JP2009513920A - Method and apparatus for low NOx combustion - Google Patents

Abstract

The present invention relates to a method and apparatus for low NO _x combustion with at least one burner (5) using fuel and oxidant and / or furnace off-gas and / or carbon dioxide and / or steam. The low NOx combustion according to the present invention can be used with the possibility of considerable savings in conventional melting or soaking furnaces, in particular aluminum soaking furnaces or rotary drum furnaces and glass melting furnaces.

Description

The present invention relates to a method and apparatus for low NO _x combustion using fuel and oxidant and / or in-furnace off-gas and / or carbon dioxide and / or steam.

In the known low-NO _x combustion, furnace off-gas is sucked by the blower covers the burner flame, thereby the flame temperature decreases, the heat release resulting NO _x is reduced.

However, this normal combustion does not completely mix the furnace off-gas recirculated in the furnace unit with the oxidant, so the required release of NO _{x in} the off-gas can only be realized at an additional cost. Has the disadvantages.

High investment cost is inherent in the known low NO _x combustion, also devices, particularly high load blower and cost for maintenance of the pipeline is still needed. Furthermore, external energy is required to operate the blower.

Accordingly, it is an object of the present invention to provide a method and apparatus that allows for economical and low pollutant (low NO _x ) combustion in a normal furnace system.

  This object is achieved by a method having the features of claim 1 and an apparatus having the features of claim 13.

  Advantageous refinements of the invention are indicated in the dependent claims.

  According to the invention, a burner block in the inner layer of the furnace of the furnace unit, together with fuel supplied separately to the burner, a mixture of oxidant and / or furnace off-gas and / or carbon dioxide and / or steam. Burn using a burner placed in

  For this purpose, an oxidant is supplied to the injector at a pressure of 0.2 to 40 bar, which is advantageously heated to 20 to 900 ° C. in a heat exchanger using furnace off-gas. Further, the oxidant may be supplied directly to the injector without heating.

The oxidant that expands as it flows out of the nozzle (which can move axially through the injector at the flow end side) generates a gas jet at a speed of 20 to 660 m / s into the injector. A suction action that causes a vacuum to draw either superheated steam generated from water by heat exchange with the furnace off-gas and / or carbon dioxide (CO ₂ ) and / or furnace off-gas into the oxidant jet. This mixture is then fed to the burner in the line connecting the injector to the burner, balancing the temperature.

  Ordinary blow nozzles, or some other equivalent technical means, can be used in place of the injectors, which are located in the stack provided for exhausting the furnace off-gas from the furnace chamber combustion chamber. Are advantageously arranged.

  As an alternative to the oxidant, fuel gas can be supplied to the injector at a pressure of 0.2 to 40 bar. In this case, an oxidizing agent is added to the burner.

  A mixture of oxidant and / or furnace off-gas and / or carbon dioxide and / or steam fed to the burner at a temperature of 20 ° C. to 1600 ° C., preferably 900 ° C., at a speed of 5 to 70 m / s, It has an oxygen content of at least 5% by volume.

  For example, the burner placed back in the burner block is preferably a parallel-flow burner, which is fuel and oxidant and / or furnace off-gas and / or carbon dioxide and / or Alternatively, it has two tubes (inner tube and outer tube) arranged substantially coaxially with each other for supplying steam to the burner port. The fuel or oxidant mixture can travel through the inner tube or outer tube to the burner port.

  The oxidizing agent used is an oxygen-containing medium with an oxygen content of at least 10% by volume.

  The fuel used can be any conventional gaseous or liquid fuel, particularly preferably natural gas.

  The injector, which is preferably operated with an oxidant, comprises an axially movable nozzle for controlling the intake and concentration and temperature of the mixture fed to the burner. This eliminates the need to supply external energy to the injector, i.e. requiring additional costs.

  A heat exchanger used for heating oxygen, carbon dioxide and water and advantageously arranged in an exhaust stack which discharges the furnace off-gas from the combustion chamber of the furnace apparatus is preferably a conventional heat transfer type It is a heat exchanger or a regenerative heat exchanger.

  The burner used is preferably a conventional co-current burner, having at least one supply path for the oxidant and at least one supply path for the fuel, preferably cylindrical and arranged coaxially Includes tubes.

