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WO2024170153A1 - Procédé de chauffage d'un four de fusion de verre et agencement de brûleur correspondant - Google Patents

Procédé de chauffage d'un four de fusion de verre et agencement de brûleur correspondant Download PDF

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Publication number
WO2024170153A1
WO2024170153A1 PCT/EP2024/050110 EP2024050110W WO2024170153A1 WO 2024170153 A1 WO2024170153 A1 WO 2024170153A1 EP 2024050110 W EP2024050110 W EP 2024050110W WO 2024170153 A1 WO2024170153 A1 WO 2024170153A1
Authority
WO
WIPO (PCT)
Prior art keywords
oxygen
furnace chamber
burner
fuel
carbon monoxide
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.)
Ceased
Application number
PCT/EP2024/050110
Other languages
German (de)
English (en)
Inventor
Martin Demuth
Christian Erich Gaber
Gyula PALMAI
Philipp SCHINDLER
Florian Toth
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.)
Messer Austria GmbH
Messer Hungarogaz Kft
Original Assignee
Messer Austria GmbH
Messer Hungarogaz Kft
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 Messer Austria GmbH, Messer Hungarogaz Kft filed Critical Messer Austria GmbH
Publication of WO2024170153A1 publication Critical patent/WO2024170153A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/04—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture in tank furnaces
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/235—Heating the glass
    • C03B5/2353—Heating the glass by combustion with pure oxygen or oxygen-enriched air, e.g. using oxy-fuel burners or oxygen lances
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/24—Automatically regulating the melting process
    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B2211/00—Heating processes for glass melting in glass melting furnaces
    • C03B2211/40—Heating processes for glass melting in glass melting furnaces using oxy-fuel burners

