WO2009102760A1 - Reformeur et procédé de démarrage - Google Patents

Reformeur et procédé de démarrage Download PDF

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Publication number
WO2009102760A1
WO2009102760A1 PCT/US2009/033751 US2009033751W WO2009102760A1 WO 2009102760 A1 WO2009102760 A1 WO 2009102760A1 US 2009033751 W US2009033751 W US 2009033751W WO 2009102760 A1 WO2009102760 A1 WO 2009102760A1
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Prior art keywords
burner
fuel
distributor
air
catalytic
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Ceased
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PCT/US2009/033751
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English (en)
Inventor
Peter David Devries
Todd Healey
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Genesis Fueltech Inc
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Genesis Fueltech Inc
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Application filed by Genesis Fueltech Inc filed Critical Genesis Fueltech Inc
Publication of WO2009102760A1 publication Critical patent/WO2009102760A1/fr
Anticipated expiration legal-status Critical
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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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/32—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air
    • C01B3/34—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/386—Catalytic partial combustion
    • 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; Reversible storage of hydrogen
    • C01B3/02—Production of hydrogen; Production of gaseous mixtures containing hydrogen
    • C01B3/32—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air
    • C01B3/34—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen; Production of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide or air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
    • 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
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
    • 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
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0405—Purification by membrane separation
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/044—Selective oxidation of carbon monoxide
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0435—Catalytic purification
    • C01B2203/0445—Selective methanation
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • 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
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/085—Methods of heating the process for making hydrogen or synthesis gas by electric heating
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • C01B2203/1064—Platinum group metal catalysts
    • C01B2203/107—Platinum catalysts
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1217—Alcohols
    • C01B2203/1223—Methanol
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1288—Evaporation of one or more of the different feed components
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • 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

Definitions

  • This invention relates to the start-up and operation of reformers used for generating hydrogen for a variety of uses.
  • a linear burner distributor for supplying reformer heat is disclosed, where burner fuel is supplied through multiple openings in the distributor.
  • a linear electric heater in heat coupling relation to the distributor is described where the heater vaporizes the burner fuel upon reformer startup.
  • the heater may also pre-heat a catalytic burner element to the necessary temperature for light-off.
  • a method for initiating burner operation is also described.
  • the invention is particularly useful for applications where the fuel is miscible in water and pre-mixed, such as a methanol-water mix for reforming.
  • Reformers are devices which convert hydrogen-rich fuels into hydrogen gas and byproduct gases. Typically the reformer will have a burner to supply heat, and the fuel will be heated and introduced to a catalyst bed, where the chemical reaction of reforming takes place, liberating hydrogen from the fuel. In some cases the reformer also includes a purification step to separate the hydrogen from the reformed gas mixture, for example, to supply hydrogen for a fuel cell. [0003] There have been a variety of patent disclosures regarding the startup and operation of reformers, and the burners utilized for such. In US 4,946,557 B.
  • Beshty disclose a reformer utilizing a burner, where the burner which can either accept a methanol-water mix, or a combustible gaseous mixture containing hydrogen and other gases. These gases are produced during operation of the reformer after startup has been completed.
  • the burner, heat exchanger, catalyst bed, and other parts are arranged such that the elements are in parallel with each other. Burner gases for supplying process heat can then flow perpendicular to the parallel arrangement of the parts. With respect to the burner, this arrangement favors a long fuel distributor, such as a tube with periodic holes for fuel distribution and mixing with burner air.
  • a fuel mix such as methanol- water are vaporized and sent to the burner, have difficulties upon application to the linear arrangement. Specifically, on cold startup, the long distributor tube for the burner will condense the vaporized methanol-water mix, preventing the proper mixing of the fuel and air for burner light-off.
  • the necessary light-off temperature for initiation of combustion may not take place without adding heat.
  • the heating element may additionally supply sufficient heat for bringing the catalytic burner element to the light-off point.
  • a single heating element can be located within the burner distributor tube, or adjacent to it, to perform this task.
  • two heaters can be employed - one to maintain the distributor above the boiling point, and another to heat the catalyst for light-off.
  • Fuel may arrive at the burner distributor in the liquid phase for vaporization at the distributor itself, or it may arrive already vaporized.
  • a method for reformer startup may therefore be employed.
