EP1828679B1 - Verbrennungsverfahren mit zyklischer oxidationsmittelzufuhr - Google Patents

Verbrennungsverfahren mit zyklischer oxidationsmittelzufuhr Download PDF

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Publication number
EP1828679B1
EP1828679B1 EP05824047A EP05824047A EP1828679B1 EP 1828679 B1 EP1828679 B1 EP 1828679B1 EP 05824047 A EP05824047 A EP 05824047A EP 05824047 A EP05824047 A EP 05824047A EP 1828679 B1 EP1828679 B1 EP 1828679B1
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EP
European Patent Office
Prior art keywords
oxidant
injectors
sub
fuel
burner
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Not-in-force
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EP05824047A
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English (en)
French (fr)
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EP1828679A1 (de
Inventor
Rémi Tsiava
Benoit Grand
Patrick Recourt
Bertrand Leroux
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Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/20—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone
    • F23D14/22—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
    • 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 
    • F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
    • F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
    • F23C6/045—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection with staged combustion in a single enclosure
    • 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 
    • F23C7/00—Combustion apparatus characterised by arrangements for air supply
    • F23C7/02—Disposition of air supply not passing through burner
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/32—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid using a mixture of gaseous fuel and pure oxygen or oxygen-enriched air
    • 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
    • F23C2900/06041—Staged supply of oxidant