The burner design according to the present invention allows the mixture of oxidant and / or furnace off-gas and / or carbon dioxide (CO ₂ ) and / or steam to exit the burner burner port at a rate 0.3 to 4 times faster than the fuel. Resulting in a total momentum flux of 1.5 to 8 N / MW based on the output of the burner, and a momentum flux density for the fuel of the oxidant and in-furnace off-gas mixture of 0.8 to 31 The ratio is ensured so that a power density of 0.2 to 0.5 KW / mm ² is reached at the outlet of the burner block.

Exit velocity of the oxidant and / or furnace off-gas and / or carbon dioxide (CO ₂₎ and / or mixtures of steam is 20 to 80 m / s at the burner outlet.

  The burner may be located on the off-gas side of the furnace device, preferably in an exhaust stack that discharges the furnace off-gas from the combustion chamber of the furnace device, or its intended in the furnace wall surrounding the furnace chamber combustion chamber It may be placed anywhere else suitable for use.

  It is also possible for the injector and the heat exchanger to be arranged in the burner. This type of injector / heat exchanger arrangement is particularly useful when the burner is installed on the offgas side of the furnace, such as in the case of a rotary drum furnace where the offgas in the furnace is around the burner mouth. This is advantageous when the air is extracted from the annular gap. In this case, the mixture of oxidant and / or furnace off-gas and / or carbon dioxide and / or steam is reheated by the furnace off-gas.

  The line carrying the oxidant, furnace off-gas, carbon dioxide and steam is made of heat-resistant and corrosion-resistant NiCr or ODS alloy, and insulation that ensures the required thermal protection from the inside and / or outside, preferably With ceramic fibers.

  The burner block with the burner preferably has a cylindrical opening.

  The burner is equipped with a UV photodetector for monitoring the flame.

Mixtures of oxidant and / or furnace off-gas and / or carbon dioxide and / or steam supplied to the burner according to the present invention reduce the reaction rate of combustion. This is because the reaction between oxygen and fuel is hindered by CO ₂ and / or H ₂ O molecules.

Mixing oxidants with furnace gases and / or carbon dioxide and / or steam results in the formation of abundant combustion flames with high concentrations of carbon dioxide and steam. Larger volume flames and higher concentrations of carbon dioxide and / or steam in the burner flame compared to that achieved by known combustion are carbon dioxide and / or steam gases occurring in the spectral region of the radiation band. significantly enhanced the radiation, as a result, the material to be treated can be heated by the flame temperature to reduce the level of the NO _x in the off-gas. The emission bands for carbon dioxide are in the range of 2.4-3 μm, 4-4.8 μm, 12.5-16.4 μm, and the emission bands for steam are 1.7-2 μm, 2.2-3 μm and 12 It is in the range of ˜30 μm.

As a result of the high viscosity mixture of oxidant and / or furnace off-gas and / or carbon dioxide and / or steam being delivered at a temperature between 20 ° C. and 1600 ° C., preferably 900 ° C., this mixture is fuel at the burner port. And mixing such that combustion occurs at a flame temperature of 800 ° C. to 2700 ° C., which significantly reduces the thermal NO _x off-gas potential of the furnace unit.

Mixtures of oxidant and / or furnace off-gas and / or carbon dioxide and / or steam fed to the burner, and the burner used according to the present invention, in the fuel tube of the burner and due to the design of the burner, In the fuel rich core of the burner flame, the fuel is at least partially self-carbonized. Self-carbonization or decomposition takes place in the oxygen-free region, in the case of hydrocarbons at temperatures above 1000 ° C., producing soot. Heating the soot particles in the burner flame results in a continuous radiation in the range of 0.2 to 20 micrometers, thus the flame is cooled, NO _x offgas level from the furnace apparatus is further reduced.

  A further advantage is improved heating of the lower layer, for example in a glass melt bath. This is because liquid glass is translucent to wavelengths in the range of 0.3 to 4 micrometers.

The NO _x off-gas level is further reduced, preferably with the use of a low N ₂ oxidant mixture and fuel.

The circulating furnace gas supplies nitrogen oxides present in the combustion chamber of the furnace apparatus to the burner flame, which in turn produces nitrogen (N ₂ ) in the fuel rich region of the burner flame. Decrease.

