CN105293435A - Method for converting hydrocarbon fuel into hydrogen-rich gas - Google Patents
Method for converting hydrocarbon fuel into hydrogen-rich gas Download PDFInfo
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- CN105293435A CN105293435A CN201510726740.8A CN201510726740A CN105293435A CN 105293435 A CN105293435 A CN 105293435A CN 201510726740 A CN201510726740 A CN 201510726740A CN 105293435 A CN105293435 A CN 105293435A
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- fuel
- hydrocarbon fuel
- preheating
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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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Abstract
The invention relates to a method for converting hydrocarbon fuel into a hydrogen-rich gas which is applied to a fuel cell and/or exhaust treatment through autothermal reaction. A reform reactor (1) is utilized by the method; the reform reactor (1) comprises a shell (2), a fuel inlet (22) and an oxidant inlet (18), wherein the shell (2) comprises two side surfaces (8a and 8b); the two side surfaces (8a and 8b) form a reaction chamber (10) of the reform reactor (1); the fuel inlet (22) is formed in one side surface (8a) of the two side surfaces to provide the hydrocarbon fuel to the reaction chamber (10); the oxidant inlet (18) is used for providing an oxidant to the reaction chamber (10); and the method comprises the following steps: preheating the oxidant to the temperature which is basically equal to or higher than the boiling pint of the hydrocarbon fuel; and preheating the hydrocarbon fuel to the temperature which is a little lower than the boiling point of the hydrocarbon fuel; and introducing the hydrocarbon fuel and the oxidant into the reaction chamber (10).
Description
divisional application
The divisional application of the application's to be application number be Chinese patent application of 200880130143.7, the applying date of above-mentioned application is on July 2nd, 2008, and denomination of invention is " reforming reactor and the method that hydrocarbon fuel are converted into hydrogen-rich gas ".
Technical field
The present invention relates to a kind of reforming reactor and use this reforming reactor hydrocarbon fuel to be converted into the method for hydrogen-rich gas, hydrocarbon fuel is converted into the hydrogen-rich gas applied for fuel cell and/or emission treatment by this reforming reactor by autothermal reaction.
Background technology
In the prior art, known by the hydrogen-rich gas produced for the fuel cell in conveyer of reforming to the hydrocarbon fuel of such as gasoline or diesel oil fuel.Traditionally, hydrogen produces in large industry equipment, is then stored on conveyer.The small size hydrogen source (so-called reforming reactor) of recent exploitation provides and produces hydrogen and possibility without the need to storing hydrogen as required.
Usually, there are three kinds of known methods that gaseous state or liquid hydrocarbon fuel are restructured as hydrogen: catalytic steam reforming, partial oxidative steam reforming and self-heating recapitalization.
In catalytic steam reforming process, the mixture of steam and hydrocarbon fuel at high temperature (between 700 DEG C to 1000 DEG C) is exposed to suitable catalyzer, such as nickel.This reaction is highly absorbed heat, and need external heat source and vapour source.
In partial oxidative steam reforming process, hydrogen fuel and oxygen-containing gas (as ambient air) are sent in reaction chamber by as unstripped gas, preferably have catalyzer.The catalyzer used is made up of precious metal or nickel usually, and temperature is between 700 DEG C to 1700 DEG C.This reaction is high exothermic heat, and just produces enough heats with self―sustaining once startup.In order to accelerating oxidation reaction, be necessary to reduce the temperature variation in reactor.
Self-heating recapitalization process is the combination of steam reformation and partial oxidative steam reforming.Used heat from partial oxidative steam reforming reaction is used to heat the steam reforming reaction of heat absorption.
The natural by product of all these reforming processes is carbon monoxide and carbonic acid gas.But, owing to hydrocarbon fuel not being designed the raw material as producing hydrogen, therefore also there is other by product, as sulphur.These by products may be harmful to fuel cell, therefore, should be removed in reforming reactor outside by subsequent step.In addition, if undercompounding in the reactor, then hydrocarbon fuel (especially diesel oil) can produce the cigarette ash as by product in the catalyst.Equally, soot particulates is very harmful to fuel cell, therefore must be noted that to avoid forming cigarette ash in reformer.
From the patent application US6 of prior art, 770, in 106, known a kind of partial oxidation reformer for reforming to the unstripped gas containing hydrocarbon or methane, oxygen G&W, wherein, achieved the minimizing of temperature variation by the reactor covered by the passage of unstripped gas, this unstripped gas is heated by the reaction heat in reactor, therefore this reactor of thermal isolation.Therefore, it is possible to reduce the temperature variation in this reactor.In order to heating raw gas, reaction heat can be reclaimed by heat exchanger.