  • the electric heating elements are heated up so that incoming liquid fuel remains vaporized in the burner distributor.
  • the catalytic burner element is preheated so that the arriving fuel will be ignited upon its arrival and mixture with incoming air.
  • the reformer will heat up to operating temperature, at which point the burner may then be fueled with combustible gases produced from the reforming reaction.
  • Fig. 1 shows the general cross section of a burner arrangement for a linear reformer.
  • the elements in Figure 1 retain a similar cross-section at various positions along the linear axis of the reformer.
  • the cross section in Fig. 1 is perpendicular to the linear axis.
  • the linear burner is enclosed within two sheet metal walls 10a and 10b, preferably constructed of higher temperature capable material such as stainless steel or any high temperature alloy.
  • Incoming combustion air 6 is mixed with fuel 5 resulting in combustible mixture 11.
  • Combustible mixture 11 arrives at catalytic burner element 12, and exits catalytic burner element 12 as heated flue gas 13.
  • Catalytic burner element 12 can consist, for example, of a support structure upon which a catalytic material, such as platinum, is deposited.
  • Insulating blocks 7, 8, and 9 prevent metal walls 10a and 10b from becoming too hot, and guide the gases into catalytic burner element 12.
  • Insulating blocks 7, 8, and 9 are preferably constructed of a low-density ceramic material.
  • Burner distributor tube 2 is disposed such that holes or aperatures 4 in burner distributor tube 2 are able to send combustible fuel 5 in mixing relation with incoming burner air 6, prior to arriving at catalytic burner element 12.
  • An electric heater 1 is placed in the interior 3 of burner distributor tube 2, such that burner distributor tube 2 can be heated and combustible fuel 5 can be vaporized.
  • Fig. 2 Holes or aperatures 4 in burner distributor tube 22 (Fig. 2) are placed at multiple intervals along burner distributor tube 2 such that fuel is supplied along the linear axis of the burner.
  • Electric heater 1 may be optionally placed adjacent and exterior to burner distributor tube 2, such that sufficient heat is transferred to burner distributor tube 2 to vaporize combustible fuel 5. Heat from electric heater 1 is also functional to heat adjacent catalytic burner element 12 to sufficient temperature for light-off of arriving mixed fuel and air 11. Optionally, an additional heater (not shown) may be used to separately heat up catalytic burner element 12 to the light-off temperature.
  • Fig. 2 shows the burner in a typical linear reformer arrangement in reformer assembly 23. Reformer assembly 23 is housed in housing 23a, typically constructed of temperature tolerant metal such as stainless steel or a high temperature alloy.
  • Combustion air for the burner arrives in inlet air plenum 21, via an air moving device such as a fan or blower (not shown).
  • the air in plenum 21 then moves into the burner as preheated burner air 6, after receiving heat from heat exchange plates 18.
  • Burner distributor 22, previously described in Fig. 1, supplies fuel 5.
  • Fuel 5 mixes with preheated air 6 and forms combustible mixture 11, which then travels through catalytic combustor 12.
  • Heated flue gas 13 then travels transversely past linear steam reforming catalyst element 14, such that heat is transferred to the steam reforming reaction within catalyst element 14.
  • catalyst element 14 may, by way of example, consist of a finned tube, with tube 14a and attached fins 14b, to facilitate heat transfer into the interior of tube 14a, which is filled with reforming catalyst 14c.
  • Catalyst 14c is effective to perform the endothermic steam reforming reaction, for example, the conversion of methanol and steam to hydrogen and carbon dioxide.
  • the catalyst element 14 may be configured in other ways as well, such as a microchannel catalyst bed arranged in a planar rather than a tubular fashion, with a main linear axis in parallel with the burner distributor 22.
  • the flow direction of the reformed gases in the catalyst bed need not always follow the linear axis; however, the catalyst bed structure will have an overall construction such that it has an axis in parallel with the burner distributor 22.
  • One such example is a helical arrangement of a catalyst- filled finned tube, where the helical axis of rotation is in parallel with burner distributor 22.
  • Other arrangements may be envisioned by those skilled in the art.
  • heated flue gas 13 travels past the catalyst bed 14, it arrives in heated space 16.
  • a hydrogen-purifying element may be optionally placed in heated space 16.
