice 15, and it is used to discharge burning gases, and fuel and the oxidation reaction between the air that described burning gases take place during by combustion air and gaseous fuel generate.
According to present embodiment, auxiliary thermal source 20 is used for when fuel reformer 100 begins to drive, and the oxidation catalyst in the main heat source 10 11 is preheating to reaction start-up temperature scope.
Auxiliary thermal source 20 produces heat energy by lighting with burning gases fuel and air, with the oxidation catalyst in the main heat source 10 11 be preheating to be used to start reaction from about 150 ℃ in about 300 ℃ temperature range.
When fuel reformer 100 begins to drive, because at room temperature the oxidation catalyst 11 in the main heat source 10 can not produce the oxidation reaction between gaseous fuel and the air, oxidation catalyst 11 in the auxiliary thermal source 20 preheating main heat sources 10, so that the oxidation catalyst 11 in main heat source 10 provides heat energy, keep the temperature range that gaseous fuel and air can begin to take place oxidation reaction.
In this embodiment, auxiliary thermal source 20 comprises the igniter 21 that is connected with an end of second pipe 52.The function that igniter 21 has is gaseous fuel and the air of lighting and burning and manage in 52 second.
Igniter 21 comprises and is used for conventional igniter plug (not shown) that gaseous fuel and air are lighted.
In addition, in auxiliary thermal source 20, be formed with second hand-hole 23 that is used for gaseous fuel and air injection second pipe 52 at igniter 21 places.When second pipe in 52 gaseous fuel and air is lighted and when burning, the burning gases that generated emit by first discharge orifice 15 of main heat source mentioned above 10.
In the present embodiment, construct by filling reforming catalyst 31 in the space between first pipe, 51 and second pipe 52 reforming reaction unit 30, and therefore, hydrogeneous reformed gas generates gaseous fuel generation reforming reaction by using reforming catalyst 31.
Here, reforming reaction unit 30 has a kind of structure, this structure such as steam reforming reaction, partial oxidation reaction, automatic thermal response or the fuel of use heat energy and the catalytic reaction of the steam reforming reaction between the water, generates hydrogeneous reformed gas by a kind of from fuel.
In reforming reaction unit 30, in the structure of reforming catalyst 31, be included in by aluminium oxide (Al such as the catalysis material of copper (Cu), nickel (Ni), platinum (Pt)
2O
3), silicon dioxide (SiO
2) or titanium dioxide (TiO
2) in the ball shape carrier made.
In addition, in reforming reaction unit 30, be formed with the 3rd hand-hole 33 at first pipe a, end of 51, it is used for gaseous fuel and water are injected into space between first pipe, 51 and second pipe 52.
In addition, in reforming reaction unit 30, the other end of first pipe 51 is formed with second discharge orifice 35, it is used to discharge the reformed gas of generation, reforming reaction takes place by using reforming catalyst 31 to make between gaseous fuel and the water vapour in described reformed gas, generates in the space between first pipe, 51 and second pipe 52.
At this moment, second discharge orifice 35 can be connected with the heap (not shown) of formation polymer dielectric film fuel cell mentioned above by conventional pipeline.
In the present embodiment, reforming reaction takes place by using reforming catalyst 31 to make between gaseous fuel and the water vapour in reforming reaction unit 30, generated hydrogeneous reformed gas, but the present invention is not limited to this.Reforming reaction unit 30 can be by generating reformed gas such as the liquid fuel of methyl alcohol and ethanol and the reforming reaction between the water vapour.
Now, the driving method of fuel reformer 100 according to an embodiment of the invention will be described in detail.
At first, when fuel reformer 100 began to be driven, in other words gaseous fuel and air were igniters 21 by auxiliary thermal source unit 20, second hand-hole 23 be provided in second pipe 52.