Definitions

  • the invention relates to a method for heating a glass melting furnace.
  • the invention further relates to a burner arrangement suitable for carrying out the method.
  • a well-known method for reducing NOx emissions in combustion processes is to stage the combustion air.
  • the combustion air is fed to the flame in two or more partial flows from spatially separated positions. Part of the combustion air is thus withheld from the main combustion zone, which usually leads to a substoichiometric combustion reaction and thus to a high level of carbon monoxide (CO) production.
  • CO carbon monoxide
  • the resulting comparatively low adiabatic combustion temperature in the main combustion zone reduces the formation of thermal NOx.
  • the carbon monoxide produced also directly reduces locally present NOx.
  • the unburned components of the fuel are afterburned at a certain distance from the main combustion zone by a secondary air flow.
  • the most prominent examples of this type of combustion are boxer furnaces in power plants, where the combustion air is even divided into primary, secondary and tertiary air.
  • oxygen burners In contrast to air burners, oxygen burners (oxyfuel burners) use technically highly pure oxygen as an oxidizer. Especially in the case of high-temperature oxygen burners, such as those used in glass melting furnaces, in which combustion chamber temperatures of 1450°C and higher are required, however, residual nitrogen in the oxidizer or the The introduction of false air into the furnace chamber results in very high concentrations of nitrogen oxides. It has therefore already been proposed to apply the principle of staged combustion to such combustion processes. However, due to the significantly reduced volume flows, oxygen burners are significantly smaller and more compact than air burners, which makes it much more difficult to accommodate or subsequently install complex gas distribution systems for staging the oxygen.
  • EP 0 762 050 A1 and EP 3 366 994 A1 disclose methods for carrying out staged combustion using oxyfuel burner arrangements.
  • the burner arrangements described therein have a flat flame burner with an oval outlet opening, from which at least one further, also oval-shaped outlet lance for secondary oxygen is arranged at a vertical distance.
  • Such a multiple oxygen supply makes it possible, on the one hand, to distribute the total oxygen flow introduced to the burner and outlet lance(s) and thus to direct the oxygen input away from the center of the furnace chamber towards the outside area, and, on the other hand, to set an oxygen concentration in the furnace chamber in an area below or below and/or above the flame.
  • a reduced oxygen concentration below the flame proves to be advantageous in glass production in particular, since a carbon monoxide-rich atmosphere forms locally there, which counteracts foam formation in the glass melt and can also reduce foam that has already formed.
  • the invention is based on the object of specifying a method for heating a glass melting furnace which produces little NOx and which further reduces the foam formation of a glass melt.
  • a method for heating a glass melting furnace is carried out according to the invention using a staged combustion in a furnace chamber by means of a A burner arrangement is used to introduce a carbon-containing fuel stream, such as natural gas, coal dust or oil, and a primary oxygen stream that is substoichiometric to the fuel stream into the furnace chamber and to burn them together there to form a flame, and a secondary oxygen stream is also introduced into the furnace chamber by means of the burner arrangement in such a way that an oxygen-rich atmosphere is generated in an upper region of the furnace chamber and an oxygen-poor and carbon monoxide-rich atmosphere is generated in a lower region of the furnace chamber adjacent to a glass melt located in the furnace chamber, the carbon monoxide content being continuously varied in at least a partial region of the oxygen-poor and carbon monoxide-rich atmosphere generated in the lower region of the furnace chamber.
  • a carbon-containing fuel stream such as natural gas, coal dust or oil
  • a primary oxygen stream that is substoichiometric to the fuel stream into the furnace chamber and to burn
  • a “burner arrangement” is to be understood here as a device for heating a glass melting furnace, which enables staged combustion in the furnace chamber of the glass melting furnace.
  • This generally requires at least one fuel supply and at least two oxygen supplies for introducing primary and secondary oxygen.
  • the oxygen supplies can be arranged in a common housing together with at least one fuel supply, for example coaxially therewith, and thus form a burner with the fuel supply(s), and/or the oxygen supplies or at least one oxygen supply is spatially separated from the fuel supply(s) in the form of lances opening into the furnace chamber.
  • the oxygen can also be introduced into the furnace chamber in the form of an oxygen-containing gas, such as air or oxygen-enriched air (with an oxygen content of >21 vol.%).
  • oxygen burner is understood here to mean a burner that is intended and suitable for burning a solid, gaseous or liquid, carbon-containing fuel, such as natural gas, oil or coal dust, with an oxidant whose oxygen content is at least 90% by volume.
