US20060096297A1 - Method and apparatus for operating a burner of a heat engine, in particular of a gas turbine installation - Google Patents

Method and apparatus for operating a burner of a heat engine, in particular of a gas turbine installation Download PDF

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Publication number
US20060096297A1
US20060096297A1 US11/256,113 US25611305A US2006096297A1 US 20060096297 A1 US20060096297 A1 US 20060096297A1 US 25611305 A US25611305 A US 25611305A US 2006096297 A1 US2006096297 A1 US 2006096297A1
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Prior art keywords
fuel
oxidizer mixture
oxygen
mixture
catalytic converter
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Abandoned
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US11/256,113
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English (en)
Inventor
Timothy Griffin
Dieter Winkler
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General Electric Technology GmbH
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Alstom Technology AG
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Assigned to ALSTOM TECHNOLOGY LTD reassignment ALSTOM TECHNOLOGY LTD ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GRIFFIN, TIMOTHY, WINKLER, DIETER
Publication of US20060096297A1 publication Critical patent/US20060096297A1/en
Abandoned legal-status Critical Current

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    • 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 an apparatus for operating a burner of a heat engine, in particular of a gas turbine installation, having a burner inlet, to which a mixture of a fuel and an oxygen-enriched carrier gas is fed for combustion within a combustion chamber which adjoins the burner inlet in the direction of flow.
  • gas turbine concept is based on the combustion of fossil fuels, in particular gaseous fuels, such as for example methane, in the presence of a mixture of recirculated exhaust gas, in which CO 2 , H 2 O and oxygen are used as oxidizing agents and not, as in conventional combustion processes, to form a fuel/air mixture which contains considerable quantities of nitrogen.
  • gaseous fuels such as for example methane
  • CO 2 , H 2 O and oxygen are used as oxidizing agents and not, as in conventional combustion processes, to form a fuel/air mixture which contains considerable quantities of nitrogen.
  • the CO 2 exhaust-gas stream is in part fed back to the gas turbine process as part of part-stream recirculation as CO 2 mass flow for the combustion, while the remaining residual exhaust-gas stream is taken for suitable utilization or is converted into compressed form for final land filling in suitable geological strata, which means that it is completely withdrawn from acting as a harmful greenhouse gas in the open atmosphere.
  • the oxidizer mixture obtained with the aid of the oxygen separation device is then mixed with gaseous fuel, preferably CH 4 , and, as a fuel/oxidizer mixture, ignited for combustion within the combustion chamber.
  • gaseous fuel preferably CH 4
  • the recirculated exhaust-gas stream which is to be enriched with oxygen, on the permeate side is passed through the oxygen separation device at a high flow rate along the MCM membrane, with the result that the oxygen concentration on the permeate side is reduced and the driving gradient between the retentate side, through which a preheated, oxygen-containing gas is flowing, and the permeate side is increased.
  • the oxygen enrichment the oxygen content within the oxygen-enriched carrier gas stream which emerges from the oxygen separation device is too low to achieve stable and effective combustion of the fuel/oxidizer mixture which forms with the aid of conventional combustion techniques.
  • the time-delayed ignition behavior also has a detrimental effect on the residence times required for complete combustion of the ignited fuel/oxidizer mixture within the combustion chamber, and moreover the CO and unburnt hydrocarbon contents which are formed during the combustion are well above the levels obtained with conventional combustion technology.
  • the reduced ignitability or reactivity of the fuel/oxidizer mixture also has a reducing action on the flame velocity, with the result that what are known as the lean extinction limits are reduced.
  • the catalyst material which is required for catalytic oxidation of the fuel typically platinum or palladium
  • support materials such as for example aluminum oxide, silicon oxide or zirconium oxide, which are or start to become unstable at such high temperatures with a steam content of greater than 50%.
  • the invention is based on the object of developing a method and an apparatus for operating a burner of a heat engine, in particular of a gas turbine installation, having a burner inlet, to which a mixture of a fuel and an oxygen-enriched carrier gas is fed for combustion within a combustion chamber which adjoins the burner inlet in the direction of flow, in such a manner that the drawbacks and technical difficulties which have been mentioned above in connection with the prior art can be avoided.
  • a first oxidizer mixture i.e. an oxygen-enriched carrier gas stream, which is obtained in a manner known per se, as mentioned above, is provided upstream of the burner inlet.
  • Fuel preferably gaseous fossil fuel, such as for example methane, is admixed with this first oxidizer mixture to form a first fuel/oxidizer mixture.
  • a second oxidizer mixture the composition of which is identical to that of the first oxidizer mixture, is likewise provided.