In this case, the igniter plug (not shown) of igniter 21 is lighted air and is injected into second gaseous fuel of managing in 52.Like this, auxiliary thermal source produces predetermined heat energy, and heat energy is offered the oxidation catalyst 11 of main heat source 10.Therefore, the oxidation catalyst 11 of main heat source 10 be preheating to from about 150 ℃ in about 300 ℃ reaction start-up temperature scope.
Then, when fuel reformer 100 by driven, second hand-hole 23 by igniter 21 provides the supply of gaseous fuel and air to be stopped by the operation of a conventional valve (not shown) to second pipe 52.
When fuel reformer 100 by driven, gaseous fuel and air are fed in second pipe by first hand-hole of main heat source 10.Then, main heat source 10 makes between gaseous fuel and the air by the oxidation catalyst 11 that uses preheating oxidation reaction takes place, produce heat energy in case keep reforming reaction in the reforming reaction unit 30 required from about 600 ℃ to about 700 ℃ predetermined temperature range.Therefore, the heat energy that keeps aforesaid temperature range offers the reforming catalyst 31 of reforming reaction unit 30 by second pipe 52.
After having passed through above-mentioned flow process, gaseous fuel and water are provided in the space between first pipe, 51 and second pipe 52 by the 3rd hand-hole 33 of reforming reaction unit 30.Then, reforming reaction unit 30 absorbs the heat energy that is produced by main heat source 10, at the steam reforming reaction that produces under the effect of reforming catalyst 31 between gaseous fuel and the water, and then generates hydrogeneous reformed gas.
Therefore, reformed gas is discharged and offers heap from second discharge orifice 35 of reforming reaction unit 30, thereby the predetermined electric energy of output so react in heap, the reduction reaction of oxidation reaction that is included in the hydrogen in the reformed gas and the air that separately provides is provided in described reaction.
Fig. 3 is the cutaway view of fuel reformer according to a second embodiment of the present invention.
With reference to Fig. 3, comprise further that according to the fuel reformer 200 of present embodiment carbon monoxide reduces unit 550, it is used for reducing the concentration of the contained carbon monoxide of the reformed gas that generated by reforming reaction unit 130.
Similar to aforesaid embodiment, fuel reformer 200 comprises main heat source 110 and auxiliary thermal source 120, and main heat source is identical with auxiliary thermal source in the structure that has of main heat source 110 and auxiliary thermal source 120 and the previous embodiment, therefore omits concrete description.
In the present embodiment, when the space between first pipe, 151 and second pipe 152 was divided into first area A and second area B, constructed by fill reforming catalyst 131 in the A of first area reforming reaction unit 130.
First area A and second area B are by netted dividing plate 180 separately.Dividing plate 180 and comprises that a plurality of holes 181, the second pipes, 152 middle bodies from dividing plate 180 pass ringwise.Dividing plate 180 is except having following function, promptly, space between first pipe, 151 and second pipe 152 is divided into first area A and second area B, also has following function, that is, the reformed gas that allows reforming reaction unit 130 to generate flow in the carbon monoxide minimizing unit 170 that will will describe hereinafter through aforesaid hole 181.
In addition, in the reforming reaction unit 130 according to present embodiment, an end of first pipe 151 is formed with hand-hole 113, and it is used for gaseous fuel and air are injected first area A.
In the present embodiment, construct by filling water gas converting catalyst 171 among the second area B between first pipe, 151 and second pipe 152 carbon monoxide minimizing unit 170.
Water gas converting catalyst 171 accelerated packet are contained in the water gas shift reaction of the carbon monoxide in the reformed gas, to reduce the concentration of carbon monoxide, in the structure of water gas converting catalyst 171, will be included in by aluminium oxide (Al such as the catalysis material of copper (Cu), zinc (Zn), iron (Fe) and chromium (Cr)
2O
3), silicon dioxide (SiO
2) or titanium dioxide (TiO
2) in the ball shape carrier that forms.