  • a gas with an O2 content of at least 90% by volume is also referred to below as "pure oxygen”.
  • at least one oxygen burner is used in the process according to the invention, in which the primary oxygen is used as an oxidant.
  • a "high-impulse burner” is to be referred to here as an oxygen burner which is designed in such a way that the fuel and/or the oxygen flow out of a burner mouth of the high-impulse burner which opens into the furnace chamber at an exit speed of at least 50 m/s, preferably at least 100 m/s, particularly preferably at least 150 m/s.
  • the design of the burner as a high-impulse burner leads to intensive recirculation in the furnace chamber, which lowers the flame temperature and thus inhibits the formation of NOx.
  • the high exit speeds promote flow conditions which lead to temporally and spatially fluctuating concentrations of certain gases in the vicinity of the flame. As explained in more detail below, this circumstance proves to be advantageous for the method according to the invention.
  • oxygen lance is understood here to mean an apparatus by means of which oxygen or an oxygen-containing gas can be introduced into the furnace chamber in the form of a jet.
  • the oxygen lances are also preferably designed as high-impulse lances from which the oxygen is ejected at a speed of at least 50 m/s, preferably at least 100 m/s, particularly preferably at least 150 m/s.
  • a staged combustion takes place in which the fuel flow and the primary oxygen flow are in a substoichiometric ratio to one another and an amount of oxygen that is stoichiometric to the fuel flow is only introduced by the addition of the secondary oxygen.
  • the method according to the invention initially follows the approach known from the prior art, according to which an oxygen-poor, carbon monoxide-rich atmosphere brought about by a staged combustion in a lower area of the furnace chamber, i.e. adjacent to the glass melt, suppresses the formation of foam in the glass melt or reduces foam that has already formed.
  • a carbon monoxide content of over 100 vpm, preferably over 1000 vpm proves to be advantageous for reducing foam formation.
  • the suppression of foam formation and/or the reduction of foam already formed in the glass melt can be further improved by reducing the carbon monoxide content is continuously changed at least in a portion of this atmosphere, i.e. continuously increases, decreases, or fluctuates spatially and/or temporally.
  • the carbon monoxide content in a given spatial area should change by at least 10% to 100% within a period of no more than 10 minutes, preferably less than 1 minute.
  • turbulent flows lead to fluctuations in the carbon monoxide content, a change of this magnitude can also occur very quickly, within a few seconds, with the strength and range of fluctuation depending on the respective conditions of the furnace chamber and the burner arrangement used.
  • the change in the carbon monoxide content in at least a partial area of the atmosphere generated in the lower area of the furnace chamber is carried out by bringing about a temporal and/or spatial variation in the flow rate(s) of fuel and/or primary oxygen and/or secondary oxygen introduced into the furnace chamber.
  • This can be done, for example, by varying the total oxygen flow supplied to the furnace chamber or by dividing an overall constant oxygen flow in a time-varying manner between the feeds for primary and secondary oxygen (and/or between different feeds for secondary oxygen).
  • the change in the carbon monoxide content can be carried out by pivoting or rotating a flame generated in the furnace chamber and/or by a pulsed or otherwise time-varying introduction of one or more of the gas flows (fuel and/or primary and/or secondary oxidizing agent) introduced into the furnace chamber.
  • the gas flows fuel and/or primary and/or secondary oxidizing agent
  • a particularly preferred embodiment of the method according to the invention provides that the fuel flow and/or the primary oxygen flow and/or the secondary oxygen flow are fed into the The high flow speeds lead to intensive recirculation of the combustion gases in the furnace chamber.
  • turbulent flow phenomena occur which mean that an atmosphere that is not stationary in its composition, i.e. essentially constant in space and time, does not form in the lower area of the furnace chamber; rather, this area is constantly subject to temporal and spatial fluctuations, particularly in its carbon monoxide content.
  • a preferred burner arrangement for carrying out the method according to the invention has the features of patent claim 5.
  • the burner arrangement is equipped with a fuel channel for introducing a carbon-containing fuel into a furnace chamber of a glass melting furnace, an oxygen supply for supplying primary oxygen into the furnace chamber and an oxygen supply for supplying secondary oxygen in an upper region of the furnace chamber, as well as with means for continuously changing the carbon monoxide content of an atmosphere forming below a horizontal burner plane defined by the burner mouth.
  • the supply of secondary oxygen into an upper area of the furnace chamber enables staged combustion, whereby, with overall stoichiometric ratios, an oxygen-poor, carbon monoxide-rich atmosphere is formed in a lower area of the furnace chamber.