In addition, have been found that: unstripped gas effectively transforms to the success of hydrogen the successful mixing depending on reactant (i.e. hydrocarbon fuel and oxygenant).The shortcoming of known prior art is: due to reactant mixing other, be arranged in outside mixing tank and carry out, so under the uncondensable situation of fuel in the reaction chamber of reformer can not be provided in, the atomization completely of hydrocarbon fuel and oxygenant or vaporization.
In order to solve this problem, such as, propose by fuel and oxygenant mixing in reformer in the prior art, preferably, even by the input air stream of preheating and this fuel mix or by the reformer surperficial carburretion that make injection of preheating for receiving fuel spray.Method due to prior art all can not completely successfully provide injected hydrocarbon fuel reliable, vaporize completely, so proposed in European patent application EP 1927579, hardware is set in the reaction chamber of reactor, thinks that carburretion provides high temperature and large surface-area.
This known fuel evaporator can be such as conductive metallic material, and it sprays to have the foam of fuel or the form of gauze/woven fibrous, or or even the form of cartridge by diffusion of volatile treating agent of longitudinally arranging along the inwall of reactor.
The defect of this known reformer is: necessary well-chosen is for the formation of the material of vaporizer.On the one hand, it must possess the ohmic resistance of appropriateness, and to make this vaporizer be rapidly heated to preferred temperature, but then, it must be chemically inert to the running environment of reactor again.So not overcritical to the material requirements of cylindricality vaporizer, but the defect of this vaporizer is: along with vaporizer be exposed to completely also as refrigerant, input air and fuel air mixture time, thermal load can increase.
Summary of the invention
Therefore, the object of this invention is to provide a kind of reforming reactor and the method that hydrocarbon fuel are converted into hydrogen-rich gas, which provide easy and irrelevant with the material atomization of hydrocarbon fuel to oxygenant.
According to an aspect of the present invention, provide a kind of method by autothermal reaction, hydrocarbon fuel being converted into the hydrogen-rich gas applied for fuel cell and/or exhaust-gas disposal, the method uses following reforming reactor, this reforming reactor has: housing, this housing has two side surfaces, and these two side surfaces form the reaction chamber of reforming reactor; Fuel inlet, this fuel inlet is arranged in a side surface in described two side surfaces, to be provided in reaction chamber by hydrocarbon fuel; And oxidant inlet, this oxidant inlet is used for oxygenant to be provided in reaction chamber, and described method comprises the steps: oxidizer preheat to temperature that is substantially equal with the boiling point of hydrocarbon fuel or that be above the boiling point; Hydrocarbon fuel is preheating to the temperature more lower slightly than the boiling point of hydrocarbon fuel; And hydrocarbon fuel and oxygenant are incorporated in reaction chamber.
According to the present invention, by introduce and make hydrocarbon fuel to mix with oxygenant before by hydrocarbon fuel preheating, substantially desirable spraying of ruel and gaseous mixture subsequently can be obtained.Such preheating can be realized by the primary heater unit of the reaction chamber outside being arranged in reformer.Preferably, this primary heater unit is arranged in fuel inlet upstream, independent device, but also can by integrated to fuel inlet and primary heater unit become single assembly.Especially, in the preferred case, when fuel injector is used as fuel inlet, advantageously heats this injector, carry out pre-heating fuel thus.Therefore, if the sidewall of fuel inlet and reaction chamber is in thermal conductive contact, then more excellent, thus the heat produced in this reaction chamber can pass to injector, with pre-heating fuel.
In a more preferred embodiment, the temperature being preheated fuel be adjusted to close to but lower than the minimum boiling point of fuel, thus provide the substantially desirable atomization of realization or the preferred heat needed for vaporization.
According to further advantageous embodiment, oxygenant was also first preheated before mixing with hydrocarbon fuel, was preferably preheating to the temperature or the higher temperature that are in same range with the temperature of pre-heating fuel.This prevents the unwanted condensation of fuel or oxygenant substantially, and this condensation can cause the lost of life of reformer.
Preferably, the preheating of oxygenant can perform by using the reforming reactor with inner and outer wall, space is formed between this inner and outer wall, wherein, described space is designed to oxidant channel, and this oxidant channel is located between the oxygenant supplying opening arranged in outer wall and the oxidant inlet arranged in inwall.Inwall is heated by the heat of the reaction occurred in reaction chamber, and thus, by from inwall to the heat trnasfer of oxygenant, oxygenant is again by inwall preheating.