Reduce in the unit 170 at carbon monoxide, the other end of first pipe 151 is formed with discharge orifice 173, and its reformed gas that is used for carbonomonoxide concentration has been lowered emits from second area B.Discharge orifice 173 can be connected to heap (not shown) with aforesaid formation polymer dielectric film fuel cell by conventional pipeline.
In driving the method for fuel reformer 200 according to an embodiment of the invention, similar to aforesaid embodiment, reforming reaction unit 130 generates reformed gas, at this moment, the reformed gas that generates offers carbon monoxide through the hole 181 on the dividing plate 180 and reduces unit 170, just the second area B between first pipe, 151 and second pipe 152.
Therefore, reduce in the unit 170 at carbon monoxide, the extra hydrogen of carbon monoxide generation water gas shift reaction generation that is included in the reformed gas by using water gas converting catalyst 171 to make, the concentration of carbon monoxide reduces simultaneously.The reformed gas that has reduced the concentration of carbon monoxide emits by the discharge orifice 173 that carbon monoxide reduces unit 170, and offers heap.
Because identical with appropriate section, so specific descriptions have wherein been omitted with operation according to the fuel reformer 100 of aforesaid first embodiment according to the other parts of the fuel reformer 200 of present embodiment and operation.
Fig. 4 is a perspective view of describing the fuel reformer of a third embodiment in accordance with the invention.
With reference to Fig. 4, fuel reformer 300 produces the heat energy with predetermined temperature range by the oxidation reaction between gaseous fuel and the air (hereinafter being called " first reactant ").Fuel reformer 300 comprises reactor block 310, and reacting has generated reformed gas by using the heat energy that is produced to make gaseous fuel and water (hereinafter being called " second reactant ") in reactor block 310.
Fig. 5 is the decomposition diagram of the reactor block 310 of fuel reformer shown in Figure 4.Fig. 6 is in conjunction with the perspective view that wherein has the structure of reactor block shown in Figure 4.Fig. 7 is the longitudinal sectional view of reactor block shown in Figure 4.
With reference to Fig. 5 to 7, comprise according to the reactor block 310 of the 3rd embodiment: the first reaction substrate 311, it provides the first raceway groove 311a to be used to allow first reactant to flow in its surface; With the second reaction substrate 312, it provides the second raceway groove 312a to be used to allow second reactant to flow in its surface.
Here, the first reaction substrate 311 and the second reaction substrate 312 are the rectangular slab with preset width and length, and are made by the metal with thermal conductivity, are for example made by aluminium, stainless steel, copper, nickel and iron.
The first reaction substrate 311 be used to oxidation reaction by first reactant produce heat energy with keep from about 600 ℃ to about 700 ℃ predetermined temperature range (temperature range that the reforming reaction of reactant is required), and the heat energy that produces offered the second reaction substrate 312.
The first reaction substrate 311 comprises a plurality of first raceway groove 311a on its upper surface.The first raceway groove 311a can form by using from the outstanding a plurality of ribs of the first reaction substrate, 311 upper surfaces.
Like this, the first raceway groove 311a is a flute profile, and is connected to the other end from an end of the first reaction substrate 311.So, on the surface of the first raceway groove 311a, forming conventional layer of oxidation catalyst 311b, it is used to quicken the oxidation reaction of first reactant.
The second reaction substrate 312 is used to receive the heat energy from the first reaction substrate 311, and uses the heat energy that is produced to make the second reactant generation reforming reaction generate hydrogeneous reformed gas.
The second reaction substrate 312 sticks on the first reaction substrate 311, has the second raceway groove 312a on the upper surface of the second reaction substrate 312.The second raceway groove 312a can form by using from the outstanding a plurality of ribs of the second reaction substrate, 312 upper surfaces.
The second raceway groove 312a is a flute profile, and is connected with a pair of manifold 312c on being positioned at diagonal.
So, on the surface of the second raceway groove 312a, being formed with conventional reforming catalyst layer 312b, it is used to quicken the reforming reaction of second reactant.