  • the first fuel/oxidizer mixture is fed to a catalytic converter unit, within which the fuel content contained in the first fuel/oxidizer mixture is at least partially catalytically oxidized.
  • the gaseous fossil fuel used is methane (CH 4 )
  • the catalyst products formed are hydrogen H 2 and substantially steam and carbon dioxide (CO 2 ).
  • the formation of hydrogen subsequently contributes to drastically increasing the reactivity of the fuel/oxidizer mixture, which has an advantageous effect in terms of shortening the ignition time of the fuel/oxidizer mixture.
  • first fuel/oxidizer mixture is ignited and burnt, it is mixed with the second oxidizer mixture which was initially provided, to form a second fuel/oxidizer mixture. Only after the second fuel/oxidizer mixture has formed is the latter ignited and burnt within the combustion chamber.
  • the method according to the invention therefore provides a combination of catalysis of a fuel-rich or rich fuel/oxidizer mixture to form reactive hydrogen and subsequent combustion of a lean fuel/oxidizer mixture, for example within a conventional premix burner.
  • the lean depletion of the catalyzed, first fuel/oxidizer mixture is effected by admixing the second oxidizer mixture which has been provided, with the result that the fuel content by volume is reduced.
  • the ignition temperature of the catalytically oxidized fuel which is fed to a catalytic converter unit in the form of a rich fuel/oxidizer mixture, is significantly reduced.
  • an apparatus for operating a burner of a heat engine, in particular of a gas turbine installation, having the features of the preamble of claim 10 is used to carry out the method according to the invention, which apparatus according to the invention is distinguished by the fact that at least one means for feeding in the oxidizer mixture and a fuel feed unit are provided in the region of the burner inlet.
  • the means for feeding in the oxidizer mixture and the fuel feed unit are arranged in the region of the burner inlet, in such a manner that substantially complete mixing between the gaseous fuel and the oxidizer mixture supplied is ensured.
  • a catalytic converter unit through which the fuel/oxidizer mixture which forms flows, is provided in the region of the burner inlet downstream of the means for feeding in oxidizer mixture and of the fuel feed unit.
  • at least one bypass line which bypasses or passes through the catalytic converter unit, connecting the region of the burner inlet upstream of the catalytic converter unit to the region of the burner inlet downstream of the catalytic converter unit.
  • Exclusively pure oxidizer mixture is passed through the at least one bypass line, and this pure oxidizer mixture, downstream of the catalytic converter unit, is admixed to the catalyzed fuel/oxidizer mixture for the purpose of targeted lean depletion of the fuel content.
  • the oxidizer mixture is advantageous for the oxidizer mixture to be produced using means which are known per se by some of the exhaust gases which emerge from the combustion chamber being introduced as carrier gas into an oxygen separation device by means of a recurculation line, with the oxygen-enriched carrier gas emerging from the oxygen separation device and being made available in the usual way via a heat exchanger in order to be introduced into the burner inlet, as described in EP 1 197 257 A1.
  • the oxidizer mixture is provided uniformly both for feeding into the bypass line in order to bypass the catalytic converter unit and for introduction into the means for feeding in oxidizer mixture, by which some of the oxidizer mixture is mixed with fuel and fed to the catalytic converter unit as fuel/oxidizer mixture.
  • FIG. 1 shows a diagrammatic illustration for preparing an ignitable fuel/oxidizer mixture using the method according to the invention
  • FIG. 2 illustrates a catalytic converter unit with a flow-guiding means arranged upstream
  • FIG. 3 shows an alternative form of a catalytic converter unit
  • FIG. 4 a - d show alternative embodiments of the catalytic converter unit in the form of cross-sectional illustrations.
  • an oxygen separation device with an MCM membrane into which some of the exhaust gas which emerges from the combustion chamber is recirculated and, as oxygen-enriched carrier stream, fed back to the burner inlet as oxidizer mixture via a preheating unit, is used to produce the oxygen-enriched carrier gas, i.e. the oxidizer mixture.
  • An apparatus of this type is described, for example, in EP 1 197 257 A1.
  • a burner inlet 1 which is diagrammatically depicted in FIG. 1 , of a gas turbine installation, which is not otherwise illustrated; medium flows through the burner inlet from the left-hand side to the right-hand side to form an ignitable fuel/oxidizer mixture, and in the region of the right-hand side the burner inlet opens out into the combustion chamber 9 . It will be assumed that an oxidizer mixture is fed into the left-hand inlet opening of the burner inlet 1 as a gaseous stream consisting of CO 2 , H 2 O and O 2 at a temperature T of between 450 and 600° C.
  • a support structure 3 Downstream of the inlet region of the burner inlet 1 , there is a support structure 3 which, as seen in the direction of flow, has a multiplicity of through-passages 4 , 5 , of which one group of flow passages 4 is lined in thin-walled form with a catalyst material, for example Pt or Pd, while the other group of through-passages 5 consists of the material of the support structure itself, preferably an inert material, for example AlO 3 , SiO 2 or ZrO.