Atomized fuel mixes with oxygenant and the combination of preheating of fuel obtains basic completely uniform reaction mixture, and the preheating of oxygenant prevents condensation.The basic uniform mixture realized thus allows transforming substantially completely of hydrocarbon fuel, and this allows again to produce fuel cell level hydrogen from heavy hydrocarbon fuel-efficient.
: inwall is also cooled to following temperature by heat trnasfer substantially prevent the cigarette ash formed owing to burning with the fuel pellet of contact internal walls at such a temperature to the useful subsidiary effect that oxygenant carries out preheating above by from reformer inwall to the heat trnasfer of oxygenant.
Generally speaking, the reactor with exterior cooling device can be provided, but which increase the size of this reactor, and for being provided the system of energy to add another energy-dissipating device by fuel cell.Therefore, preferred embodiment utilizes relatively cold oxygenant to carry out the inwall of cooling reactor.Meanwhile, this means to consider the heat insulation of inwall, make the size of reactor reduce further thus.
Another advantage cooling this inwall is: the temperature in reaction chamber can keep constant, and can the temperature of controlled oxidization agent.
As shown in another preferred embodiment of the present invention, the oxidant inlet be arranged in inner walls is formed as multiple aperture, especially multiple hole or slit.This is convenient to oxygenant and distributes roughly equably in reaction chamber.Preferably, the size in described multiple aperture, shape and/or position can change according to used oxygenant, the hydrocarbon fuel used and/or their temperature.Most preferably, this oxidant inlet is arranged near fuel inlet.
Another preferred embodiment is provided with the catalyzer for autothermal reaction in reaction chamber, to accelerate the conversion of hydrocarbon fuel to hydrogen-rich gas.Because pre-mixing carries out in creative mode, therefore, it is possible to be placed to and catalyst exposure by basic completely uniform mixture, and substantially prevent the inactivation that condensation also just substantially prevent catalyzer, extend the life-span of reformer thus.Preferably, this catalyzer can be ceramic monoliths or metal grating.
Preferably, the size in described aperture and the distance between these aperture and fuel inlet are designed, to realize best turbulent mixing, and make oxidant/fuel mixture be basic completely uniform before contacting the catalyst.Distance between mixing zone (position in aperture) and catalyzer is also constructed to make oxygenant achieve stabilized with mixture, and can not cause the autoxidation of oxidant/fuel mixture.
Define other preferred embodiment and advantage in the dependent claims.
Accompanying drawing explanation
Hereinafter, the preferred embodiment according to reforming reactor of the present invention will be discussed by means of accompanying drawing.This description should be considered as the example of the principle of the invention, and the scope of not intended to be limiting claim.
Fig. 1 shows the schematic diagram of the preferred embodiment of reforming reactor according to the present invention.
Embodiment
Reforming reactor 1 in Fig. 1 comprises housing 2, and this housing 2 has inwall 4, outer wall 6 and sidewall 8a, 8b.Inwall 4 and sidewall 8a, 8b define reaction chamber 10, hydrocarbon fuel 20 and oxygenant 14 by together with send in this reaction chamber 10, and can autothermal reaction be there is in this reaction chamber 10.
Inwall 4 and outer wall 6 define the space 12 between them.Space 12 define again between oxygenant supplying opening 16 and oxidant inlet 18, for the passage of oxygenant 14.
In addition, reforming reactor 1 comprises the catalyzer 28 for carrying out catalysis to the autothermal reaction in reaction chamber 10.Catalyzer 28 makes autothermal reaction accelerate, but also can use according to reforming reactor of the present invention when catalyst-free.Preferably, catalyzer 28 is metal grating or ceramic monoliths, but also can use other base material any of the design being suitable for catalyzer 28.
Oxidant inlet 18 is formed as multiple aperture, especially multiple hole or slit, and the size in described multiple aperture, shape and position can change according to used oxygenant 14, the hydrocarbon fuel 20 used and their temperature.Described multiple aperture can have identical size and dimension, but the size and dimension in these apertures each other also can be different.Preferably, the size in described aperture and the distance between these aperture and fuel inlet are designed, to realize best turbulent mixing, and make oxidant/fuel mixture be basic completely uniform before contacting with catalyzer 28.Distance D between mixing zone (position in aperture 18) and catalyzer 28 is also constructed to make oxygenant achieve stabilized with mixture, and can not cause the autoxidation of oxidant/fuel mixture.