In the 3rd embodiment,, formed cell cube 319 by second lower surface that reacts substrate 312 being adhered to the upper surface of the first reaction substrate 311.By with cell cube 319 order bonding reactor blocks 310 that form mutually.Then, cover plate 318 is adhered to the upper surface of the second reaction substrate 312 that is positioned at reactor block 310 tops.
Alternatively, reactor block 310 can comprise single cell cube 319.Like this, cover plate 318 is adhered on the upper surface of the second reaction substrate 312, just on the upper surface of cell cube 319.
Here, the first reaction substrate 311 and second reaction substrate 312 and the cover plate 318 are by such as the conventional link of screw and nut or by carry out each other bonding such as the conventional method of attachment of welding and brazing.
Therefore, in reactor block 310, the first reaction substrate 311 and the second reaction substrate, the 312 mutual bonding first passages 313 that formed, this passage is configured for allowing first reagent flow by the first raceway groove 311a of the first reaction substrate 311 and the adhesive surface of the second reaction substrate 312.
Like this, because the first raceway groove 311a is connected to the other end from first end that reacts substrate 311, first passage 313 comprises a plurality of hand-hole 313a, that is, be positioned at opening and a plurality of discharge orifice 313b (with reference to Fig. 8) of an end of reactor block 310, that is, be positioned at the opening of the other end of reactor block 310.
In addition, in reactor block 310, the lower surface of the first reaction substrate 311 is adhered to the upper surface of the second reaction substrate 312, and cover plate 318 is adhered to the upper surface of the second reaction substrate that is positioned at reactor block 310 tops, to form second channel 315, this passage is made of the adhesive surface of the second raceway groove 312a and cover plate 318, to allow second reagent flow.
When the fuel reformer 300 with said structure begins to drive, because layer of oxidation catalyst 311b oxidation at room temperature first reactant of the first reaction substrate 311, layer of oxidation catalyst 311b need be preheating in the temperature range that first reactant can begin oxidation reaction.
As shown in Figure 4, fuel reformer 300 comprises preheating unit 350, and it is used for by lighting and first reactant that burns comes preheat reactor body 310.
Fig. 8 is the transverse sectional view of Fig. 4.With reference to Fig. 8, when fuel reformer 300 begins to drive, preheating unit 350 is lighted and first reactant that burns, and the heat energy that first reactant that will burn produces offers the first reaction substrate 311, so with the layer of oxidation catalyst 311b of the first reaction substrate 311 be preheating to start reaction from about 150 ℃ in about 300 ℃ temperature range.
Particularly, preheating unit 350 comprises the shell 351 that is used for encapsulated reaction heap body 310 and burner 357, and wherein burner 357 is arranged in shell 351, and is used at reactor block 310 fired outside and burning first reactant.
In the present embodiment, shell 351 is used for encapsulated reaction heap body 310, and this shell made by the heat-insulating material of routine, discharges from shell 351 to prevent heat energy.
In shell 351, be formed with the trumpet-shaped 351a of first at reactor 310 1 ends, be formed with trumpet-shaped second portion 315b at the other end of reactor block 310, third part 351c is adhered to the place of reactor block 310 except that two ends.
Because the side of 351a of first and third part 351c combines, the cross section of the profile of the 351a of first begins to reduce from the side of third part 351c, like this, predetermined inner space is formed at an end of reactor block 310, is formed with the hand-hole 313a of first passage 313 herein.
Then, because the other end of third part 351c is formed with second portion 351b, the cross section of the profile of second portion 351b begins to reduce from the opposite side of third part 351c, like this, predetermined inner space is formed at the other end of reactor block 310, is formed with the discharge orifice 313b of first passage 313 herein.
The 351a of first has horn-like profile, so that first hand-hole 353 of first reactant by hereinafter describing, the direction that increases along first 351a cross section spreads, and be injected into the inner space of the 351a of first, and first reactant is injected among the hand-hole 313a of first passage 313.
