EP1616131A1 - Procede et dispositif d'utilisation d'un bruleur d'un moteur thermique, notamment d'un systeme de turbines a gaz - Google Patents

Procede et dispositif d'utilisation d'un bruleur d'un moteur thermique, notamment d'un systeme de turbines a gaz

Info

Publication number
EP1616131A1
EP1616131A1 EP03735236A EP03735236A EP1616131A1 EP 1616131 A1 EP1616131 A1 EP 1616131A1 EP 03735236 A EP03735236 A EP 03735236A EP 03735236 A EP03735236 A EP 03735236A EP 1616131 A1 EP1616131 A1 EP 1616131A1
Authority
EP
European Patent Office
Prior art keywords
fuel
oxidizer mixture
oxygen
mixture
burner
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Withdrawn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
EP03735236A
Other languages
German (de)
English (en)
Inventor
Timothy Griffin
Dieter Winkler
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.)
General Electric Technology GmbH
Original Assignee
Alstom Technology AG
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 Alstom Technology AG filed Critical Alstom Technology AG
Publication of EP1616131A1 publication Critical patent/EP1616131A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/007—Supplying oxygen or oxygen-enriched air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23R—GENERATING COMBUSTION PRODUCTS OF HIGH PRESSURE OR HIGH VELOCITY, e.g. GAS-TURBINE COMBUSTION CHAMBERS
    • F23R3/00—Continuous combustion chambers using liquid or gaseous fuel
    • F23R3/40—Continuous combustion chambers using liquid or gaseous fuel characterised by the use of catalytic means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/13002—Catalytic combustion followed by a homogeneous combustion phase or stabilizing a homogeneous combustion phase
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07001—Injecting synthetic air, i.e. a combustion supporting mixture made of pure oxygen and an inert gas, e.g. nitrogen or recycled fumes
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/32—Direct CO2 mitigation
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to a method and a device for operating a burner of a heat engine, in particular a gas turbine system, with a burner inlet to which a mixture of a fuel and an oxygen-enriched carrier gas is supplied for combustion within a combustion chamber adjoining the burner inlet in the flow direction becomes.
  • the above-mentioned gas turbine concept is based on the combustion of fossil fuels, in particular gaseous fuels, such as methane, in the presence of a mixture of recirculated exhaust gas, in which C0 2 , H 2 0 and oxygen as an oxidizing agent and not, as in conventional combustion processes, under Formation of a fuel-air mixture that contains considerable nitrogen.
  • gaseous fuels such as methane
  • the C0 2 exhaust gas stream is, on the one hand, fed back into the gas turbine process as a C0 2 mass flow for combustion as part of a partial stream recirculation, the remaining residual exhaust gas stream is deposited on the other hand in a suitable recycling or in compressed form for final storage in suitable geological layers of earth and thus to the free atmosphere as harmful greenhouse gas completely removed.
  • oxygen separation devices are suitable for this purpose, which are equipped with a membrane which conducts oxygen ions and electrons, a so-called MCM membrane (mixed conducting membrane).
  • MCM membrane mixed conducting membrane
  • the carrier gas stream enriched with oxygen consists exclusively of C0 2 , H 2 0 and pure oxygen as the oxidizer, this mass flow is also referred to below as the oxidizer mixture.
  • the oxidizer mixture obtained with the aid of the oxygen separation device is further mixed with gaseous fuel, preferably CH 4 , and ignited as a fuel / oxidizer mixture within the combustion chamber and brought to combustion.
  • the recirculated exhaust gas stream to be enriched with oxygen is conducted on the permeate side through the oxygen separation device along to the MCM membrane at high flow velocity, as a result of which the permeate-side oxygen concentration is reduced and the propellant gradient between the retentate side, through which a preheated, oxygen-containing gas flows, and the permeate side is increased.
  • the oxygen enrichment the oxygen content within the carrier gas stream exiting from the oxygen separation device is too low to achieve a stable and effective combustion of the fuel / oxidizer mixture which is formed with the aid of common combustion techniques.
  • Time-delayed ignition behavior also disadvantageously affects the dwell times for the complete combustion of the ignited fuel / oxidizer mixture within the combustion chamber, whereby the CO and unburned hydrocarbon components that are produced during the combustion are also far above those values which are obtained with conventional combustion technology .
  • the reduced ignitability or reactivity of the fuel / oxidizer mixture also has a reducing effect on the flame speed, as a result of which the so-called lean extinguishing limits are reduced.