Very long resulting in the combustion chamber of the furnace device, smooth, no visible flame, allows a particularly advantageous low-NO _x combustion in an aluminum soaking furnace and rotary drum furnaces.

  Furthermore, the combustion according to the invention is stable and low noise. The noise level is 50-80 decibels.

Unlike known flameless combustion, the low NO _x combustion by the present invention, the flame radiation in the visible region, advantageously, improves the heat transfer to the material to be treated.

The high concentration and volume of CO ₂ / H ₂ O vapor in the burner flame further increases the gas emission of CO ₂ and / or H ₂ O vapor, which occurs in the spectral region of the emission band, for example in the case of molten glass And to ensure improved heat transfer to the material being processed.

  In addition, turbulence and convolutions that have destructive effects when dust-containing products are introduced are reduced.

  Injector inserts significantly reduce wear and maintenance costs of such furnace equipment, for example, for blowers made of expensive refractory materials used so far. Furthermore, the supply of external energy previously required to operate the blower is no longer necessary.

  Furthermore, the heat load and the resulting wear on the pipe tube is reduced. This is because mixing the oxidant with the furnace off-gas and / or carbon dioxide and / or steam reduces the temperature of the transported medium.

  In addition, primary energy can be saved by preheating oxygen and / or carbon dioxide and / or steam as oxidants with furnace off-gas in the heat exchanger, resulting in operating costs of the furnace equipment. Is further reduced.

With a uniform temperature distribution (the burner flame) in the low temperature level in the combustion chamber, as a result, low-NO _x combustion by the present invention with the NO _x off-gas potential is significantly reduced is used in any conventional furnace apparatus It can be used particularly advantageously in an aluminum soaking furnace or a glass melting furnace.

  The invention is explained in more detail below on the basis of exemplary embodiments shown in the drawings.

  The furnace apparatus shown in FIG. 1 includes a furnace inner layer 1 that surrounds a combustion chamber, and has an off-gas opening 19 and an exhaust pipe 2 that discharge off-gas in the furnace, as well as a pipeline 3 and a burner 5. A burner block 4 is provided, and the burner 5 is connected by a pipeline 7 to an injector 6 and a heat exchanger 8 located in the exhaust stack 2.

  The in-furnace off-gas flowing out of the combustion chamber through the off-gas opening 19 is cooled when flowing around the heat exchanger 8, and flows out of the furnace device through the exhaust stack 2.

  Gaseous oxygen used as an oxidant at a temperature of −20 to 40 ° C. and a pressure of 0.2 to 40 bar flows into the heat exchanger 8 through the inlet 9.

  Oxygen flowing through the heat exchanger 8 designed as a heat transfer heat exchanger or a heat storage heat exchanger is heated by the furnace off-gas flowing around the heat exchanger 8, and the outlet of the heat exchanger 8. 10 flows to the injector 6 through the inlet 11 at a temperature of 20-900 ° C.

  The oxygen flowing out from the outflow nozzle 12 of the injector 6 at a speed of 20 to 660 m / s expands to generate an oxygen jet that flows at a speed of 20 to 660 m / s.

  The fast flow rate of the oxygen jet creates a decompression at position 13 of the injector 6, and the suction action of the decompression sucks the furnace off-gas from the combustion chamber through the pipeline 3 into the oxygen jet, as a mixing zone of length x In the designed pipeline 7, this is mixed while balancing the temperature with the oxygen jet, and then the mixture of oxygen and in-furnace off-gas is supplied to the burner 5 through the connecting section 14 at a temperature of 20 to 1600 ° C. Is supplied with natural gas as gaseous fuel via a further connection 15.

  The pipeline through which oxygen and off-gas in the furnace pass is made of heat-resistant NiCr or ODS alloy and has a heat protection material on the inside and / or a heat insulation on the outside, for example, ceramic fiber or ceramic block. Have.

  The burner 5 used as a parallel-flow burner advantageously has an inner tube and an outer tube, and natural gas used as gaseous fuel is a fuel tube 18 arranged as an inner tube. The mixture of oxygen and furnace off-gas flows through the outer tube, which is designed as an annular gap 21, to the burner port 16 for processing. A long, smooth and visible burner flame is produced in the combustion chamber of the furnace apparatus for heating the material.