In addition, second portion has horn-like profile, so that, by burning gases and the reacting gas of collecting first reactant, through first discharge orifice 355 that will further introduce hereinafter, easily discharge the burning gases and the reacting gas of first reactant, wherein, by using burner 357 burnings first reactant that hereinafter will describe to generate the burning gases of first reactant, hand-hole 313a by first passage 313 is injected into burning gases in the first passage 313, and by the discharge orifice 313b of first passage 313 burning gases is emitted; Wherein the reacting gas of first reactant passes through the hand-hole 313a of first passage 313 and is injected in the first passage 313, and oxidized catalyst layer 311b oxidation, and the discharge orifice 313b by first passage 313 emits reacting gas again.
In aforesaid shell 351, be formed with first hand-hole 353 among the 351a of first, it is used for first reactant is injected into the inner space of the 351a of first.
Then, form first hand-hole 353 at the place, tip of the 351a of first.In addition, be formed with first discharge orifice 355 among the second portion 351b, it is used to discharge burning gases that generated by burner 357 burnings first reactant and the reacting gas that is generated by first layer of oxidation catalyst 311b oxidation first reactant that reacts substrate 311.First discharge orifice 355 is formed in the tip of second portion 351b.
As previously mentioned, burner 375 comprises igniter 358, and igniter 358 places the 351a of first, and is connected with first hand-hole 353, is used for lighting and burns being injected into first reactant of the inner space of first 351 by first hand-hole 353.
Igniter 358 has the igniter plug (not shown) that is used to light first reactant, and this igniter plug is a conventional igniter plug, and it controls generation flame by the additional controller (not shown).
In Fig. 8, point to not clear reference number 59a and represent second hand-hole, it is used for second reactant is injected into the second channel 315 of reactor block 310, point to not clear reference number 59b and represent second discharge orifice, it is used to discharge reformed gas, and wherein said reformed gas uses reforming catalyst layer 312b that reforming reaction takes place when second reactant process second channel 315 and generates.
Like this, the aforesaid second hand-hole 359a and the second discharge orifice 359b are connected with the manifold 312c of as shown in Figure 2 the second reaction substrate 312.
Hereinafter will describe the method that a kind of driving has the fuel reformer 300 of aforementioned structure in detail.
When fuel reformer 300 began to be driven, first reactant was injected into the inner space of the 351a of first by first hand-hole 353 of shell 351.
The igniter plug (not shown) of igniter 358 produces flame to light first reactant in the inner space that is injected into the 351a of first.Then, first reactant burns in the inner space of the 351a of first, to produce predetermined heat energy.
Therefore, the high-temperature combustion gas that produces by first reactant that burns injects first passage 313 through the hand-hole 313a of first passage 313, flow along first passage 313, and emit, thereby heat energy is offered the layer of oxidation catalyst 311b of the first reaction substrate 311 through the discharge orifice 313b of first passage 313.
First the reaction substrate 311 layer of oxidation catalyst 311b be preheating to from about 150 ℃ in about 300 ℃ reaction start-up temperature scope, the oxidation reaction of first reactant can begin in this temperature range.
Then, the burning gases of the discharge orifice 313b discharging by first passage 313 are collected in the inner space of second portion 351b, and discharge shells 351 by first discharge orifice 355.
Subsequently, when fuel reformer 300 during by driven, because first reactant is provided in the inner space of the 351a of first by first hand-hole 353 by shell 351 continuously, igniter plug is not being controlled by controller and is being started.
When fuel reformer 300 during by driven, first reactant is injected in the first passage 313 from the inner space of the 351a of first by the hand-hole 313a of first passage 313.Then, in the first reaction substrate 311, the oxidized catalyst layer 311b of first reactant oxidation of flowing along first passage 313, thus produce heat energy with the reforming reaction that keeps second reactant required from about 600 ℃ to about 700 ℃ predetermined temperature range.
At this moment, because the first reaction substrate 311 and the second reaction substrate 312 are bonding, heat energy is sent to the second reaction substrate 312 by the first reaction substrate 311, and then heat energy is provided for the reforming catalyst layer 312b of the second reaction substrate 312.