  • the absolutely critical effects listed above on the combustion behavior when using a fuel / oxidizer mixture are further aggravated if one takes into account the fact that the maximum temperature of the exhaust gas products resulting from the combustion should be relatively low, for example max. 1250 ° C. in order to avoid damage to the components provided along the exhaust gas recirculation, such as, for example, an MCM membrane within the oxygen separation device and the high-temperature heat exchanger for preheating the oxygen-containing gas to be supplied to the oxygen separation device.
  • the catalyst material required for the catalytic oxidation of the fuel typically platinum or palladium
  • support materials such as, for example, aluminum oxide, silicon oxide or zirconium oxide, which is unstable at such high temperatures and a water vapor content of greater than 50% are or will begin.
  • the invention is based on the object of a method and a device for operating a burner of a heat engine, in particular a gas turbine system, with a burner inlet, which has a mixture of a fuel and an oxygen-enriched carrier gas for combustion within a flow adjoining the burner inlet Combustion chamber is supplied to develop such that the disadvantages mentioned above as well as technical difficulties to the prior art are to be avoided.
  • a working gas for the operation of a burner working according to the AZEP principle using common combustion techniques, which enables stable and complete combustion within the combustion chamber, while complying with all the temperature limits required by the components for providing the working gas.
  • a first oxidizer mixture i.e. an oxygen-enriched carrier gas stream is provided, which is obtained in a manner known per se, as mentioned above.
  • This first oxidizer mixture is mixed with fuel, preferably gaseous fossil fuel, such as methane, to form a first fuel / oxidizer mixture.
  • a second oxidizer mixture is also provided, the material composition of which is identical to the first oxidizer mixture.
  • the first fuel / oxidizer mixture is fed to a catalyst unit within which the fuel fraction contained in the first fuel / oxidizer mixture is catalytically oxidized.
  • the catalyst products are hydrogen (H 2 ) and essentially water vapor and carbon dioxide (C0 2 ).
  • the formation of hydrogen also contributes to a drastic increase in the reactivity of the fuel / oxidizer mixture, which has an advantageous effect on shortening the ignition period of the fuel / oxidizer mixture.
  • the method according to the invention thus provides for a combination of catalysis of a fuel-rich or rich fuel / oxidizer mixture with the formation of reactive hydrogen and subsequent combustion of an emaciated fuel / oxidizer mixture, for example by means of a conventional premix burner.
  • the catalyzed, first fuel / oxidizer mixture is emaciated by admixing the second oxidizer mixture provided, as a result of which the fuel fraction per volume fraction is reduced.
  • the ignition temperature of the catalytically oxidized fuel which is fed to a catalyst unit in the form of a rich fuel / oxidizer mixture, is significantly reduced.
  • the reduction in the ignition temperature and also a stabilization of the flame front which forms downstream of a premix burner within a combustion chamber can be attributed to the generation of hydrogen, which is formed by the catalytic oxidation of the fuel CH.
  • the feed means for the oxidizer mixture and the fuel supply unit are arranged in the area of the burner inlet in such a way that a largely complete intermixing between the gaseous fuel and the supplied oxidizer mixture is ensured.
  • a catalyst unit is provided in the area of the burner inlet downstream of the feed means and the fuel supply unit, through which the fuel / oxidizer mixture that forms flows.
  • At least one bypass line which bypasses or penetrates the catalyst unit is provided, which extends the area of the Connects the burner inlet upstream of the catalyst unit with the area of the burner inlet downstream of the catalyst unit. Only pure oxidizer mixture is passed through the at least one bypass line and is mixed downstream of the catalyst unit with the catalyzed fuel / oxidizer mixture for the purpose of deliberately reducing the fuel content.
  • the preparation of the oxidizer mixture is advantageously carried out using means known per se, by means of a recirculation line, a part of the exhaust gases emerging from the combustion chamber is introduced as carrier gas into an oxygen separation device from which the oxygen-enriched carrier gas exits and usually via a heat exchanger for feeding into the Burner entry according to EP 1 197 257 A1 is made available.
  • the oxidizer mixture is provided uniformly both for feeding into the bypass line to bypass the catalyst unit and for introducing it into the feed medium via which part of the oxidizer mixture is mixed with fuel and fed to the catalyst unit as a fuel / oxidizer mixture.
  • Fig. 1 is a schematic representation for the preparation of an ignitable
