EP2027061A1 - Procédé de régénération d'un reformeur - Google Patents

Procédé de régénération d'un reformeur

Info

Publication number
EP2027061A1
EP2027061A1 EP06742411A EP06742411A EP2027061A1 EP 2027061 A1 EP2027061 A1 EP 2027061A1 EP 06742411 A EP06742411 A EP 06742411A EP 06742411 A EP06742411 A EP 06742411A EP 2027061 A1 EP2027061 A1 EP 2027061A1
Authority
EP
European Patent Office
Prior art keywords
reformer
fuel
zone
regeneration
air ratio
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP06742411A
Other languages
German (de)
English (en)
Inventor
Stefan Käding
Stefan Kah
Andreas Lindermeir
Marco Mühlner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Enerday GmbH
Original Assignee
Enerday GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Enerday GmbH filed Critical Enerday GmbH
Publication of EP2027061A1 publication Critical patent/EP2027061A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C01B3/382—Multi-step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
    • B01J8/0214—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical annular shaped bed
    • 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
    • C01B3/384—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 the catalyst being continuously externally heated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/12—Treating with free oxygen-containing gas
    • B01J38/14—Treating with free oxygen-containing gas with control of oxygen content in oxidation gas
    • 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
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C01B2203/0255—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a non-catalytic partial oxidation 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • 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
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • 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
    • C01B2203/16—Controlling the process
    • C01B2203/169—Controlling the feed
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Definitions