The reacting gas of first reactant of oxidized catalyst layer 311b oxidation is collected in the inner space of second portion 351b through the discharge orifice 313b of first passage 313 discharging, and discharges shell 351 by first discharge orifice 355.
After having passed through aforesaid flow process, second reactant is supplied with to the second channel 315 of reactor block 310 through the second hand-hole 359a.Then, when the second reaction substrate 312 is absorbed in the heat energy that produces in the first reaction substrate 311, thereby use reforming catalyst layer 312b to make the second reactant generation reforming reaction generate hydrogeneous reformed gas.
Therefore, because reformed gas is discharged in the heap by the second discharge orifice 359b, the oxidation reaction of hydrogen contained in reformed gas and the reduction reaction of separating the air of supplying with have taken place in heap, thus the predetermined electric energy of output.
As mentioned above, according to embodiments of the invention, because fuel reformer comprises auxiliary thermal source, this auxiliary thermal source comes the preheating oxidation catalyst by lighting with combustion fuel when fuel reformer begins to be driven, during by driven, fuel reformer can use oxidation catalyst to make fuel generation oxidation reaction produce heat energy at fuel reformer.
Therefore, since when fuel reformer begins to be driven by having lighted with the combustion fuel preheating oxidation catalyst, the beginning driving time of fuel reformer has reduced, the energy efficiency of fuel reformer is improved, the fireproof durability of auxiliary thermal source is improved, and then obtains the useful life of fuel reformer prolonging.
Though practical, exemplary embodiment that related content described in the invention is considered at present, but will be appreciated that, the present invention is not limited to disclosed embodiment, on the contrary, the present invention is intended to contain various transformations and the equivalence arrangement in the spirit and scope that are included in subsidiary claims.
Claims (22)
1, a kind of fuel reformer, it comprises:
First pipe;
Place second pipe of described first pipe;
Main heat source, it comprises the oxidation catalyst that is filled in described second pipe, thus described main heat source uses described oxidation catalyst to make fuel generation oxidation reaction be suitable for producing the heat energy with predetermined temperature range;
Auxiliary thermal source, it comprises igniter, and described igniter is connected to described second pipe, thereby lights and combustion of gaseous fuel, and then described oxidation catalyst is preheating among the reaction start-up temperature scope;
The reforming reaction unit, it comprises reforming catalyst, described reforming catalyst be filled in described second the pipe and described first pipe between the space in, the described heat energy that described reforming reaction unit uses described reforming catalyst and uses described main heat source to produce, make described fuel generation reforming reaction, thereby be suitable for generating hydrogeneous reformed gas.
2, fuel reformer as claimed in claim 1, comprise that further carbon monoxide reduces the unit, it is constructed by the concentration that filling water gas converting catalyst in the space between described first pipe and described second pipe reduces contained carbon monoxide in the described reformed gas.
3, fuel reformer as claimed in claim 2, further comprise the dividing plate that places between described first pipe and described second pipe, described dividing plate is divided into a zone and a zone that is filled with described water gas converting catalyst that is filled with described reforming catalyst with the space between described first pipe and described second pipe.
4, fuel reformer as claimed in claim 3, wherein said dividing plate has netted profile.
5, fuel reformer as claimed in claim 1, the described reaction start-up temperature scope of wherein said oxidation catalyst is from 150 ℃ to 300 ℃.
6, fuel reformer as claimed in claim 5, wherein the temperature range that heat energy had that is produced by described main heat source is from 600 ℃ to 700 ℃.
7, a kind of fuel reformer comprises:
Reactor block, it comprises a plurality of reaction substrates, the oxidation reaction of first reactant of wherein said reaction substrate by including fuel produces heat energy, and the reforming reaction of second reactant by including described fuel produces reformed gas; With
Preheating unit, it places described reactor block, be used to light and described first reactant that burns so that the described reactor block of preheating.