  • FIG. 2 shows an illustration of a catalytic converter unit with an upstream flow guide means
  • Fig. 3 shows an alternative embodiment of a catalyst unit as well
  • an oxygen separating device with an MCM membrane into which a part of the exhaust gas emerging from the combustion chamber is recirculated, and as an oxygen-enriched carrier stream via a preheating unit, the burner inlet as an oxidizer mixture is used to produce the carrier gas enriched with oxygen, that is to say the oxidizer mixture is fed again.
  • a device can be found, for example, in EP 1 197 257 A1.
  • a burner inlet 1 shown schematically in FIG. 1, of a gas turbine system, not shown, which is flowed through from the left to the right to form an ignitable fuel / oxidizer mixture and opens into the combustion chamber 9 in the right area. It is assumed that an oxidizer mixture is fed as a gaseous stream consisting of C0 2 , H 2 0 and 0 2 at a temperature T between 450 and 600 ° C. into the left inlet opening of the burner inlet 1.
  • a support structure 3 Downstream of the inlet area of the burner inlet 1, a support structure 3 is provided which has a plurality of through channels 4, 5 in the direction of flow, of which a group of flow channels 4 has a thin wall with a Catalyst material, for example Pt or Pd, are lined and the other group of through channels 5 consists of the material of the support structure itself, preferably of an inert material, for example Al0 3 , Si0 2 or ZrO.
  • an inert material for example Al0 3 , Si0 2 or ZrO.
  • a fuel supply unit 6 is provided in the flow area in front of the through-channels 4 lined with catalytic material, through which gaseous, fossil fuel, preferably methane (CH 4 ), is fed into the burner inlet to form a first fuel / oxidizer mixture 7.
  • gaseous, fossil fuel preferably methane (CH 4 )
  • CH 4 methane
  • a first partial flow from the side of the oxidizer mixture 2 provided by the oxygen separation device enters the inflow region of the gaseous fuel provided by the fuel supply unit to form the first fuel / oxidizer mixture 7.
  • the remaining portion of the oxidizer mixture 2 provided flows through the through channels 5 designed as bypass lines.
  • the first fuel / oxidizer mixture 7 which forms has a gas mixture consisting of oxygen, carbon dioxide, water and methane as fuel, the so-called oxygen number ⁇ i, which means the ratio of the actual oxygen supply to the minimum oxygen requirement for complete combustion, less than 1, is preferably 0.25.
  • This relatively fuel-rich or rich gas mixture comes into superficial contact with the catalyst material, for example rhodium (Rh), platinum (Pt), palladium (Pd) or nickel (Ni) within the catalyst unit, consisting of the through channels 4 lined with catalyst material. , whereby the fossil fuel gas is at least partially catalytically oxidized and chemically converted.
  • the chemical secondary products of the exothermic chemical reaction are hydrogen and carbon monoxide or carbon dioxide, whereby the process temperature within the catalyst unit rises to temperatures between 550 and 1000 ° C and the entire material flow, which passes through the catalyst unit and thus also the support structure 3, consisting of the the first fuel / oxidizer mixture and the second oxidizer mixture, which passes through the through channels 5, is heated accordingly.
  • the amount of heat released by the exothermic reaction and the resulting process temperature depend on the oxygen content within the fuel / oxidizer mixture and can be influenced by regulating the oxygen content.
  • the support structure 3 is preferably designed in the manner of a honeycomb body structure and interspersed with a plurality of parallel through-channels, of which, as stated, a first group 4 is lined with catalytic active material are.
  • a first group 4 is lined with catalytic active material are.
  • upper operating temperature limits are set which are in the range between 700 and 900 ° C., preferably 750 ° C. If these are exceeded due to the process, material degradation or detachment of the catalyst material from the corresponding support structure is to be expected, as a result of which the operating life of the catalyst unit is limited.
  • the ratios of the individual components of the chemically reacting fuel / oxidizer mixture within the catalyst unit ie fuel, oxygen, CO 2 and water, must be set in a targeted manner in order to achieve a desired cooling effect.
  • Passive cooling is also possible by selecting the volume fraction of the bypass lines passing through the support structure, within which no exothermic chemical reactions occur, as a result of which the oxidizer mixture flowing through the bypass lines or through channels 5 can be regarded as a cooling flow.
  • the catalyzed first fuel / oxidizer mixture arrives in a mixture with the pure oxidizer mixture fed through the through channels 5, as a result of which the volume fraction of the fuel within the second fuel which forms in the region 8 of the burner inlet 1 / oxidizer Mixture decreases, so that the second fuel / oxidizer mixture is much leaner than the first fuel / oxidizer mixture supplied to the catalyst unit.