Definitions

  • the present invention relates to a combustion process for an industrial furnace.
  • the distribution of the heating power over a given furnace surface, the reduction of the quantity of nitrogen oxides produced and the stability of the combustion flame (s) generated in the furnace are among the principal stakes in the technology of combustion furnaces.
  • the surface to be heated can be large. This is usually the top surface of a feed of raw materials or melt contained in a tank. It is then difficult to distribute the heating power delivered by the flame (s) of combustion in a substantially uniform manner over the entire surface, so as to avoid the formation of colder zones which would be harmful vis-à- screw of the melt or the subsequent process of treating it.
  • the amount of nitrogen oxides (NO x) produced in a combustion flame depends on the local concentrations of oxygen and nitrogen, denoted [O 2] and [N 2].
  • an evaluation of the quantity of thermally produced nitric oxide (denoted [NO] th ) is given by the following formula: where k is a numerical constant, exp is the exponential function, E a is a positive activation energy, R is the ideal gas constant and T is the local temperature.
  • Another way to achieve further reduction in the amount of nitrogen oxides produced is to inject a major portion of the oxidant and the fuel at two locations in the furnace separated from each other by a relatively large distance. A combustion performed under these conditions is called “staged” (see for example EP 0 748 981 or WO 02/081967 ). A small portion of the oxidant is further injected near the fuel outlet to stabilize the combustion regime. The main part of the oxidant and the fuel are then gradually mixed in a spread volume where the jets overlap. In this way, a gap effect is still obtained between the ratio of the local concentrations of fuel and oxidizer on the one hand, and the stoichiometry of the combustion reaction on the other hand.
  • An object of the present invention is therefore to provide a combustion process which does not have the disadvantages mentioned above, or for which these disadvantages are reduced.
  • An oxidizer feed system cyclically distributes a determined flow rate of oxidizing between at least the second and third injectors of the two burner units.
  • the burner assemblies are substantially horizontal, the flame produced in the furnace is itself contained in a horizontal plane. In this way, the heat generated by the flame is efficiently transferred to the furnace charge without excessively heating a vault structure disposed above the furnace at a particular location thereof. Premature wear of the arch structure is thus avoided.
  • the oxidant is thus introduced into the oven at three points for each of the two burner units.
  • the first point of introduction of the oxidant is constituted by the first injector, which is the closest to the corresponding fuel injector. It allows to generate a first incomplete combustion of the fuel, which is then completed by the oxidant introduced by the second and third injectors.
  • the first injector also generally stabilizes the combustion regime at its output.
  • the third point of introduction of the oxidant is the farthest from the fuel injector, and the second oxidizer injector is located at a distance from the intermediate fuel injector between the distances of the first and third injectors .
  • the oxidant preferably has an oxygen content greater than 30% by volume, and even greater than 70% by volume.
  • the total flow rate of oxidant introduced into the furnace is distributed between the first, second and third injectors of the two burner units. A determined part of this total flow is injected by the second and third oxidizer injectors, with a distribution between at least some of these which is variable cyclically.
  • the determined part of the total flow rate of oxidant which is injected by the two second and the two third oxidizer injectors is substantially constant. It may possibly vary, but much more slowly than those of the individual flows of the second and / or third oxidizer injectors which are variable.
  • a specific fraction of the oxidant is injected into the furnace by some of the second and / or third injectors at a given instant, then is injected by the other second and / or third injectors at a later time.
  • the oxidant injection obtained by a device according to the invention is therefore alternated between some of said second and / or third injectors.
  • the cyclic distribution of the oxidant flow rate between some of the second and third injectors of the two burner units is preferably carried out at a frequency of less than 1 hertz.
  • the oscillation period of the flame in the oven is then greater than 1 second. The inventors have observed that such conditions provide a particularly stable combustion.
  • the fuel and the oxidant that are introduced into the furnace are diluted by recirculation of the exhaust gas in the combustion zone.
  • a main part of the oxidant is introduced into the furnace at a great distance from the fuel introduction locations.
  • the oxidant is strongly diluted with ambient gases present in the furnace before entering the main combustion zone.
  • the part of oxidant that is introduced near the fuel is called primary flow, and that which is introduced at a distance from the fuel is called secondary flow.
  • the oxidizer supply system feeds the first injectors respectively of each burner assembly with respective primary oxidant flow rates at each instant.
  • Each burner assembly generates a flame in the furnace, but when the two burner units are not too far apart, their respective flames are united and form a single combustion volume.
  • a single flame is obtained, in particular, when the distance between the respective fuel injectors of the two burner units is less than 30 times the diameter of each fuel injector.
  • flame generally denote by flame the total volume in which combustion occurs, it being understood that this volume can be divided into two parts for a significant separation distance between the two burner units.