  • the invention relates to a method for regenerating a reformer, the continuous reformer operation, a mixture of fuel and oxidant is supplied with an average air ratio ⁇ i, wherein for the purpose of regeneration of the reformer, the air ratio is changed.
  • the invention further relates to a system with a reformer and a controller.
  • Generic methods have numerous fields of application. In particular, they serve to supply a hydrogen-rich gas mixture to a fuel cell, from which then on the basis of electrochemical processes electrical
  • APUs auxiliary power unit
  • the reforming process for converting fuel and oxidant to reformate can be done according to different principles.
  • catalytic reforming is known in which part of the fuel is oxidized in an exothermic reaction.
  • a disadvantage of this catalytic reforming is the high heat generation, the system components, in particular the catalyst can irreversibly damage.
  • Another possibility for generating a reformate from hydrocarbons is the "steam reforming". In this case, hydrocarbons are converted by means of water vapor in an endothermic reaction to hydrogen.
  • a combination of these two principles that is, the reforming based on an exothermic reaction and the generation of hydrogen by an endothermic reaction in which the energy for steam reforming is derived from the combustion of the hydrocarbons, is referred to as autothermal reforming.
  • autothermal reforming there are the additional disadvantages that a supply of water must be provided. High temperature gradients between the oxidation zone and the reforming zone pose further problems in the temperature regime of the entire system.
  • reaction in which air and fuel are converted into a hydrogen-rich gas mixture in a reformer can be formulated as follows:
  • DE 101 52 083 A1 describes a reformer to which fuel, steam and oxygen are supplied. As a solution for avoiding overheating, it is proposed in DE 101 52 083 A1 to carry out the regeneration in a pulsed manner by increasing the air ratio of the supplied mixture for limited time intervals. An influence on the reforming operation is inevitable, so that, for example, the fuel cell system removable e- lectric power is reduced.
  • the invention has for its object to enable the regeneration of a reformer while avoiding influencing the reforming operation.
  • the invention is based on the method according to the invention in that the regeneration is carried out in a shutdown phase of the reformer by operating the reformer during several successive time intervals with an air ratio ⁇ 2 > ⁇ i which is increased compared to the reformer operation.
  • fuel and air are continuously fed to the reformer.
  • Temperatures in the range above and above 650 ° C. prevail.
  • the reformer operates in thermal equilibrium, so that no increase in temperature is to be expected in steady-state operation.
  • the described deposits in the catalyst gradually lead to a deactivation.
  • a fuel cell system and thus also the reformer are switched off regularly, at least during a longer standstill of the vehicle.
  • the switch-off phase can be used advantageously for regeneration. It should be noted, however, that even during the shutdown phase with long-term increase in the air ratio, be it by reducing the amount of fuel supplied, by increasing the amount of air supplied or by both, excessive heating is expected, resulting in destruction of the catalyst or of the complete reformer. This is related to the fact that the Rußabbrandretim C + O 2 -> CO 2
  • the fuel supply be reduced in a pulsed manner during the switch-off phase, wherein the individual pulses last only over a short period of time. Oxygen or air is brought to the soot deposit, so that the oxidation process can begin. Consequently, the temperature in the catalyst also increases. However, before the temperature is so high that the reformer can be damaged, the fuel supply is increased again. Thus, at the end of a time interval with a reduced feed rate, a part of the reformer is regenerated, that is, substantially soot-free or deposit-free.
  • the invention is advantageously developed in that the feed rate of the fuel during at least one of the successive time intervals is zero. wearing. Due to the complete shutdown of the fuel supply during the successive time intervals, an efficient burning of the deposits can take place. Not complete shutdown of the fuel supply leads to an increased water production in the reformer. This water is able to remove the soot and other deposits from the reformer according to the equation
  • the oxygen content at the outlet of the reformer thus serves as an indicator for the complete regeneration of the reformer.
  • the oxygen content is measured by a lambda probe.
  • the oxygen content is measured by a fuel cell. If you want to save the installation of a lambda probe, the electrical output values of the fuel cell can be used directly to detect an increase in the oxygen content. Other measurement methods for determining the lambda value can also be used, for example infrared or CO measurements.
  • the method according to the invention is particularly useful in the context that, in a reformer with two fuel feeds, one of the fuel feeds operates during regeneration at a feed rate substantially equal to the feed rate in continuous operation. In a reformer with two fuel feeds, one thus has a greater possibility of variation with regard to a change in the fuel feed rate. This concerns in particular the possibility of a partially unchanged operation of the reformer, while in other areas of the reformer by functional changes a regeneration takes place, if this is desired during the reformer operation, ie outside the shutdown phase.
  • the process according to the invention is usefully developed in this connection by the reformer having an oxidation zone and a reforming zone that heat can be supplied to the reforming zone, that the oxidation zone is supplied with a mixture of fuel and oxidant using a first fuel feed, which after at least Partial oxidation of the fuel is at least partially fed to the reforming zone, that the reforming zone additionally fuel is fed using a second fuel supply and that the second fuel supply operates during the successive time intervals with a reduced feed rate.
  • the additionally supplied fuel thus forms, together with the exhaust gas from the oxidation zone, the starting gas mixture for the reforming process.
  • ⁇ 0.4
  • heat can be supplied to the reforming zone from the exothermic oxidation in the oxidation zone.
  • the heat energy generated in the oxidation zone is thus converted in the context of the reforming reaction, so that the net heat production of the overall process does not lead to problems in the temperature budget of the reformer.
  • the reforming zone has an oxidant feed, via which additionally oxidizing agent can be fed.
  • the reforming zone has an oxidant feed, via which additionally oxidizing agent can be fed.
  • another parameter for influencing the reforming is available, so that it can be optimized.
  • the invention is developed in a particularly useful way in that the additional fuel can be fed to an injection and mixture-forming zone and that the additional fuel can flow from the injection and mixture-forming zone into the reforming zone.
  • This injection and mixture-forming zone is thus upstream in the flow direction of the reforming zone, so that the reforming zone is provided with a well-mixed starting gas for the reforming reaction.