  • the mixture of both material flows takes place so effectively and quickly that no ignition phenomena occur before complete mixing is achieved.
  • the aim of the rapid mixing downstream of the support structure 2 is to produce a completely and uniformly mixed, lean, catalyzed fuel / oxidizer mixture with an oxygen number ⁇ 2 > 1, which is ultimately burned within a combustion chamber 9 adjoining the burner inlet 2.
  • the combustion of the lean catalyzed fuel / oxidizer mixture typically takes place in the context of a premix burner which is conventional per se or in the context of a catalytic combustion.
  • a further catalyst unit 10 is provided before entry into the combustion chamber 9, by means of which the catalytic combustion is initiated.
  • the method according to the invention provides for a targeted generation of highly reactive hydrogen by means of a catalytic oxidation of fossil gaseous fuel in the context of a rich fuel / oxidizer mixture, by means of which the reactivity of the catalyzed fuel / oxidizer mixture which forms is considerably increased.
  • the actual combustion process of the catalyzed fuel / oxidizer mixture which is thinned by the additional admixture of an oxidizer mixture takes place through the presence of hydrogen with very short ignition delay times and at temperatures below 1250 ° C.
  • the ignition temperature and the lean extinguishing temperature within the combustion chamber can thus be significantly reduced by the targeted conversion of fossil fuel, preferably CH 4 into hydrogen and carbon monoxide or carbon dioxide / water vapor.
  • fossil fuel preferably CH 4 into hydrogen and carbon monoxide or carbon dioxide / water vapor.
  • FIG. 2 shows an exemplary embodiment of a support structure 3 which has a plurality of through channels which are arranged in columns and rows and have a rectangular cross section.
  • alternating arrangement through channels 4, which are lined with a catalyst material, and through channels 5 made of largely chemically inert material and designed as bypass lines are provided.
  • through channels 4 and 5 are lined with a catalyst material, and through channels 5 made of largely chemically inert material and designed as bypass lines.
  • the flow guide means 11 is directly gas-tight, firmly connected to the left front front of the support structure 3 facing in the direction of flow.
  • the fluid 11 has a fan arrangement which is adapted to the row arrangement of the passage channels 4 and 5 within the support structure 3 and which, in relation to the direction of flow through the passage channels 4 and 5 of the support structure 3, alternately provides laterally open entry side flanks 12, 13.
  • the first fuel / oxidizer mixture 7 is introduced along the inlet side flanks 12 of the flow guide 11, which is deflected by the otherwise trapezoidal design of the flow guide 11 in the direction of the passage channels 4 lined with catalyst material.
  • the flow deflection takes place row by row within the flow guide means 11, corresponding to the passage channels 4 arranged in rows. This ensures that only the fuel / oxidizer mixture 7 flows through the passage channels 4 lined with catalyst material.
  • the pure oxidizer mixture is supplied via the inlet side flanks 13 of the flow guide 11.
  • one closed side wall opposite the open inlet side flanks in each row plane in the inlet flow direction serves to block the respective flows in Deflect the direction of passage through the passage channels 4, 5.
  • the through channels 4, 5 are to be arranged as directly as possible next to one another and the cross-section is to be dimensioned as small as possible.
  • FIG. 3 an embodiment variant of the support structure 3 is provided, through which a particularly effective mixing of the material flows emerging from the through channels 4, 5 is effected.
  • the through-channels 4 lined with the catalyst material and the uncoated through-channels 5 are arranged in the manner of a checkerboard pattern.
  • the through-channels only provide rectangular cross-sections, but these can also have different cross-sectional shapes, such as hexagonal cross-sectional shapes.
  • a perforated plate 14 is provided between the flow guide 11, which is identical to that according to FIG.
  • the exemplary embodiment according to FIG. 4a shows a relatively large proportion of the area of through-channels 4 with catalyst material, especially since the through-channels 4 have four microchannels in the wall.
  • Such an arrangement involves high catalytic reaction fractions, which lead to an increased occurrence of exothermic reactions and ultimately to an increased production of hydrogen.
  • the cross-sectional arrangement according to FIG. 4b provides a larger proportion of through channels 5, along which the oxidizer mixture is fed. Such a cross-sectional arrangement is suitable for better cooling purposes.