8, fuel reformer as claimed in claim 7, wherein said preheating unit comprises:
Encapsulate the shell of described reactor block;
Burner, it places described shell, is used for fired outside and described first reactant of burning at described reactor block.
9, a kind of fuel reformer comprises:
One or more first reaction substrate, it comprises first raceway groove that is used to allow include first reagent flow of fuel, and in the described first reaction substrate, is formed with layer of oxidation catalyst on the surface of described first raceway groove;
One or more second reaction substrate, it comprises second raceway groove that is used to allow include second reagent flow of described fuel, and in the described second reaction substrate, is formed with reforming catalyst layer on the surface of described second raceway groove;
Reactor block by bonding described first reaction substrate and the described second reaction substrate formation;
Preheating unit, it places described reactor block, is used to light and described first reactant that burns, so that described layer of oxidation catalyst is preheating to a reaction start-up temperature scope.
10, fuel reformer as claimed in claim 9, wherein said reactor block comprises one or more cell cube, it is by reacting the described first reaction substrate and described second to the bonding formation of substrate.
11, fuel reformer as claimed in claim 10, wherein said reactor block comprises cover plate, the described second reaction substrate of itself and described cell cube is bonding.
12, fuel reformer as claimed in claim 10, wherein said reactor block is made of the mutual bonding described cell cube of order.
13, fuel reformer as claimed in claim 12, wherein said reactor block comprises cover plate, it is adhered to the described second reaction substrate that places described reactor block top.
14, fuel reformer as claimed in claim 9, wherein said preheating unit comprises:
Encapsulate the shell of described reactor block; With
Burner, it places described shell, is used for fired outside and burning first reactant at described reactor block.
15, fuel reformer as claimed in claim 14, wherein said shell comprises:
First, its flare and be positioned at described reactor block one end;
Second portion, its flare and be positioned at the described reactor block other end;
Third part, the part beyond described two ends of itself and described reactor block is bonding.
16, fuel reformer as claimed in claim 9, wherein said reactor block comprises passage, described passage constitutes by the described bonded surface of described first raceway groove and the described second reaction substrate, flows through to allow described first reactant;
Wherein said passage comprises: a plurality of hand-holes, described hand-hole are formed in the opening at described reactor block one end place; With a plurality of discharge orifices, the opening that described discharge orifice is formed in described reactor block other end place and is connected with described hand-hole.
17, fuel reformer as claimed in claim 16, wherein said preheating unit comprises:
Encapsulate the shell of described reactor block; With
Burner, it places described shell, is used to light and described first reactant that burns, and injects flames in the described hand-hole.
18, fuel reformer as claimed in claim 17, wherein said shell comprises:
First, its flare and be positioned at described hand-hole side;
Second portion, its flare and be positioned at described discharge orifice side;
Third part, the part beyond described two ends of itself and described reactor block is bonding.
19, fuel reformer as claimed in claim 15, wherein said burner places described first.
20, fuel reformer as claimed in claim 15, wherein in described shell, in described first, be formed with a hand-hole, it is used for described first reactant is injected described first, be formed with a discharge orifice in described second portion, it is used to discharge burning gases that generated by described first reactant of described burner combustion and the reacting gas that is generated by described first reactant of described layer of oxidation catalyst oxidation.
21, fuel reformer as claimed in claim 9, the reaction start-up temperature scope of wherein said layer of oxidation catalyst is from 150 ℃ to 300 ℃.