  • the additional fuel is at least partly due to the thermal energy of the gas mixture emerging from the oxidation zone.
  • the heat of reaction from the oxidation can also be used advantageously for the evaporation process of the fuel.
  • the gas mixture produced in the oxidation zone may be fed to the reforming zone, bypassing the injection and mixture-forming zone.
  • a further possibility for influencing the reforming process is available so that a further improvement of the reformate leaving the reformer can be achieved with regard to its application.
  • the invention is based on the method according to the invention in that the regeneration takes place in a starting phase of the reformer in that the reformer with an air ratio ⁇ 2 > ⁇ ! as long as it is operated continuously until a critical temperature threshold is reached.
  • the temperatures occurring in the reformer are not critical. It is therefore not necessary to choose a pulsed reformer operation for the purpose of regeneration. Rather, regeneration of the reformer can be carried out continuously via the increased air ratio.
  • the reformer is operated in the starting phase with an air ratio ⁇ l.
  • the Re- shaper therefore ultimately works like a burner, with air ratios of ⁇ > 1 being uncritical at comparatively low temperatures of a downstream fuel cell system.
  • the critical temperature threshold is defined by the fact that the reformer or components of the reformer have temperatures between 450 and 650 ° C.
  • the critical temperature threshold is defined by the fact that a fuel cell stack or components of the fuel cell stack downstream of the reformer have temperatures between 450 and 550 ° C. If you end the regeneration during the start-up phase, for example, at a temperature of the fuel cell stack of 500 0 C, it is avoided that in a further increase in temperature in the fuel cell stack of entering the fuel cell stack excess oxygen leads to damage to the anode side.
  • the invention is developed in a particularly advantageous manner by virtue of the fact that regeneration following the starting phase of the reformer takes place in that the reformer is operated for several successive time intervals with an increased air ratio compared to the reformer operation. Pulsed operation is useful after the startup phase to avoid overheating.
  • the regeneration takes place during each start-up phase of the reformer. Since the operation of the reformer in the manner of a burner can serve both the preheating of the system and the regeneration, can at every system start the advantageous regeneration are performed.
  • the invention further relates to a system with a reformer and a controller which enables a regeneration of the reformer, wherein the controller is suitable for controlling a method according to the invention.
  • FIG. 1 shows a flow chart for explaining a method according to the invention
  • FIG. 2 is a flowchart for explaining a regeneration during the reforming operation.
  • Figure 3 is a schematic representation of a reformer according to the invention.
  • FIG. 1 shows a flow chart for explaining a method according to the invention.
  • the reformer is operated with an air ratio ⁇ l. This corresponds to a burner operation.
  • the burner operation is used for regeneration, in particular carbon, carbon compounds, sulfur and sulfur compounds are removed from the reformer. Regeneration also affects other organic and inorganic compounds that are deposited in the reformer.
  • T is already an N critical value T ⁇ has exceeded. This critical value can be determined by the reformer himself, for example, the temperature upper limit permissible for the catalyst in the reforming zone, or else determined by the fuel cell stack downstream of the reformer.
  • step S07 the operation of the reformer is ended (step S07).
  • FIG. 2 shows a flowchart for explaining a regeneration during the reforming operation.
  • the fuel supply is turned off in step S02.
  • step S03 a temperature in the reformer is detected.
  • step S04 it is determined whether this detected temperature is greater than a predetermined threshold T S ⁇ . If this is not the case, the temperature in the reformer is again detected in step S03 when the fuel supply is switched off. If it is determined in step S04 that the temperature exceeds the threshold value T s i, is in Step S05, the fuel supply is turned on again. Subsequently, the temperature in the reformer is detected again in step S06.
  • step S07 it is determined whether this detected temperature is smaller than a predetermined threshold T 32 . If this is not the case, the temperature in the reformer is detected again in step S06; the fuel supply remains switched on. If it is determined in step S07 that the temperature is lower than the threshold temperature Ts 2r , the fuel supply is turned off again according to step S02, so that the next time interval to the reformer generation begins.
  • step S8 In parallel to the temperature monitoring, there is a monitoring for oxygen breakdown in the reformer according to step S08. This is to determine the end of the regeneration. Thus, if an oxygen breakthrough takes place, if the fuel supply is switched off, the fuel supply is turned on in accordance with step S09. Subsequently, the regeneration ends according to step S10.
  • FIG. 3 shows a schematic representation of a reformer according to the invention.
  • the invention is not bound to the specific design of the reformer shown here. Rather, the regeneration according to the invention can take place in different types of reformers, as long as it is possible to reduce or interrupt the supply of fuel in the short term.
  • the reformer 10 shown here which is based on the principle of partial oxidation, preferably without supplying water vapor, fuel 12 and oxidizing agent 16 can be fed via respective feeders.
  • the oxidizing agent 16 is usually air.
  • the immediate at the beginning Combustion resulting heat of reaction can be partially removed in an optionally provided cooling zone 36.
  • the mixture then continues into the oxidation zone 24, which may be realized as a pipe located within the reforming zone 26.
  • the oxidation zone is realized by a plurality of tubes or by a special tube guide within the reforming zone 26.
  • conversion of fuel and oxidant takes place in an exothermic reaction with ⁇ »1.
  • the resulting gas mixture 32 then enters an injection and mixture forming zone 30 in which it is mixed with injected fuel 14.
  • the thermal energy of the gas mixture 32 can support the evaporation of the fuel 14.
  • the mixture thus formed then passes into the reforming zone 26, where it is reacted in an endothermic reaction with, for example, ⁇ ⁇ 0.4.
  • the heat 28 required for the endothermic reaction is removed from the oxidation zone 24.
  • oxidizing agent 18 can additionally be fed into the reforming zone 26. Furthermore, it is possible to supply part of the gas mixture 34 generated in the oxidation zone 24 directly to the reforming zone 26, bypassing the injection and mixture-forming zone 30. The reformate 22 then flows out of the reforming zone 26 and is available for other applications.
  • a controller 38 which can control, among other things, both the primary 12 and secondary fuel feeds 14.
  • controller 38 can control, among other things, both the primary 12 and secondary fuel feeds 14.
  • the catalyst provided in the reforming zone 26 is then burned with combustion exhaust gases containing oxygen.