In addition, reforming reactor 1 also has the hydrocarbon fuel entrance 22 of the sidewall 8a being arranged in housing 2.Preferably, this fuel inlet 22 is formed as fuel injector, and it provides fuel spray in reaction chamber 10.Reformed gas outlet 24 is provided with in the opposite side walls 8b of housing 2.Reformed gas 26 is hydrogen-rich gas, and it is the product of autothermal reaction, and can be used in the operation of fuel cell.
As shown in Figure 1, reforming reactor 1 also comprises the primary heater unit 30 for carrying out preheating to hydrocarbon fuel 20.In FIG, this fuel preheating device is illustrated as independent device 30, but also fuel injector 22 and fuel preheating device 30 can be integrated into single assembly.If fuel injector 22 is other and sidewall 8a thermal conductive contact, then the heat produced in reaction chamber 10 can be delivered to fuel injector 22, thus this heat can be utilized in fuel injector 22 to carry out hydrocarbon fuel 20 described in preheating.
Hereinafter, by exemplarily the diesel oil as hydrocarbon fuel being converted into hydrogen using air/steam mixture as oxygenant, the operation of reforming reactor 1 is described.Reaction for transforming is autothermal.
According to the present invention, before air/steam mixture 14 is injected in space 12 by oxygenant supplying opening 16, make air and vapor mixing, this space 12 is used as the air/steam passage of the oxidant inlet 18 air/steam mixture 14 being transported to reforming reactor 1 from oxygenant supplying opening 16.
In the way of the multiple hand-holes 18 in the inwall 4 leading to housing 2, air/steam mixture 14 utilizes the preheating to the heat trnasfer of air/steam mixture from inwall, and thus, this heat trnasfer also makes the inwall 4 of reaction chamber 10 cool.By cooling the inwall 4 of this reaction chamber 10, the diesel oil fuel molecule in reaction chamber 10 burns into cigarette ash risk when colliding in reaction chamber wall reduces.When the oxygen from air/steam mixture 14 reacts (C compared with " comparatively lightweight " hydrocarbon molecule of the diesel oil fuel 20 of short chain with having
xh
y+ O
2→ CO
2+ CO+H
2o), time, the inwall 4 of reaction chamber 10 is heated by the basic uniform oxidation occurred in reaction chamber 10.
Air/steam mixture 14 enters in the reaction chamber 10 of this reactor by aperture 18, thus in reaction chamber 10, form basic uniform air/steam smog, in reaction chamber 10, this air/steam mixture 14 is with by fuel injector 22, the diesel oil fuel 20 be sprayed onto in this air/steam smog mixes.
In order to the success of diesel oil fuel 20 with air/steam smog 14 mixes, need diesel oil fuel 20 to the substantially desirable atomization in air/steam smog 14 or vaporization, substantially to stop the condensation of fuel 20 or air/steam smog 14.To occur, so according to the present invention, diesel oil fuel 20 also carries out preheating by primary heater unit 30 because of the temperature difference between the air/steam smog 14 of preheating and usually colder diesel oil fuel 20 because this less desirable condensation is likely.By being preheating to by diesel oil fuel 20 close to but lower than the temperature of fuel minimum boiling point, achieving substantially desirable spraying of ruel or vaporization and air/steam mixture subsequently, also provide the heat of atomization for substantially desirable or vaporization thus.Preferably, air/steam smog 14 is also preheating to the temperature or the higher temperature that are in same range with the temperature of diesel oil fuel 20, and thus provide the temperature of the rising between fuel 20 and steam 14, this prevents condensation again substantially.
Due to the mixture that fuel (particularly diesel oil fuel) is different components, thus, each component has different boiling points, therefore preferably air/steam mixture is preheating to the temperature higher than the boiling point of the most light constituent in diesel oil fuel, the boiling point of this most light constituent defines the minimum boiling point of diesel oil fuel.If the temperature that the temperature of the air/steam mixture of preheating provides higher than the minimum boiling point by diesel oil fuel, then substantially avoid the light component condensation in this fuel, and the boiling point of the heavy component of the temperature convergence of fuel/air mixture/vapour mixture in fuel, thus can easily realize carburretion substantially completely.It should be noted that the condensation of the air/steam mixture caused owing to contacting with the pre-heating fuel of " colder " can not occur, because when air/steam mixture contacts with pre-heating fuel, this air/steam mixture is not cooled under its boiling point.