Abstract

L'invention concerne un procédé et un dispositif d'utilisation d'un brûleur d'un moteur thermique, notamment d'un système de turbines à gaz, comportant une entrée de brûleur recevant un mélange de combustible et d'un gaz porteur enrichi en oxygène pour la combustion dans une chambre de combustion adjacente à l'entrée de brûleur dans le sens d'écoulement. Le procédé selon l'invention est caractérisé en ce qu'il consiste à se munir d'un premier flux de gaz porteur enrichi en oxygène, appelé premier mélange oxydant, auquel le combustible est mélangé de manière à former un premier mélange combustible/oxydant ; à se munir d'un deuxième flux de gaz porteur enrichi en oxygène, appelé deuxième mélange oxydant ; à catalyser le premier mélange combustible/oxydant de manière à former un premier mélange combustible/oxydant catalysé, dans lequel le combustible est au moins partiellement oxydé ; à mélanger le premier mélange combustible/oxydant catalysé avec le deuxième mélange oxydant afin de former un deuxième mélange combustible/oxydant ; et, à allumer et brûler le deuxième mélange combustible/oxydant.
EP03735236A 2003-04-24 2003-07-16 Procede et dispositif d'utilisation d'un bruleur d'un moteur thermique, notamment d'un systeme de turbines a gaz Withdrawn EP1616131A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10318669 2003-04-24
PCT/CH2003/000478 WO2004094909A1 (fr) 2003-04-24 2003-07-16 Procede et dispositif d'utilisation d'un bruleur d'un moteur thermique, notamment d'un systeme de turbines a gaz

Publications (1)

Publication Number Publication Date
EP1616131A1 true EP1616131A1 (fr) 2006-01-18

Family

ID=33304921

Family Applications (1)

Application Number Title Priority Date Filing Date
EP03735236A Withdrawn EP1616131A1 (fr) 2003-04-24 2003-07-16 Procede et dispositif d'utilisation d'un bruleur d'un moteur thermique, notamment d'un systeme de turbines a gaz

Country Status (5)

Country Link
US (1) US20060096297A1 (fr)
EP (1) EP1616131A1 (fr)
AU (1) AU2003236766A1 (fr)
NO (1) NO20055528L (fr)
WO (1) WO2004094909A1 (fr)