  • the continuous change in the carbon monoxide content results in a particularly efficient reduction in foam formation on the glass melt.
  • the oxidant used in the burner arrangement according to the invention is preferably pure oxygen.
  • the burner arrangement according to the invention preferably comprises a burner in which the fuel channel and the oxygen supply for primary oxygen are arranged coaxially to one another in a common housing which opens into the furnace chamber at a burner mouth.
  • the oxygen supply for secondary oxygen is preferably designed as an oxygen lance which opens into the furnace chamber above a horizontal plane ("burner plane") of the burner which runs through a flame which forms in front of the burner mouth.
  • the means for continuously changing the carbon monoxide-rich atmosphere that forms below the burner level comprise means for temporally or spatially changing the flow rate(s) of fuel and/or primary oxygen and/or secondary oxygen introduced into the furnace chamber, such as, for example, corresponding control devices for controlling the corresponding gas flow and/or a distribution device by means of which an overall constant oxygen flow supplied to the furnace chamber is divided between the primary and secondary oxygen supplies with proportions that vary over time.
  • means for pivoting and/or rotating the flame can be used, as known for example from EP 1 821 036 A1. Rotating or pivoting the flame usually also changes the carbon monoxide concentration in a given area of the room.
  • the burner of the burner arrangement is a high-impulse burner and/or the at least one oxygen supply for secondary oxygen is a high-impulse lance in accordance with the above definition, in which the gas supplied is introduced at a speed of at least 50 m/s, preferably at least 100 m/s, particularly preferably at least 150 m/s. Due to the high recirculation of furnace gases in the furnace chamber when using such high-impulse burners or high-impulse lances, there is, as already explained above, a continuous change in the chemical composition of the atmosphere below a flame-induced temperature due to turbulent flows. defined burner level, and thus to a continuous change in the carbon monoxide content in this area.
  • the fuel channel and the oxygen supply of the high-impulse burner are preferably essentially cylindrical in shape and arranged coaxially with one another, whereby the fuel channel can be arranged within the oxygen supply or, conversely, the oxygen supply can be arranged within the fuel supply.
  • the fuel channel and/or the oxygen supply can be conically shaped at their respective exit opening at the burner mouth.
  • the high-impulse burner is preferably guided through the burner stone horizontally or at an inclination of less than 10° relative to the horizontal.
  • the at least one oxygen lance which is preferably guided through the burner stone parallel to the axis of the high-impulse burner, opens out of the burner stone geodetically above the high-impulse burner, i.e.
  • the at least one oxygen lance also preferably has a circular or almost circular cross-section.
  • An expedient further development of the invention is characterized by at least one additional oxygen supply for secondary oxygen, which opens vertically into the furnace chamber below the burner mouth. This makes it possible to directly influence the chemical composition of the atmosphere below the flame.
  • Fig. 1 A burner arrangement according to the invention in longitudinal section
  • Fig. 2 The burner arrangement from Fig. 1 in a front view, seen from
  • Fig. 3 A burner assembly from Fig. 1 , 2 equipped with
  • the burner arrangement 1 shown in Fig. 1 has a high-impulse burner 2 which is accommodated in a passage 3 of a burner block 4.
  • the high-impulse burner 2 has a central fuel channel 5 for supplying a carbon-containing fuel and an oxygen supply 6 arranged coaxially around it for supplying primary oxygen.
  • the fuel channel 5 and oxygen supply 6 are arranged in a common housing 7 which opens into a furnace chamber 8 at a burner mouth 9.
  • the high-impulse burner 2 is designed so that fuel and primary oxygen are introduced into the furnace chamber at a flow rate of at least 50 m/s, preferably at least 100 m/s, particularly preferably at least 150 m/s.
  • the high flow velocity of the introduced gases leads to an intensive recirculation of the combustion gases present in the furnace chamber, which, among other things, leads to a reduction in the temperature of a flame forming in the furnace chamber 8 (not shown here).
  • the burner arrangement 1 has oxygen lances 10, 11 for introducing secondary oxygen, which in the exemplary embodiment are arranged axially parallel to the burner axis 12 of the high-impulse burner 2 and at a distance from it.
  • the oxygen lance 10 is arranged vertically above a horizontal plane running through the axis of the high-impulse burner 2 (burner plane 13), while the oxygen lance 11 is arranged vertically below the burner plane 13.
  • the vertical distance of the oxygen lances 10, 11 from the high-impulse burner 2 should be at least 1.8 times, preferably at least 2.5 times the diameter of the high-impulse burner 2 at the burner mouth 9.