  • a typical example is a membrane purifier using a palladium alloy, which allows only hydrogen to permeate the membrane, effectively purifying the reformed gases.
  • Cooler flue gas 17 further transfers heat via heat exchange plates 18 to effectively heat incoming burner air 6.
  • Heat exchange plates 18 are separated by thermally insulating gaskets 19 to form a counterflow heat exchanger. After traveling through the heat exchanger exit gases arrive at exhaust plenum 20.
  • Boiler assembly 15 as shown consists of a serpentine assembly containing three boiler tubes, 15a, 15b, and 15c.
  • Boiler tubes consist of metal tubes such as 15-b2, with attached fins 15-bl, to assist with heat transfer from the flue gas 13 to the fuel inside the tubes.
  • Fuel arrives first in tube 15a, and is subsequently transferred to tube 15b via a connection (not shown), and subsequently to tube 15c.
  • serpentine arrangement of tubes 15 can therefore pull heat from heated flue gas 13 in counterflow fashion. This allows the fuel to be boiled and preheated prior to arrival in catalyst bed 14 via a connection between boiler tube 15c and catalyst bed 14 (not shown).
  • Flue gas heat exchanger plates 18 and gaskets 19 are more clearly shown in Figs. 3 and 4.
  • Fig. 3 a typical set of heat exchanger plates 18 are shown with gas flow apertures 18b shown.
  • the heat exchanger plates are preferably staggered when they are stacked, as shown in Fig. 3, so that the heat exchange gases are continually making 90 degree turns to flow past the plates, facilitating heat exchange.
  • Between each plate is a thermally insulating gasket 19 (Fig. 2), further illustrated in Fig. 4.
  • Typical construction of the gasket includes materials such as an alumina-silica felt. Air traveling to the burner travels through aperture 25a, while exiting flue gas 17 travels through aperture 25b.
  • Heat exchanger plates 18 are typically constructed of aluminum, however the plates most proximal to the burner may be constructed of a higher temperature material such as stainless steel to shield the aluminum plates from excessive temperature.
  • the reformer may be effective as a hydrogen supplying steam reformer as long as carbon monoxide levels in the reformed gases are reduced. In such cases, it may be desirable to include a low- temperature shift stage to the reformer, downstream of the first catalyst bed 14.
  • a low- temperature shift stage to the reformer, downstream of the first catalyst bed 14.
  • Reformed gases from catalyst bed 14 exit the catalyst bed 14 via connection line 30 to cooldown stage 28.
  • Cooldown stage 28 may, for example, consist of a finned tube for transferring excess heat 29 to plenum 35.
  • Plenum 35 is located within the plates 18 of the counterflow heat exchanger at a position where the amount of heat shed 29 from cooldown stage 28 is at the desired level. Moving the cooldown stage 28 and plenum 35 closer to the air inlet plenum 21 (by adjusting the number of heat exchange plates 18 above and below plenum 35) allows the amount of heat shed 29 at cooldown stage 28 to increase, as the air in plenum 35 will be cooler. Placement within the heat exchanger can thus be adjusted until the desired exit temperature at cooldown stage 29 via connection line 31 is achieved to low temperature shift bed 32 in plenum 36.
  • a desirable inlet temperature to low temperature shift bed 32 can be between 150 to 250 Celsius when using a typical CuZnO low temperature shift catalyst 33 in shift bed 32.
  • Reformed gases with reduced carbon monoxide levels exit the shift bed 32 via exit line 34, where they may be sent to a fuel cell or further processed prior to being sent to a fuel cell. Further processing might include a methanation step to convert carbon monoxide to methane, selective oxidation of carbon monoxide, or a hydrogen purification step using pressure swing absorption. Other steps might include using the available heat from the reformed gases to preheat the incoming fuel arriving at the boiler assembly 15, preferably in counterflow fashion.
  • FIG. 5 The embodiment in Fig. 5 is flexible in regard to which processes are inserted into plenum 35 or plenum 36. Heat may be removed from the reformed gases in either plenum, and various catalytic processes can be introduced into either plenum, either endothermic or exothermic.
  • the desired temperature of the particular process will dictate the position of the heat exchanger, such as cooldown stage 29, to achieve the desired process temperature by coupling the heat exchanger to either the incoming air for the burner or the cooling gases exhausting the unit.