  • the cyclic variations in the distribution of the oxidant flow between at least some of the second and third injectors cause a horizontal displacement of the flame in the furnace.
  • the displacement of the flame consists of a flapping thereof between two positions or in an oscillation of the flame between two configurations.
  • the cyclic variations of the distribution of the gases in the furnace improve the stability of the flame, especially in the vertical direction, by moving the flame alternately in a substantially horizontal direction.
  • the displacement of the flame contributes to further improving the distribution of the heating power throughout the volume of the furnace: a heat transfer to the load of the furnace is obtained, which is more uniform thanks to an effect of average in the time of the thermal contributions taking place at each point of the furnace.
  • the invention also provides an oven adapted to implement a method as described above.
  • the figure 1 represents a vertical wall 101 of a furnace 100, for example a melting furnace of raw materials.
  • the furnace 100 may be batch-operated, with separate stages of loading, heating and discharging of the furnace, or continuous operation, with permanent flows of raw material loading and melt output.
  • F denotes the trace of the free surface of material charged to the wall 101 of the oven.
  • the fuel and oxidizer injectors are disposed on the wall 101, with respective directions of fluid outlet substantially horizontal. They are aligned on a horizontal line located at a height h above the trace F. h is preferably between 250 mm (millimeters) and 550 mm.
  • the injectors 10 G , 1 G , 2 G and 3 G form a first burner assembly, associated with the left part of the wall 101.
  • this burner assembly is designated G in the following.
  • the injectors 10D , 1D , 2D and 3D form a second burner assembly, designated D and associated with the right portion of the wall 101.
  • the fuel introduced into the furnace 100 by the injectors 10G and 10D can be gaseous or liquid.
  • the injectors 10 and G 10 D each incorporate a spray nozzle so as to produce jets of fuel droplets.
  • the distance d 10 between the fuel injector of each burner assembly, 10 G or 10 D, and the median plane P is less than 15 times the diameter of each injector 10 or G 10 D, denoted ⁇ 10. Under these conditions, a single flame common to the two burner units G and D is generated in the oven 100.
  • the oxidant introduced by the injectors 1G , 2G , 3G , 1D , 2D and 3D is a gas usually having an oxygen content greater than 70% by volume.
  • the third oxidizer injector of each burner assembly is located at a distance from the fuel injector of said assembly at least ten times greater than the output diameter of the third injector.
  • d 3 -d 10 > 10. ⁇ 3 , where ⁇ 3 denotes the exit diameter of injectors 3 G and 3 D.
  • ⁇ 3 denotes the exit diameter of injectors 3 G and 3 D.
  • All the injectors of each burner assembly are directed substantially horizontally, so that the flame produced is parallel to the surface of the melt bath contained in the furnace 100.
  • the oxidizer supply system supplies each of the first injectors respectively of each burner assembly, that is to say the injectors 1G and 1D , with a respective primary flow of constant oxidant.
  • the oxidizer feed system is then simplified, as regards the feeding of injectors 1G and 1D .
  • x G and x D each correspond to 10% of the total flow rate of oxidant injected into each burner assembly.
  • the oxidant flow rates of two injectors arranged symmetrically with respect to the median plane P are equal at each instant.
  • the oxidizer supply system feeds the second injectors respectively of each burner assembly with respective secondary flows of oxidant substantially equal at each instant, and feeds the third injectors respectively of each burner assembly with respective tertiary flows of oxidant substantially equal every moment.
  • the supply system of injectors 2G , 2D , 3G and 3D may comprise two identical distribution boxes respectively assigned to each burner assembly G and D. These distribution boxes are coupled to a common control member variable, and each box has a movable partition wall of oxidant flows directed respectively to the second or the third injector.
  • the flame obtained is then centered on the median plane P and is symmetrical with respect thereto at each instant.
  • the figure 2a illustrates an example of variation of the rates y G and y D on the one hand, and rates z G and z D on the other hand.
  • the abscissa axis represents the time, indicated in seconds, and the ordinate axis represents the fraction of the oxidizer flow rate of each burner assembly that is introduced by each injector thereof. It is assumed that the total oxidant flow rate of each burner assembly G or D is constant, and that x G and x D are also constant and are each equal to 10% of the flow rate of the corresponding burner assembly.
  • the mixing volume is greater in state 1 than in state 2.
  • state 1 corresponds to an extended flame, both in width and in length
  • state 2 corresponds to a narrower and shorter flame .
  • the flow introduced into the furnace by each oxidizer injector is indicated on the figure 2b .
  • state 1 the fuel and the oxidant are more diluted within the flame.
  • the temperature is then lower, but a better coverage of the entire surface of the material is obtained.
  • the heat transfer of the flame to the furnace charge is then particularly homogeneous. Conversely, the flame is more concentrated and intense in state 2.
  • This second mode corresponds to an alternating oxidant feed between the two burner units. More particularly, the oxidizer feed system cyclically distributes a determined tertiary total flow of oxidant between said third injectors of the two burner units.
  • the oxidizer supply system can further supply each of the second injectors respectively of each burner assembly with a respective secondary flow of constant oxidant.
  • a particularly simple implementation of the alternate supply of oxidant is thus obtained.