22, fuel reformer as claimed in claim 9, the oxidation reaction generation temperature range of the wherein said first reaction substrate by described first reactant is from 600 ℃ to 700 ℃ heat energy.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1020050089814 | 2005-09-27 | ||
| KR1020050089814A KR100684771B1 (en) | 2005-09-27 | 2005-09-27 | Apparatus for reforming fuel and driving method of the same |
| KR1020060010566 | 2006-02-03 |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101673840A Division CN101436671B (en) | 2005-09-27 | 2006-09-27 | Fuel reformer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1941483A true CN1941483A (en) | 2007-04-04 |
| CN100490239C CN100490239C (en) | 2009-05-20 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101673840A Expired - Fee Related CN101436671B (en) | 2005-09-27 | 2006-09-27 | Fuel reformer |
| CNB2006101278931A Expired - Fee Related CN100490239C (en) | 2005-09-27 | 2006-09-27 | Fuel reformer |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101673840A Expired - Fee Related CN101436671B (en) | 2005-09-27 | 2006-09-27 | Fuel reformer |
Country Status (2)
| Country | Link |
|---|---|
| KR (1) | KR100684771B1 (en) |
| CN (2) | CN101436671B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7985506B2 (en) | 2007-12-27 | 2011-07-26 | Samsung Sdi Co., Ltd. | Fuel cell system and reformer |
| CN101900329B (en) * | 2009-05-28 | 2012-07-18 | 三星Sdi株式会社 | Catalytic combustor and fuel reformer having the same |
| CN103956508A (en) * | 2014-05-19 | 2014-07-30 | 哈尔滨工业大学 | Miniature methanol and steam reforming chamber |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101237778B1 (en) * | 2010-04-29 | 2013-02-28 | 에스티엑스중공업 주식회사 | Reformer having spiral reactor |
| KR101216456B1 (en) * | 2010-04-29 | 2012-12-28 | 에스티엑스중공업 주식회사 | Reformer |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0648701A (en) * | 1992-07-24 | 1994-02-22 | Mitsubishi Heavy Ind Ltd | Steam-reforming reactor |
| DE59610198D1 (en) * | 1996-06-19 | 2003-04-10 | Sulzer Hexis Ag | Method for operating a device with fuel cells |
| JP3921477B2 (en) | 1999-04-20 | 2007-05-30 | 東京瓦斯株式会社 | Single tube cylindrical reformer and its operating method |
| JP2002208426A (en) * | 2001-01-11 | 2002-07-26 | Tokyo Gas Co Ltd | Reforming device for fuel cell |
| JP4045755B2 (en) * | 2001-05-23 | 2008-02-13 | 日産自動車株式会社 | Fuel cell system |
| JP2003095610A (en) | 2001-09-20 | 2003-04-03 | Mitsubishi Heavy Ind Ltd | Method for producing hydrogen |
| KR100570752B1 (en) | 2004-02-26 | 2006-04-12 | 삼성에스디아이 주식회사 | Reformer for fuel cell system and fuel cell system having thereof |
-
2005
- 2005-09-27 KR KR1020050089814A patent/KR100684771B1/en not_active IP Right Cessation
-
2006
- 2006-09-27 CN CN2008101673840A patent/CN101436671B/en not_active Expired - Fee Related
- 2006-09-27 CN CNB2006101278931A patent/CN100490239C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7985506B2 (en) | 2007-12-27 | 2011-07-26 | Samsung Sdi Co., Ltd. | Fuel cell system and reformer |
| CN101471449B (en) * | 2007-12-27 | 2011-11-09 | 三星Sdi株式会社 | Fuel cell system and reformer |
| CN101900329B (en) * | 2009-05-28 | 2012-07-18 | 三星Sdi株式会社 | Catalytic combustor and fuel reformer having the same |
| US8617269B2 (en) | 2009-05-28 | 2013-12-31 | Samsung Sdi Co., Ltd. | Catalytic combustor and fuel reformer having the same |
| CN103956508A (en) * | 2014-05-19 | 2014-07-30 | 哈尔滨工业大学 | Miniature methanol and steam reforming chamber |
Also Published As
| Publication number | Publication date |
|---|---|
| KR100684771B1 (en) | 2007-02-20 |
| CN101436671B (en) | 2011-08-17 |
| CN101436671A (en) | 2009-05-20 |
| CN100490239C (en) | 2009-05-20 |
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