  • the heat exchanger such as heat exchanger 29 may also be combined with the catalyst bed such as shift bed 32 into a single integrated unit in either plenum.
  • the variations and processes are apparent to those skilled in the art. Example 1
  • a linear reformer was constructed generally with the layout shown in
  • the exhaust heat exchanger comprised of 20 slotted aluminum plates less than 0.032" thick, with 50% open area, with offset openings between successive plates.
  • the two plates closest to the burner were constructed of stainless steel.
  • Thin spacer gaskets constructed of alumina-silica felt were placed between the plates to form a seal and to space the plates.
  • the reformer further consisted of a 200 cell per inch extruded cordierite catalytic burner with a platinum coating for catalytic activity.
  • the catalyst bed consisted of a finned tubes filled with platinum-based catalyst, and the boiler assembly consisted of a serpentine of 4 finned !4" diameter tubes. Gases exiting the catalyst bed were routed to a hydrogen purifier which resided in the flue gas stream downstream of the catalyst bed.
  • the purifier, catalyst bed, boiler, catalytic burner, and burner distributor were all on a common parallel axis.
  • the burner distributor consisted of a 5/16" metal tube with 10 round aperatures 0.030" in diameter.
  • the distributor was 7" long and had a 1/8", 125 watt heater in the center of the distributor tube.
  • a fuel pump was used to pump a 65/35 volume percent methanol water mix to the burner distributor.
  • Operation of the reformer was initiated by turning on the electric heater for 4 minutes, blowing a small amount of air through the burner to additionally move some heat into the catalytic burner material. Once the burner distributor and catalytic burner material were sufficiently hot, small amounts of methanol/ water mix were pumped through a diverting valve into the burner distributor. As the exit flue gas temperature from the catalytic burner increased, the fuel pumping rate and air flow rate were increased. The electric heater was turned off once the burner was hot enough to no longer require the electric heat.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un reformeur linéaire destiné à libérer de l’hydrogène à partir d’un stock d’alimentation qui contient de l’hydrogène. Le reformeur est utilisable sur des combustibles tant gazeux que liquides et possède un distributeur de brûleur linéaire qui comporte au moins deux ouvertures de distribution de combustible pour distribuer le combustible, une alimentation en air, où le combustible et l’air se mélangent dans une cavité de mélange linéaire pour former un mélange combustible de façon catalytique, un élément de brûleur catalytique, un élément chauffant électrique dans une relation de transfert thermique avec au moins l’un parmi le distributeur de brûleur et l’élément de brûleur catalytique, un lit catalytique, une chaudière pour faire bouillir et chauffer le stock d’alimentation, et un échangeur thermique d’échappement efficace pour préchauffer l’alimentation en air du brûleur. Le distributeur de brûleur, le lit catalytique, la chaudière de stock d’alimentation, et l’échangeur thermique d’échappement sont tous des éléments linéaires qui possèdent un axe parallèle commun, de sorte que des gaz d’échange thermique issus du brûleur se déplacent transversalement à l’axe parallèle commun. Le distributeur de brûleur reçoit de la chaleur de l’élément chauffant électrique de sorte que le combustible qui arrive peut être au moins partiellement vaporisé, et l’élément chauffant électrique chauffe l’élément brûleur catalytique jusqu’à une température suffisante pour que le mélange de combustible et d’air vaporisé amorce la combustion catalytique.
PCT/US2009/033751 2008-02-12 2009-02-11 Reformeur et procédé de démarrage Ceased WO2009102760A1 (fr)

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US2804708P 2008-02-12 2008-02-12
US61/028,047 2008-02-12

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WO2010066464A1 (fr) * 2008-12-12 2010-06-17 Ezelleron Gmbh Système de pile à combustible à barrière anti-réoxydation
ITCO20100005A1 (it) * 2010-01-27 2011-07-28 Giacomini Spa "combustore per la combustione di idrogeno su un catalizzatore e caldaia per tali combustori"
DE102015004121A1 (de) * 2015-03-31 2016-10-06 Linde Aktiengesellschaft Ofen mit elektrisch sowie mittels Brennstoff beheizbaren Reaktorrohren zur Dampfreformierung eines kohlenwasserstoffhaltigen Einsatzes
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