  • a catalyst material for example Pt or Pd
  • a fuel feed unit 6 Immediately upstream of the catalytic converter unit 3 , in each case in the flow region ahead of the through-passages 4 lined with catalyst material, there is a fuel feed unit 6 , 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 part-stream passes from the oxidizer mixture 2 provided by the oxygen separation device into the inflow region of the gaseous fuel provided by the fuel feed unit, to form the first fuel/oxidizer mixture 7 .
  • the remaining part of the oxidizer mixture 2 which is provided flows through the through-passages 5 designed as bypass lines.
  • the first fuel/oxidizer mixture 7 which is formed includes a gas mixture consisting of oxygen, carbon dioxide, water and methane as fuel, the so-called oxygen ratio ⁇ 1 of which, i.e. the ratio of the actual oxygen supply to the minimum oxygen demand for complete combustion, is less than 1, preferably 0.25.
  • this relatively fuel-rich or rich gas mixture comes into surface contact with the catalyst material, for example rhodium (Rh), platinum (Pt), palladium (Pd) or nickel (Ni), with the result that the fossil fuel gas is at least partially catalytically oxidized and chemically converted.
  • Hydrogen and carbon monoxide or carbon dioxide are formed as chemical by-products of the exothermic chemical reactions, with the result that the process temperature within the catalytic converter unit rises to temperatures between 550 and 1000° C., and the entire stream of substance passing through the catalytic converter unit and therefore also the support structure 3 , consisting of the first fuel/oxidizer mixture and the second oxidizer mixture, which passes through the through-passages 5 , is correspondingly heated.
  • the heat quantity which is 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 controlling the oxygen content.
  • the support structure 3 is preferably designed in the form of a honeycomb structure with a multiplicity of parallel through-passages passing through it, a first group 4 of which, as has been stated, are lined with catalytically active material on the inner wall.
  • the support structure it is also possible for the support structure to be designed in other ways, for example in a simple case by forming a bundle of tubes.
  • the catalyzed first fuel/oxidizer mixture is mixed with the pure oxidizer mixture which has been supplied through the through-passages 5 , with the result that the volumetric content of the fuel within the second fuel/oxidizer mixture which forms in the region 8 of the burner inlet 1 decreases, so that the second fuel/oxidizer mixture is much leaner than the first fuel/oxidizer mixture fed to the catalytic converter unit.
  • the mixing of the two streams is so efficient and fast that no ignition phenomena occur before complete mixing has taken place.
  • the aim of rapid mixing downstream of the support structure 2 is to produce a complete, uniformly mixed, lean-depleted, catalyzed fuel/oxidizer mixture with an oxygen ratio ⁇ 2 >1, which is ultimately burnt within a combustion chamber 9 that adjoins the burner inlet 2 .
  • the combustion of the lean catalyzed fuel/oxidizer mixture is typically carried out within an inherently standard premix burner or as part of catalytic combustion.
  • a further catalytic converter unit 10 which initiates the catalytic combustion, is provided upstream of the entry to the combustion chamber 9 .
  • the method according to the invention provides for controlled generation of highly reactive hydrogen, which considerably increases the reactivity of the catalyzed fuel/oxidizer mixture which forms.
  • the actual combustion of the catalyzed fuel/oxidizer mixture which has been lean-depleted by the additional admixing of an oxidizer mixture is effected by the presence of hydrogen with very short ignition delay times and at temperatures of less than 1250° C.
  • the ignition temperature and the lean extinction temperature within the combustion chamber can be significantly reduced by the targeted conversion of fossil fuel, preferably CH 4 , into hydrogen and carbon monoxide or carbon dioxide/steam.
  • fossil fuel preferably CH 4
  • the method according to the invention for operating a burner it is possible to keep the exhaust-gas temperatures below those which would lead to destruction of all the components within the oxygen-enriching device.
  • FIG. 2 illustrates an exemplary embodiment for a support structure 3 , which has a multiplicity of through-passages which are arranged in rows and columns and are rectangular in cross section.
  • Through-passages 4 which are lined with a catalyst material on the inner wall
  • through-passages 5 which consist of chemically substantially inert material and are designed as bypass lines are provided in an arrangement of alternating rows.
  • the cross-sectional shape and arrangement of the respective through-passages 4 and 5 to be arranged and designed in an equivalent, alternative three-dimensional ordered pattern, for example in a honeycomb structure, a checkerboard arrangement or similar embodiments.
  • a flow-guiding means 11 which is connected upstream of the support structure 3 as seen in the direction of flow and is illustrated separately from the support structure 3 purely to provide a better view, is used to spatially separately supply the respective streams into the through-passages 4 and 5 , which have been divided into groups.
  • the flow-guiding means 11 is fixedly joined in a gastight manner directly to the left-hand front of the support structure 3 facing it as seen in the direction of flow.