  • the secondary flows of oxidant may be substantially equal.
  • x and y are respectively called primary and secondary total flows of the oxidant.
  • the tertiary total oxidant flow rate that is to say the oxidant flow rate introduced by the injectors 3 G and 3 D , is noted.
  • x and y are substantially constant or vary much more slowly than the individual cyclically varying flow rates of injectors.
  • the oxidizer feed system may be a distribution box connected to the injectors 3 G and 3 D , which has a movable partition wall disposed between the oxidant flows directed respectively to the injectors 3 G and 3 D.
  • the y-axis of the figure 3b is expressed as a percentage of the total flow rate of oxidant introduced into the furnace, that is to say x + y + z.
  • z G and z D each vary between 10% and 65%. The period of flow variations is still 2 seconds.
  • the mixing volume and the flame have symmetrical configurations between the preceding states 1 and 2 ( figure 3b ).
  • the flame is moved to the side of the 3 G or 3 D injector having the largest oxidant flow rate.
  • the flame is moved to the left side in state 1, and to the right side in state 2.
  • This lateral reciprocation of the flame stabilizes the height thereof, so that the flame remains at a substantially constant distance from the free surface of material charged on the one hand, and at a substantially constant distance from the vault of the oven on the other hand.
  • the lateral back and forth of the flame provides a sufficient heat transfer uniformly between the flame and the furnace charge in a horizontal direction parallel to the wall 101.
  • the flame is longer on the side of the injector 3 G or 3 D having the instantaneous flow rate of the highest oxidant.
  • a good average coverage of the furnace surface by the flame results.
  • the oxidant is expelled by injectors 3 G and 3 D with a speed of between 20 ms -1 (meter per second) and 160 ms -1 , for example 90 ms -1 .
  • the average fuel and oxidant mixing distance, as well as the average distance at which the combustion occurs, located from the wall 101 of the furnace are all the greater the greater the speed of expulsion of the furnace.
  • oxidizer by injectors 3 G and 3 D is high.
  • the high flow rate of the oxidant introduced by one of the two injectors 3 G or 3 D causes a significant dilution of the fuel on the side of the median plane P which corresponds to this injector.
  • the fuel is more concentrated in a zone of the flame offset from the median plane P on the side of the injector 3 G or 3 D which has the instantaneous flow rate of the weakest oxidant.
  • This area is marked A on the figure 3b , for the flame edges 200 corresponding to each of the two states 1 and 2.
  • the zone A moves at each alternation between two symmetrical positions located on either side of the median plane P.
  • zone A corresponds to the part of the flame that contributes the most to the heat transfer to the load at every moment.
  • a zone A inside the flame may be favorable or harmful to the material that is being melted, in particular as a function of the chemical behavior of this material when the temperature is not uniform.
  • a fuel supply system can cyclically distribute a determined total flow of fuel between the fuel injectors of the two burner units.
  • the fuel supply system is coupled to the oxidizer supply system so that the total fuel flow is cyclically distributed between the fuel injectors of the two burner assemblies in phase or in phase opposition with respect to the distribution. cyclic tertiary total flow of oxidizer between the third injectors of the two burner units.
  • another distribution box may be disposed at the inlet of injectors 10G and 10D .
  • This other distribution box has a movable separation wall arranged between the fuel flows directed respectively to the injectors 10G and 10D .
  • the two distribution boxes, connected to the injectors 3 G and 3 D for the first, and the injectors 10 G and 10 D for the second, can then be controlled synchronously in opposition of phase: the fuel flow rate sent into the one of the two injectors 10 G or 10 D is maximum or minimum at the same time that the flow of oxidizer sent into the injector 3 D or 3 G on the opposite side is also maximum or minimum.
  • a reinforcement of the zone A is thus obtained, which causes an increase in the brightness of the flame near the exit of the fuel injector 10G or 10D when the fuel flow therein is maximum.
  • the fuel concentration is depleted on the side of the 3 G or 3 D injector for which the oxidizer flow rate is maximum. This increased depletion causes a shortening of the flame to its furthest point of the injectors.
  • the two distribution boxes can be controlled synchronously in phase.
  • the flow rate of fuel sent into one of the two injectors 10 G or 10 D is then maximum or minimum at the same time as the oxidizer flow rate sent into the injector 3 G or 3 D of the same side is also maximum or minimum.
  • Zone A is then blurred and can be confused with the entire extent of the flame. It then oscillates between the two left and right sides with a greater amplitude of transverse displacement. At the same time, the flame is lengthened so that the two effects are combined to obtain an optimal scanning of the entire furnace surface by the flame. This results in an average heat transfer area with a particularly large load.
  • FIG. 1 Flame boundaries obtained when the distribution of fuel flows varies with the distribution of oxidizer flows are shown in Table 1. figure 4 .
  • the traces 200a and 200b respectively correspond to variations in phase opposition and in phase.
  • the trace 200 corresponds to a constant distribution of the fuel flow, and balanced between the two injectors 10 G and 10 D. It is represented in dotted lines for comparison.
  • the traces 200, 200a and 200b all correspond to the total flows of fuel and oxidant identical. For the sake of clarity of figure 4 only the contour of the flame in state 1 defined above is represented for each case.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Combustion Of Fluid Fuel (AREA)
  • Liquid Carbonaceous Fuels (AREA)