Atomized fuel mixes with air/steam smog and the combination of preheating of fuel obtains basic completely uniform reaction mixture, and it allows transforming substantially completely of hydrocarbon fuel, and this allows again High-efficient Production fuel cell level hydrogen.
According to the position in described aperture, size and the distance between these apertures and fuel injector 22, in reaction chamber 10, achieve the turbulent mixing that air/steam smog and diesel oil fuel are sprayed, make this mixture be basic completely uniform before contacting with catalyzer 28.
Then, this basic uniform gaseous mixture is introduced in catalyzer 28, in this catalyzer 28, and the hydro carbons experience autothermal reaction process of diesel oil fuel 20.In the autothermal reaction process occurred in catalyzer, the hydrogen (H), CO and CO that produce
2for main process product.These products are processed in the subsequent step of this reactor outside, its objective is to be separated with other process products all by H.
Reference numerals list:
1 reforming reactor
2 housings
4 inwalls
6 outer walls
8a, 8b side surface
10 reaction chambers
12 spaces=oxidant channel
14 oxygenants
16 oxygenant supplying openings
18 oxidant inlets
20 hydrocarbon fuel
22 hydrocarbon fuel entrances
24 hydrogen-rich gas outlets
26 hydrogen-rich gases
28 catalyzer
30 primary heater units
Claims (12)
1. hydrocarbon fuel is converted into the method for the hydrogen-rich gas applied for fuel cell and/or exhaust-gas disposal by one kind by autothermal reaction, described method uses following reforming reactor (1), described reforming reactor (1) has: housing (2), described housing (2) has two side surface (8a, 8b), described two side surfaces (8a, 8b) form the reaction chamber (10) of described reforming reactor (1); Fuel inlet (22), described fuel inlet (22) is arranged in a side surface (8a) in described two side surfaces, hydrocarbon fuel to be provided in described reaction chamber (10); And oxidant inlet (18), described oxidant inlet (18) is for being provided to oxygenant in described reaction chamber (10), and described method comprises the steps:
By described oxidizer preheat to substantially equal with the boiling point of described hydrocarbon fuel or higher than the temperature of described boiling point;
Described hydrocarbon fuel is preheating to the temperature more lower slightly than the boiling point of described hydrocarbon fuel; And
Described hydrocarbon fuel and described oxygenant are incorporated in described reaction chamber.
2. method according to claim 1, wherein, the mixing in described reaction chamber (10) of described hydrocarbon fuel and described oxygenant.
3. method according to claim 1 and 2, wherein, before described hydrocarbon fuel and described oxygenant are introduced in described reaction chamber (10), hydrocarbon fuel described in preheating and described oxygenant.
4. the method according to any one in aforementioned claim, wherein, in order to hydrocarbon fuel described in preheating, provide fuel preheating device, described fuel preheating device carried out preheating to described hydrocarbon fuel before described hydrocarbon fuel enters in described reaction chamber (10).
5. the method according to any one in aforementioned claim, wherein, uses air and steam as oxygenant, wherein preferably, before preheated air/vapour mixture, and air described in pre-mixing and steam.
6. the method according to any one in aforementioned claim, wherein, the preheating of described hydrocarbon fuel is by carrying out from described sidewall (8a) to the heat exchange of described fuel inlet (22).
7. the method according to any one in aforementioned claim, wherein, described hydrocarbon fuel is the mixture of different components, and wherein, by described oxidizer preheat to the temperature higher than the boiling point of the most light constituent in described hydrocarbon fuel, and/or wherein, described hydrocarbon fuel is preheating to the low-boiling temperature than the most light constituent in described hydrocarbon fuel.
8. the method according to any one in aforementioned claim, at least one in also comprising the steps:
In described reaction chamber, described hydrocarbon fuel and described oxygenant are mixed into uniform mixture, wherein preferably, described mixing is turbulent mixing; And
By autothermal reaction, described hydrocarbon fuel is converted into hydrogen-rich gas, wherein, preferably uses catalyzer.
9. the method according to any one in aforementioned claim, wherein, described reforming reactor (1) also comprises inwall (4) and outer wall (6), space (12) is formed between described inwall (4) and described outer wall (6), wherein said space (12) is designed to oxidant channel, described oxidant channel is located between the oxygenant supplying opening (16) arranged in described outer wall (6) and the described oxidant inlet (18) arranged in described inwall (4), and wherein, the step of oxygenant described in preheating is by carrying out from described inwall (4) to the heat exchange of described oxygenant.