  • the flow means 11 has an arrangement of compartments which is matched to the arrangement of the through-passages 4 and 5 in rows within the support structure 3 , with this arrangement of compartments providing inlet side flanks 12 , 13 which are open on alternate sides relative to the direction of flow through the through-passages 4 and 5 in the support structure 3 .
  • the first fuel/oxidizer mixture 7 is introduced along the inlet side flanks 12 of the flow-guiding means 11 and is diverted by the otherwise trapezoidal design of the flow-guiding means 11 toward the through-passages 4 lined with catalyst material.
  • fuel and oxidizer mixture it is also possible for fuel and oxidizer mixture to be supplied separately through the inlet side flanks 12 of the flow-guiding means 11 . In this case, the mixing of fuel and oxidizer mixture takes place within the flow-guiding means 11 , which in the interior provides suitable means for initiating flow turbulence to achieve intimate mixing.
  • the flow diversion in each case takes place in rows within the flow-guiding means 11 , corresponding to the arrangement of the through-passages 4 in rows. This ensures that only the fuel/oxidizer mixture 7 flows through the through-passages 4 lined with catalyst material.
  • the pure oxidizer mixture is supplied in the same way via the inlet side flanks 13 of the flow-guiding means 11 .
  • the flow of the respective streams which enter via the inlet side flanks 12 , 13 is in each case diverted by a closed side wall, which lies opposite the open inlet side flanks in each row plane in the direction of incoming flow and diverts the respective streams into the direction of passage through the through-passages 4 , 5 .
  • the through-passages 4 , 5 are to be arranged as closely adjacent to one another as possible and are to be provided with the minimum possible dimensions in cross section. Therefore, during mixing, it is appropriate to select the mixing length to be as short as possible, i.e. complete mixing of the streams which emerge from the through-passages 4 , 5 should take place as close as possible to the emergence of the flow from the support structure 3 .
  • FIG. 3 provides a variant embodiment of the support structure 3 , which produces particularly effective mixing of the streams which emerge from the through-passages 4 , 5 .
  • the through-passages 4 which are lined with the catalyst material on the inner wall and the uncoated through-passages 5 are arranged in a checkerboard pattern.
  • the through-passages only provide rectangular cross sections, these cross sections may also adopt different shapes, such as for example hexagonal shapes.
  • a perforated plate 14 which has passage openings 15 corresponding to the respective through-passages 4 , 5 , is provided between the flow-guiding means 11 , which is designed identically to that shown in FIG.
  • the perforated plate 14 ensures targeted supply of the fuel/oxidizer mixture exclusively through the through-passages 4 lined with catalyst material, and the same correspondingly also applies to the supply of the pure oxidizer mixture to be fed through the through-passages 5 .
  • the components illustrated in FIG. 3 comprising flow-guiding means 11 , perforated plate 14 and support structure 3 , are illustrated separately from one another purely to improve the clarity of the illustration. In a practical embodiment, the three components are joined to one another in a gastight manner, which ensures the desired supply of substance flow through the respective through-passages 4 , 5 .
  • FIGS. 4 a - d illustrate details from cross sections through the support structure 3 which show regions of through-passages 4 lined with catalyst material on the inner wall and through-passages 5 whose passage walls consist solely of the material of the support structure 3 itself, and in this respect have no catalytic effect on the stream passing through the through-passages 5 .
  • the level of the catalyzing reactions and the associated release of exothermic energy within the support structure 3 can be influenced by suitable selection of the ratio between the catalyzing surface area and the inert surface areas along the through-passages.
  • the exemplary embodiment shown in FIG. 4 a shows a relatively large proportion of the area being formed by through-passages 4 with catalyst material, particularly since the through-passages 4 have four micro-passages on the inner wall.
  • An arrangement of this type produces high catalytic reaction levels, which lead to increased exothermic reactions and ultimately to increased production of hydrogen.
  • the cross-sectional arrangement shown in FIG. 4 b provides a greater proportion of through-passages 5 along which the oxidizer mixture is supplied.
  • a cross-sectional arrangement of this type is suitable for improving the cooling.
  • the method according to the invention allows stable combustion of a gaseous fossil fuel using the AZEP principle, forming exclusively CO 2 and water.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
US11/256,113 2003-04-24 2005-10-24 Method and apparatus for operating a burner of a heat engine, in particular of a gas turbine installation Abandoned US20060096297A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10318669 2003-04-24
DE10318669.7 2003-04-24
PCT/CH2003/000478 WO2004094909A1 (de) 2003-04-24 2003-07-16 Verfahren und vorrichtung zum betreiben eines brenners einer wärmekraftmaschine, insbesondere einer gasturbinenanlage