Claims (12)

  1. Verbrennungsverfahren, wobei zwei Brennergesamtheiten (G, D) im Wesentlichen horizontal, zueinander parallel und in Bezug auf eine zwischen den zwei Gesamtheiten verlaufende Mittelebene (P) symmetrisch angeordnet sind, wobei jede Brennergesamtheit enthält:
    - eine Brennstoff-Einspritzeinrichtung (10G, 10D) ;
    - erste (1G, 1D), zweite (2G, 2D) und dritte (3G, 3D) Sauerstoffträger-Einspritzeinrichtungen, die in zunehmenden Abständen von der jeweiligen Brennstoff-Einspritzeinrichtung (10G, 10D) angeordnet sind,
    und wobei ein Sauerstoffträger-Versorgungssystem einen bestimmten Sauerstoffträger-Durchsatz wenigstens zwischen Bestimmten der zweiten und dritten Einspritzeinrichtungen (2G, 2D, 3G, 3D) der zwei Brennergesamtheiten zyklisch verteilt.
  2. Verfahren nach Anspruch 1, wobei die zyklische Verteilung des Sauerstoffträger-Durchsatzes zwischen Bestimmten der zweiten und dritten Einspritzeinrichtungen (2G, 2D, 3G, 3D) der zwei Brennergesamtheiten mit einer Frequenz von weniger als 1 Hertz erfolgt.
  3. Verfahren nach Anspruch 1 oder 2, wobei ein Abstand zwischen den jeweiligen Brennstoff-Einspritzeinrichtungen (10G, 10D) der zwei Brennergesamtheiten kleiner als der 30-fache Durchmesser (Φ10) jeder Brennstoff-Einspritzeinrichtung ist.
  4. Verfahren nach einem der Ansprüche 1 bis 3, wobei der Sauerstoffträger einen Sauerstoffgehalt von mehr als 30 Vol.-% hat.
  5. Verfahren nach einem der Ansprüche 1 bis 4, wobei sich die dritte Sauerstoffträger-Einspritzeinrichtung (3G, 3D) jeder Brennergesamtheit in einem Abstand von der Brennstoff-Einspritzeinrichtung (10G, 10D) dieser Brennergesamtheit befindet, der wenigstens zehnmal größer als der Auslassdurchmesser (Φ3) der dritten Einspritzeinrichtung ist.
  6. Verfahren nach einem der Ansprüche 1 bis 5, wobei das Sauerstoffträger-Versorgungssystem jede der ersten Einspritzeinrichtungen (1G, 1D) jeder Brennergesamtheit mit einem jeweils konstanten Sauerstoffträger-Primärdurchsatz (xG, xD) versorgt.
  7. Verfahren nach einem der Ansprüche 1 bis 6, wobei das Sauerstoffträger-Versorgungssystem die jeweiligen ersten Einspritzeinrichtungen (1G, 1D) jeder Brennergesamtheit mit jeweiligen Sauerstoffträger-Primärdurchsätzen (xG, xD) versorgt, die zu jedem Zeitpunkt im Wesentlichen gleich sind.
  8. Verfahren nach einem der Ansprüche 1 bis 7, wobei das Sauerstoffträger-Versorgungssystem die jeweiligen zweiten Einspritzeinrichtungen (2G, 2D) jeder Brennergesamtheit mit jeweiligen sekundären Sauerstoffträger-Durchsätzen (yG, yD) versorgt, die zu jedem Zeitpunkt im Wesentlichen gleich sind, und die jeweiligen dritten Einspritzeinrichtungen (3G, 3D) jeder Brennergesamtheit mit jeweiligen tertiären Sauerstoffträger-Durchsätzen (zG, zD) versorgt, die zu jedem Zeitpunkt im Wesentlichen gleich sind.
  9. Verfahren nach einem der Ansprüche 1 bis 7, wobei das Sauerstoffträger-Versorgungssystem einen bestimmten tertiären Gesamt-Sauerstoffträger-Durchsatz zwischen den dritten Einspritzeinrichtungen (3G, 3D) der zwei Brennergesamtheiten zyklisch verteilt.
  10. Verfahren nach Anspruch 9, wobei das Sauerstoffträger-Versorgungssystem jede der jeweiligen zweiten Einspritzeinrichtungen (2G, 2D) jeder Brennergesamtheit mit einem jeweiligen konstanten sekundären Sauerstoffträger-Durchsatz (yG, yD) versorgt.
  11. Verfahren nach Anspruch 9 oder 10, wobei ein Brennstoffversorgungssystem einen bestimmten Gesamt-Brennstoffdurchsatz zwischen den Brennstoff-Einspritzeinrichtungen (10G, 10D) der zwei Brennergesamtheiten zyklisch verteilt.
  12. Verfahren nach Anspruch 11, wobei das Brennstoffversorgungssystem mit dem Sauerstoffträger-Versorgungssystem in der Weise gekoppelt ist, dass der Gesamt-Brennstoffdurchsatz zwischen den Brennstoff-Einspritzeinrichtungen (10G, 10D) der zwei Brennergesamtheiten mit gleicher Phase oder mit entgegengesetzter Phase in Bezug auf die zyklische Verteilung des tertiären Gesamt-Sauerstoffträger-Durchsatzes zwischen den dritten Einspritzeinrichtungen (3G, 3D) der zwei Brennergesamtheiten zyklisch verteilt wird.
EP05824047A 2004-12-13 2005-12-05 Verbrennungsverfahren mit zyklischer oxidationsmittelzufuhr Not-in-force EP1828679B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0452949A FR2879283B1 (fr) 2004-12-13 2004-12-13 Procede de combustion avec alimentation cyclique du comburant
PCT/FR2005/051033 WO2006064144A1 (fr) 2004-12-13 2005-12-05 Procede de combustion avec alimentation cyclique du comburant