  • the oxygen lances 10, 11 are also high-impulse introduction systems, ie the oxygen flow introduced into the furnace chamber 8 by the oxygen lances 10, 11 has a speed of at least 50 m/s, preferably at least 100 m/s, particularly preferably at least 150 m/s.
  • the oxygen lances 10, 11 and the high-impulse burner 2 are arranged one above the other in a vertical plane 14.
  • a plurality of oxygen lances 10, 11 are provided above and/or below the burner 2; these can open into the furnace chamber 8, for example, along a horizontal line or in another way, for example in a ring around the high-impulse burner 2.
  • the fuel channel 5 is in flow connection with a source for a fuel (not shown here) via a fuel line 15.
  • the oxygen supply 6 and the oxygen lances 10, 11 are in flow connection with an oxygen line 19 via connecting lines 16, 17, 18, which in turn is connected to a source for an oxidant (also not shown here), for example pure oxygen with an oxygen content of at least 90 vol.%.
  • a distribution device 20 is provided in the oxygen line 19, by means of which the distribution of an oxygen flow supplied via the oxygen line 19 to the connecting lines 16, 17, 18 and thus to the oxygen supply 6 and the oxygen lances 10, 11 can be controlled.
  • This distribution device 20 exists independently of a control device (not shown here but nevertheless present) by means of which the total flows of fuel and oxygen supplied to the furnace chamber 8 via the fuel line 15 or the oxygen line 19 can be regulated.
  • the distribution device 20 can be controlled by means of a control 21, which can be a mechanical or electronic control, as explained in more detail below by way of example.
  • a glass melting furnace 23 equipped with the burner arrangement 1 according to the invention is shown.
  • the burner arrangement 1 opens into the furnace chamber 8 of the glass melting furnace 23 on a side wall 24 of the glass melting furnace 23, above a glass melt 25 present in the glass melting furnace 23.
  • the glass melting furnace 23 also has a Smoke exhaust 26, through which the smoke gases generated in the glass melting furnace 23 can escape.
  • a flow of fuel is introduced into the furnace chamber 8 via the fuel line 15 and the fuel channel 5 at the high speed described above.
  • a hydrocarbon-containing gas such as natural gas, is used as the fuel, for example.
  • an oxygen flow is introduced via the oxygen line 19, which is preferably stoichiometric or slightly overstoichiometric to the fuel flow.
  • the supplied oxygen flow is completely divided between the connecting lines 16, 17, 18 in the manner described in more detail below in the distribution device 20 and reaches the furnace chamber 8 via the oxygen supply 6 or the oxygen lances 10, 11. There it is ignited with the fuel flow, whereupon a flame 27 forms in the furnace chamber 8.
  • the following operating modes are preferred: a) The majority of the oxygen is fed to the oxygen supply 6. The flows of fuel and primary oxygen introduced into the furnace chamber 8 at the burner mouth 9 of the high-impulse burner 2 are therefore at least almost stoichiometric to one another. No oxygen is introduced via the oxygen lances 10, 11, or at most a small oxygen flow is introduced, which only serves to cool the oxygen lances 10, 11 and which does not contribute significantly to the combustion of the fuel in the furnace chamber 8. This operating mode is preferred, for example, when starting the high-impulse burner 2 or for heating up the furnace chamber 2. b) At least a large portion of the oxygen is fed evenly into the furnace chamber 8 via both oxygen lances 10, 11 (two-stage combustion).
  • any small residual flow is fed via the oxygen supply 6 solely for the purpose of stabilizing the flame forming in front of the burner mouth 9 and cooling the high-impulse burner 2.
  • the supply of oxygen via the oxygen supply may even be completely eliminated.
  • the high-impulse burner 2 is therefore operated significantly substoichiometrically, the majority of the oxygen required for combustion is introduced as secondary oxygen. The combustion process therefore takes place largely on the outer edges of the flame, which overall lowers the temperature of the flame and reduces the formation of NOx compounds.
  • a large part of the oxygen is introduced into the furnace chamber 8 via the upper oxygen lance 10 (single-stage combustion).
  • a smaller residual flow is introduced via the oxygen supply 6 solely for the purpose of stabilizing a flame forming in front of the burner mouth 9 and cooling the high-impulse burner.
  • No oxygen is introduced via the oxygen lances 11, or at most a small oxygen flow, which primarily serves to cool the oxygen lance 11 and which does not contribute significantly to the combustion of the fuel in the furnace chamber 8.
  • an atmosphere 28 with a significant excess of oxygen forms in the area above the burner level 13.
  • the combustion below the burner level 13 is substoichiometric overall.
  • the atmosphere 29 that forms in this area is very low in oxygen. Therefore, carbon monoxide is increasingly formed in this area, which suppresses the formation of foam on the glass melt 25 when the burner arrangement 1 is in use or reduces foam that has already formed.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Glass Melting And Manufacturing (AREA)