Families Citing this family (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20050189097A1 (en) * 2004-03-01 2005-09-01 The Boeing Company Formed sheet heat exchanger
DE102004041794A1 (de) * 2004-03-30 2005-10-20 Alstom Technology Ltd Baden Vorrichtung und Verfahren zur Flammenstabilisierung in einem Brenner
DE502005003324D1 (de) 2004-03-30 2008-04-30 Alstom Technology Ltd Vorrichtung und verfahren zur flammenstabilisierung in einem brenner
US7444820B2 (en) * 2004-10-20 2008-11-04 United Technologies Corporation Method and system for rich-lean catalytic combustion
JP2008534896A (ja) 2005-03-23 2008-08-28 アルストム テクノロジー リミテッド 前混合バーナにおいて水素を燃焼する方法と装置
SE529333C2 (sv) * 2005-11-23 2007-07-10 Norsk Hydro As Förbränningsinstallation
US8671658B2 (en) 2007-10-23 2014-03-18 Ener-Core Power, Inc. Oxidizing fuel
US8393160B2 (en) 2007-10-23 2013-03-12 Flex Power Generation, Inc. Managing leaks in a gas turbine system
US8701413B2 (en) 2008-12-08 2014-04-22 Ener-Core Power, Inc. Oxidizing fuel in multiple operating modes
US8621869B2 (en) 2009-05-01 2014-01-07 Ener-Core Power, Inc. Heating a reaction chamber
US8893468B2 (en) 2010-03-15 2014-11-25 Ener-Core Power, Inc. Processing fuel and water
US9057028B2 (en) 2011-05-25 2015-06-16 Ener-Core Power, Inc. Gasifier power plant and management of wastes
US9273606B2 (en) 2011-11-04 2016-03-01 Ener-Core Power, Inc. Controls for multi-combustor turbine
US9279364B2 (en) 2011-11-04 2016-03-08 Ener-Core Power, Inc. Multi-combustor turbine
US9347664B2 (en) 2012-03-09 2016-05-24 Ener-Core Power, Inc. Gradual oxidation with heat control
US8807989B2 (en) 2012-03-09 2014-08-19 Ener-Core Power, Inc. Staged gradual oxidation
US8926917B2 (en) 2012-03-09 2015-01-06 Ener-Core Power, Inc. Gradual oxidation with adiabatic temperature above flameout temperature
US8980192B2 (en) 2012-03-09 2015-03-17 Ener-Core Power, Inc. Gradual oxidation below flameout temperature
US9328916B2 (en) 2012-03-09 2016-05-03 Ener-Core Power, Inc. Gradual oxidation with heat control
US9234660B2 (en) 2012-03-09 2016-01-12 Ener-Core Power, Inc. Gradual oxidation with heat transfer
US9371993B2 (en) 2012-03-09 2016-06-21 Ener-Core Power, Inc. Gradual oxidation below flameout temperature
US9206980B2 (en) 2012-03-09 2015-12-08 Ener-Core Power, Inc. Gradual oxidation and autoignition temperature controls
US9017618B2 (en) 2012-03-09 2015-04-28 Ener-Core Power, Inc. Gradual oxidation with heat exchange media
US9328660B2 (en) 2012-03-09 2016-05-03 Ener-Core Power, Inc. Gradual oxidation and multiple flow paths
US9534780B2 (en) 2012-03-09 2017-01-03 Ener-Core Power, Inc. Hybrid gradual oxidation
US8980193B2 (en) 2012-03-09 2015-03-17 Ener-Core Power, Inc. Gradual oxidation and multiple flow paths
US9381484B2 (en) 2012-03-09 2016-07-05 Ener-Core Power, Inc. Gradual oxidation with adiabatic temperature above flameout temperature
US9353946B2 (en) 2012-03-09 2016-05-31 Ener-Core Power, Inc. Gradual oxidation with heat transfer
US8844473B2 (en) 2012-03-09 2014-09-30 Ener-Core Power, Inc. Gradual oxidation with reciprocating engine
US9267432B2 (en) 2012-03-09 2016-02-23 Ener-Core Power, Inc. Staged gradual oxidation
US9359947B2 (en) 2012-03-09 2016-06-07 Ener-Core Power, Inc. Gradual oxidation with heat control
US9726374B2 (en) 2012-03-09 2017-08-08 Ener-Core Power, Inc. Gradual oxidation with flue gas
US9273608B2 (en) 2012-03-09 2016-03-01 Ener-Core Power, Inc. Gradual oxidation and autoignition temperature controls
US9567903B2 (en) 2012-03-09 2017-02-14 Ener-Core Power, Inc. Gradual oxidation with heat transfer
US9359948B2 (en) 2012-03-09 2016-06-07 Ener-Core Power, Inc. Gradual oxidation with heat control
US8671917B2 (en) 2012-03-09 2014-03-18 Ener-Core Power, Inc. Gradual oxidation with reciprocating engine
CN103322581B (zh) * 2013-07-09 2015-07-15 魏伯卿 富氧催化助燃装置
GB2551134B (en) * 2016-06-06 2019-05-15 Energy Tech Institute Llp Heat exchanger