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EP1828679A1 EP1828679A1 (de) 2007-09-05
EP1828679B1 true EP1828679B1 (de) 2008-04-23

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US (1) US8231380B2 (de)
EP (1) EP1828679B1 (de)
JP (1) JP4913747B2 (de)
AT (1) ATE393359T1 (de)
DE (1) DE602005006321T2 (de)
FR (1) FR2879283B1 (de)
WO (1) WO2006064144A1 (de)

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JP5451455B2 (ja) 2010-03-01 2014-03-26 大陽日酸株式会社 バーナの燃焼方法
DE102010053068A1 (de) * 2010-12-01 2012-06-06 Linde Ag Verfahren und Vorrichtung zur verdünnten Verbrennung
CN104532063B (zh) * 2014-12-09 2016-09-14 抚顺特殊钢股份有限公司 以高Al、Ti返回料为原材料冶炼低碳超纯净镍基合金的方法

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FR2823290B1 (fr) * 2001-04-06 2006-08-18 Air Liquide Procede de combustion comportant des injections separees de combustible et d oxydant et ensemble bruleur pour la mise en oeuvre de ce procede
US6659762B2 (en) * 2001-09-17 2003-12-09 L'air Liquide - Societe Anonyme A' Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Oxygen-fuel burner with adjustable flame characteristics
FR2853953B1 (fr) * 2003-04-18 2007-02-09 Air Liquide Procede de combustion etagee d'un combustible liquide et d'un oxydant dans un four
US7624707B2 (en) * 2004-01-29 2009-12-01 Babcock & Wilcox Power Generation Group, Inc. Re-oriented over fire air ports for reduction of NOx production from pulverized coal-fired burners

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DE602005006321D1 (de) 2008-06-05
US20090239182A1 (en) 2009-09-24
DE602005006321T2 (de) 2009-07-09
WO2006064144A1 (fr) 2006-06-22
ATE393359T1 (de) 2008-05-15
JP4913747B2 (ja) 2012-04-11
US8231380B2 (en) 2012-07-31
FR2879283B1 (fr) 2007-01-19
FR2879283A1 (fr) 2006-06-16
JP2008523346A (ja) 2008-07-03
EP1828679A1 (de) 2007-09-05

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