10. the method according to any one in aforementioned claim, wherein, described in preheating, the step of hydrocarbon fuel is performed by fuel preheating device, and described fuel preheating device is the integral part of described fuel inlet (22).
11. methods according to any one in aforementioned claim, wherein, the step of hydrocarbon fuel described in preheating is by carrying out from described sidewall (8a) to the heat exchange of described fuel inlet (22).
12. methods according to any one in aforementioned claim, wherein, described hydrocarbon fuel is injected in described reaction chamber (10), sprays preferably by fuel injector.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510726740.8A CN105293435A (en) | 2008-07-02 | 2008-07-02 | Method for converting hydrocarbon fuel into hydrogen-rich gas |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008801301437A CN102143907A (en) | 2008-07-02 | 2008-07-02 | Reformer reactor and method for converting hydrocarbon fuels into hydrogen rich gas |
| CN201510726740.8A CN105293435A (en) | 2008-07-02 | 2008-07-02 | Method for converting hydrocarbon fuel into hydrogen-rich gas |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008801301437A Division CN102143907A (en) | 2008-07-02 | 2008-07-02 | Reformer reactor and method for converting hydrocarbon fuels into hydrogen rich gas |
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| Publication Number | Publication Date |
|---|---|
| CN105293435A true CN105293435A (en) | 2016-02-03 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510726740.8A Pending CN105293435A (en) | 2008-07-02 | 2008-07-02 | Method for converting hydrocarbon fuel into hydrogen-rich gas |
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2697032A (en) * | 1949-05-05 | 1954-12-14 | Phillips Petroleum Co | Acetylene gas producer |
| US3920416A (en) * | 1973-12-26 | 1975-11-18 | California Inst Of Techn | Hydrogen-rich gas generator |
| US5997596A (en) * | 1997-09-05 | 1999-12-07 | Spectrum Design & Consulting International, Inc. | Oxygen-fuel boost reformer process and apparatus |
| US20040086436A1 (en) * | 2002-10-31 | 2004-05-06 | Webasto Thermosysteme Gmbh | Mixture formation means for a reformer of a fuel cell system or for a heater |
| CN1496589A (en) * | 2000-10-30 | 2004-05-12 | Multifunction energy system operable as fuel cell, reformer or thermal plant | |
| US20040151663A1 (en) * | 2003-01-23 | 2004-08-05 | Luc Nougier | Partial oxidation reactor |
| EP1621246A1 (en) * | 2004-07-30 | 2006-02-01 | Delphi Technologies, Inc. | Reformer with a static mixer within the gas feeding means |
| US20080107937A1 (en) * | 2006-11-07 | 2008-05-08 | Francois Ravenda | Electrically-heated metal vaporizer for fuel/air preparation in a hydrocarbon reformer assembly |
| CN100519707C (en) * | 2003-04-04 | 2009-07-29 | 德士古发展公司 | Method and apparatus for rapid heating of fuel reforming reactants |
-
2008
- 2008-07-02 CN CN201510726740.8A patent/CN105293435A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2697032A (en) * | 1949-05-05 | 1954-12-14 | Phillips Petroleum Co | Acetylene gas producer |
| US3920416A (en) * | 1973-12-26 | 1975-11-18 | California Inst Of Techn | Hydrogen-rich gas generator |
| US5997596A (en) * | 1997-09-05 | 1999-12-07 | Spectrum Design & Consulting International, Inc. | Oxygen-fuel boost reformer process and apparatus |
| CN1496589A (en) * | 2000-10-30 | 2004-05-12 | Multifunction energy system operable as fuel cell, reformer or thermal plant | |
| US20040086436A1 (en) * | 2002-10-31 | 2004-05-06 | Webasto Thermosysteme Gmbh | Mixture formation means for a reformer of a fuel cell system or for a heater |
| US20040151663A1 (en) * | 2003-01-23 | 2004-08-05 | Luc Nougier | Partial oxidation reactor |
| CN100519707C (en) * | 2003-04-04 | 2009-07-29 | 德士古发展公司 | Method and apparatus for rapid heating of fuel reforming reactants |
| EP1621246A1 (en) * | 2004-07-30 | 2006-02-01 | Delphi Technologies, Inc. | Reformer with a static mixer within the gas feeding means |
| US20080107937A1 (en) * | 2006-11-07 | 2008-05-08 | Francois Ravenda | Electrically-heated metal vaporizer for fuel/air preparation in a hydrocarbon reformer assembly |
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