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4101287A (en) * 1977-01-21 1978-07-18 Exxon Research & Engineering Co. Combined heat exchanger reactor
GB9212794D0 (en) * 1992-06-16 1992-07-29 Ici Plc Catalytic combustion
US6339925B1 (en) * 1998-11-02 2002-01-22 General Electric Company Hybrid catalytic combustor
US6358040B1 (en) * 2000-03-17 2002-03-19 Precision Combustion, Inc. Method and apparatus for a fuel-rich catalytic reactor
EP1197257B1 (fr) 2000-10-13 2009-11-04 ALSTOM Technology Ltd Procédé et dispositif pour la production de gaz d'alimentation chaud
EP1197256A1 (fr) * 2000-10-13 2002-04-17 ALSTOM (Switzerland) Ltd Procédé et dispositif pour la production de gaz de combustion chaud
US6619043B2 (en) * 2001-09-27 2003-09-16 Siemens Westinghouse Power Corporation Catalyst support structure for use within catalytic combustors
CH695793A5 (de) * 2001-10-01 2006-08-31 Alstom Technology Ltd Verbrennungsverfahren, insbesondere für Verfahren zur Erzeugung von elektrischem Strom und/oder von Wärme.
NO321805B1 (no) * 2001-10-19 2006-07-03 Norsk Hydro As Fremgangsmate og anordning for a lede to gasser inn og ut av kanalene i en flerkanals monolittenhet.
US6829896B2 (en) * 2002-12-13 2004-12-14 Siemens Westinghouse Power Corporation Catalytic oxidation module for a gas turbine engine

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2004094909A1 *

Also Published As

Publication number Publication date
US20060096297A1 (en) 2006-05-11
AU2003236766A1 (en) 2004-11-19
NO20055528L (no) 2005-11-23
WO2004094909A1 (fr) 2004-11-04

Similar Documents

Publication Publication Date Title
WO2004094909A1 (fr) Procede et dispositif d'utilisation d'un bruleur d'un moteur thermique, notamment d'un systeme de turbines a gaz
EP1532400B1 (fr) Procede et dispositif pour faire bruler un melange combustible-oxydant
DE69913429T2 (de) Synthesegasreaktor mit keramischer Membran
EP1730441B1 (fr) Dispositif et procede pour stabiliser une flamme
WO2006100176A1 (fr) Procede et dispositif de combustion d'hydrogene dans un bruleur de premelange
WO2005095856A1 (fr) Reacteur catalytique et procede de combustion de melanges air-combustible a l'aide d'un reacteur catalytique
EP1378488B1 (fr) Dispositif de génération d'hydrogène
DE1964810C3 (de) Vorrichtung zur Gewinnung von Wasserstoff
DE2409950B2 (de) Verfahren zum Verbrennen von Kohlenwasserstoffbrennstoff
DE2232506C2 (de) Verfahren und Vorrichtung zur Erzeugung eines durch katalytische Umsetzung von Brennstoff und einem als Sauerstoffträger dienenden Gas zu bildenden Gasgemisches
WO2010020358A2 (fr) Cascade de réacteurs à plusieurs étages pour produire du gaz de synthèse sans formation de suie
EP1197256A1 (fr) Procédé et dispositif pour la production de gaz de combustion chaud
EP1963748B1 (fr) Chambre de combustion dotee d'un brûleur et procede d'exploitation correspondant
EP1446610A1 (fr) Procede de combustion destine notamment a un procede de production de courant electronique et/ou de chaleur
DE10057420A1 (de) Mehrstufiger Shiftreaktor und Reformeranlage
DE102020119619A1 (de) Düsencluster
DE102006019409B4 (de) Reformer-Reaktor, seine Verwendung und Verfahren zum Betrieb des Reformers
DE10243250A1 (de) Verfahren zum Erzeugen von Wasserdampf, insbesondere Reinstwasserdampf sowie Dampferzeuger
DE10007766A1 (de) Brenneranordnung
EP3246557A1 (fr) Système de propulsion d'une fusée et son procédé de fonctionnement
DE2708940A1 (de) Verfahren zum betreiben einer gasturbine sowie verbesserte gasturbinen- verbrennungskammer
DE19955892A1 (de) Verfahren und Vorrichtung zur Reformierung eines Kohlenwasserstoffs mit langkettigen Kohlenwasserstoffanteilen
EP1491824B1 (fr) Réacteur catalytique et procédé d'utilisation correspondant
EP3246558A1 (fr) Procédé de fonctionnement d'un système de propulsion de fusée et système de propulsion de fusée
DE102007027881B4 (de) Verfahren und Vorrichtung zur Mischung von Gasen

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20051012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LI LU MC NL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL LT LV MK

DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20130201