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  • Chemical & Material Sciences (AREA)
  • 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)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Fuel Cell (AREA)

Abstract

L'invention concerne un procédé de régénération d'un reformeur, qui est alimenté, lors d'un fonctionnement continu du reformeur, par un mélange de combustible (12, 14) et d'agent d'oxydation (16, 18, 20) avec un indice d'air moyen ?<SUB>1</SUB>, l'indice d'air étant modifié en vue de la régénération du reformeur. Selon l'invention, la régénération a lieu pendant une phase d'interruption du reformeur. À cet effet, le reformeur est mis en fonctionnement pendant plusieurs intervalles successifs de temps avec un indice d'air augmenté ?<SUB>2</SUB>>?<SUB>1</SUB> par rapport au fonctionnement du reformeur. Selon l'invention, la régénération peut également avoir lieu pendant une phase de début du reformeur. À cet effet, le reformeur est mis en fonctionnement en continu avec un indice d'air augmenté ?<SUB>2</SUB>>?<SUB>1 </SUB>par rapport au fonctionnement du reformeur, jusqu'à ce qu'un seuil critique de température soit atteint. L'invention concerne d'autre part un système comportant un reformeur et un dispositif de commande permettant la mise en oeuvre dudit procédé.
EP06742411A 2006-06-12 2006-06-12 Procédé de régénération d'un reformeur Withdrawn EP2027061A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/DE2006/001008 WO2007143960A1 (fr) 2006-06-12 2006-06-12 Procédé de régénération d'un reformeur

Publications (1)

Publication Number Publication Date
EP2027061A1 true EP2027061A1 (fr) 2009-02-25

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Country Status (10)

Country Link
US (1) US20100112392A1 (fr)
EP (1) EP2027061A1 (fr)
JP (1) JP2009539749A (fr)
CN (1) CN101479187A (fr)
AU (1) AU2006344607A1 (fr)
BR (1) BRPI0621741A2 (fr)
CA (1) CA2653415A1 (fr)
DE (1) DE112006003993A5 (fr)
EA (1) EA200870481A1 (fr)
WO (1) WO2007143960A1 (fr)

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CN101479187A (zh) 2009-07-08
WO2007143960A1 (fr) 2007-12-21
DE112006003993A5 (de) 2009-06-10
AU2006344607A1 (en) 2007-12-21
CA2653415A1 (fr) 2007-12-21
JP2009539749A (ja) 2009-11-19
EA200870481A1 (ru) 2009-04-28
US20100112392A1 (en) 2010-05-06

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