Abstract

Selon un procédé de réalisation d'une combustion par étapes dans un four de fusion de verre, une région à faible teneur en oxygène ayant une concentration élevée en monoxyde de carbone est formée entre l'étage de brûleur et la masse fondue de verre. Selon l'invention, des fluctuations temporelles et/ou locales de la concentration en monoxyde de carbone sont délibérément amenées dans cette région. La variation continue de la concentration en monoxyde de carbone permet de réguler plus efficacement la formation de mousse dans la masse fondue de verre.
PCT/EP2024/050110 2023-02-15 2024-01-03 Procédé de chauffage d'un four de fusion de verre et agencement de brûleur correspondant Ceased WO2024170153A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102023103719.6 2023-02-15
DE102023103719.6A DE102023103719A1 (de) 2023-02-15 2023-02-15 Verfahren zum Beheizen eines Glasschmelzofens und Brenneranordnung dazu

Publications (1)

Publication Number Publication Date
WO2024170153A1 true WO2024170153A1 (fr) 2024-08-22

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Family Applications (1)

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PCT/EP2024/050110 Ceased WO2024170153A1 (fr) 2023-02-15 2024-01-03 Procédé de chauffage d'un four de fusion de verre et agencement de brûleur correspondant

Country Status (2)

Country Link
DE (1) DE102023103719A1 (fr)
WO (1) WO2024170153A1 (fr)

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4634461A (en) * 1985-06-25 1987-01-06 Ppg Industries, Inc. Method of melting raw materials for glass or the like with staged combustion and preheating
EP0762050A2 (fr) 1995-09-05 1997-03-12 Air Products And Chemicals, Inc. Brûleur à combustion étagée à faible émission de NOx pour le chauffage contrÔlé par rayonnement des fours à haute température
US5833730A (en) * 1992-11-27 1998-11-10 Pilkington Glass Limited Method for reducing NOx emissions from a regenerative glass furnace
EP1821036A2 (fr) 2006-02-21 2007-08-22 Messer Group GmbH Brûleur
EP2679991A2 (fr) * 2012-06-25 2014-01-01 Software & Technologie Glas GmbH (STG) Procédé de détermination d'un taux de monoxyde de carbone dans un flux de gaz d'échappement, notamment un dispositif de commande et un four industriel régénératif
EP3366994A1 (fr) 2017-02-22 2018-08-29 Air Products And Chemicals, Inc. Brûleur oxycombustible à double étage

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2659729B1 (fr) * 1990-03-16 1992-06-05 Air Liquide Procede de fusion et d'affinage d'une charge.
JP5485193B2 (ja) * 2011-01-26 2014-05-07 大陽日酸株式会社 バーナの燃焼方法
US11261117B2 (en) * 2019-10-25 2022-03-01 Air Products And Chemicals, Inc. System and method for synchronized oxy-fuel boosting of a regenerative glass melting furnace

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4634461A (en) * 1985-06-25 1987-01-06 Ppg Industries, Inc. Method of melting raw materials for glass or the like with staged combustion and preheating
US5833730A (en) * 1992-11-27 1998-11-10 Pilkington Glass Limited Method for reducing NOx emissions from a regenerative glass furnace
EP0762050A2 (fr) 1995-09-05 1997-03-12 Air Products And Chemicals, Inc. Brûleur à combustion étagée à faible émission de NOx pour le chauffage contrÔlé par rayonnement des fours à haute température
EP1821036A2 (fr) 2006-02-21 2007-08-22 Messer Group GmbH Brûleur
EP2679991A2 (fr) * 2012-06-25 2014-01-01 Software & Technologie Glas GmbH (STG) Procédé de détermination d'un taux de monoxyde de carbone dans un flux de gaz d'échappement, notamment un dispositif de commande et un four industriel régénératif
EP3366994A1 (fr) 2017-02-22 2018-08-29 Air Products And Chemicals, Inc. Brûleur oxycombustible à double étage

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