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/CH2003/000478 Continuation WO2004094909A1 (de) 2003-04-24 2003-07-16 Verfahren und vorrichtung zum betreiben eines brenners einer wärmekraftmaschine, insbesondere einer gasturbinenanlage

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US20060096297A1 true US20060096297A1 (en) 2006-05-11

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US11/256,113 Abandoned US20060096297A1 (en) 2003-04-24 2005-10-24 Method and apparatus for operating a burner of a heat engine, in particular of a gas turbine installation

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US (1) US20060096297A1 (de)
EP (1) EP1616131A1 (de)
AU (1) AU2003236766A1 (de)
NO (1) NO20055528L (de)
WO (1) WO2004094909A1 (de)

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US8393160B2 (en) 2007-10-23 2013-03-12 Flex Power Generation, Inc. Managing leaks in a gas turbine system
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US8621869B2 (en) 2009-05-01 2014-01-07 Ener-Core Power, Inc. Heating a reaction chamber
US8671658B2 (en) 2007-10-23 2014-03-18 Ener-Core Power, Inc. Oxidizing fuel
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US8701413B2 (en) 2008-12-08 2014-04-22 Ener-Core Power, Inc. Oxidizing fuel in multiple operating modes
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US8980192B2 (en) 2012-03-09 2015-03-17 Ener-Core Power, Inc. Gradual oxidation below flameout temperature
US9017618B2 (en) 2012-03-09 2015-04-28 Ener-Core Power, Inc. Gradual oxidation with heat exchange media
US9057028B2 (en) 2011-05-25 2015-06-16 Ener-Core Power, Inc. Gasifier power plant and management of wastes
US9206980B2 (en) 2012-03-09 2015-12-08 Ener-Core Power, Inc. Gradual oxidation and autoignition temperature controls
US9234660B2 (en) 2012-03-09 2016-01-12 Ener-Core Power, Inc. Gradual oxidation with heat transfer
US9267432B2 (en) 2012-03-09 2016-02-23 Ener-Core Power, Inc. Staged gradual oxidation
US9273606B2 (en) 2011-11-04 2016-03-01 Ener-Core Power, Inc. Controls for multi-combustor turbine
US9273608B2 (en) 2012-03-09 2016-03-01 Ener-Core Power, Inc. Gradual oxidation and autoignition temperature controls
US9279364B2 (en) 2011-11-04 2016-03-08 Ener-Core Power, Inc. Multi-combustor turbine
US9328660B2 (en) 2012-03-09 2016-05-03 Ener-Core Power, Inc. Gradual oxidation and multiple flow paths
US9328916B2 (en) 2012-03-09 2016-05-03 Ener-Core Power, Inc. Gradual oxidation with heat control
US9347664B2 (en) 2012-03-09 2016-05-24 Ener-Core Power, Inc. Gradual oxidation with heat control
US9353946B2 (en) 2012-03-09 2016-05-31 Ener-Core Power, Inc. Gradual oxidation with heat transfer
US9359947B2 (en) 2012-03-09 2016-06-07 Ener-Core Power, Inc. Gradual oxidation with heat control
US9359948B2 (en) 2012-03-09 2016-06-07 Ener-Core Power, Inc. Gradual oxidation with heat control
US9371993B2 (en) 2012-03-09 2016-06-21 Ener-Core Power, Inc. Gradual oxidation below flameout temperature
US9381484B2 (en) 2012-03-09 2016-07-05 Ener-Core Power, Inc. Gradual oxidation with adiabatic temperature above flameout temperature
US9534780B2 (en) 2012-03-09 2017-01-03 Ener-Core Power, Inc. Hybrid gradual oxidation
US9567903B2 (en) 2012-03-09 2017-02-14 Ener-Core Power, Inc. Gradual oxidation with heat transfer
US9726374B2 (en) 2012-03-09 2017-08-08 Ener-Core Power, Inc. Gradual oxidation with flue gas

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EP1616131A1 (de) 2006-01-18
NO20055528L (no) 2005-11-23

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