  Partial self-carbonization of the fuel occurs in the fuel tube 18 of the burner 5 through recuperative heat exchange between the oxidant and the furnace off-gas mixture.

The burner structure according to the present invention allows the mixture of oxidant and furnace off-gas to flow out of the burner port 16 at a rate 0.3 to 4 times faster than the fuel, resulting in a burner output. Based on the total momentum flux of 1.5 to 8 N / MW and the ratio of the momentum flux density to the fuel of the mixture of oxidizer and off-gas in the furnace of 0.8 to 31 is ensured, and as a result the outlet of the burner block 4 To reach a power density of 0.2 to 0.5 KW / mm ² .

  The mixture of the oxidizing agent and the furnace off-gas flows out from the burner port 16 at a speed of 20 to 80 m / s.

  The burner flame that burns the treated material in the combustion chamber has a flame temperature of 800-2700 ° C.

  The burner block 4 containing the burner 5 preferably has a cylindrical opening.

  The burner is advantageously equipped with a UV light detector 20 for monitoring the flame.

  If the furnace off-gas contains dust or other substances that are aggressive or promote oxidation, the furnace apparatus shown schematically in FIG. 2 is advantageously used. This furnace apparatus comprises a furnace inner layer 1 surrounding its combustion chamber, and has an off-gas opening 19 and an exhaust cylinder 2, which discharges the off-gas in the furnace and accommodates a heat exchanger 8, A burner block 4 having a burner 5 is connected to an injector 6 and a heat exchanger 8 by a pipeline 7.

  The in-furnace off-gas flowing from the combustion chamber through the off-gas opening 19 is cooled when flowing around the heat exchanger 8 to which water is supplied, and then flows out from the furnace device through the exhaust pipe 2.

  When flowing through the heat exchanger 8, the water supplied to the heat exchanger 8 through the inlet 9 evaporates by heat exchange with the furnace off-gas flowing around the heat exchanger 8, and then the injector 6. It flows in as superheated steam at 20 to 900 ° C. at position 13.

  Gaseous oxygen used as an oxidant at −20 to 40 ° C. and a pressure of 0.2 to 40 bar flows through the inlet 11 to the injector 6. The oxygen jet that expands as it flows out of the outflow nozzle 12 of the injector 6 increases its speed to 20-340 m / s, resulting in a reduced pressure at position 13 of the injector 6, and the suction action of the reduced pressure is the injector. The superheated steam is sucked into the oxygen jet flowing through 6 at position 13 and is mixed with the oxygen jet in the pipeline 7 designed as a mixing site of length x while balancing the temperature with the oxygen jet. The steam mixture flows at a temperature of 20 to 1600 ° C. through the connecting part 14 to the burner, and the burner is supplied with natural gas as a gaseous fuel through the connecting part 15.

  The pipeline through which oxygen and steam flow is made of heat-resistant and corrosion-resistant NiCr or ODS alloy, designed with heat protection from the inside or designed with heat insulation from the outside, such as ceramic fiber or ceramic Has a block.

  The burner 5 used as a co-current burner advantageously has an inner tube and an outer tube, and natural gas used as gaseous fuel passes through a fuel tube 18 arranged as an inner tube to the burner port 16. Flow, a mixture of oxygen and steam, flows into the burner port 16 through the outer tube, which is designed as an annular gap 21, containing the inner tube, thereby heating the material being processed. This produces a long, smooth and visible burner flame having a flame temperature of 800 ° C. to 2700 ° C. in the combustion chamber.

  Partial self-carbonization of the fuel occurs in the fuel tube 18 of the burner 5 by heat transfer heat exchange between the oxidant and steam mixture.

The burner design according to the present invention allows the mixture of oxidant and steam to exit from the burner port 16 of the burner at a rate 0.3 to 4 times faster than the fuel, and as a result, based on the burner output. Ensure a total momentum flux of 1.5 to 8 N / MW and a ratio of 0.8 to 31 oxidant and steam mixture to fuel momentum flux density, resulting in a 0. A power density of ^{2 to} 0.5 KW / mm ² is reached.

  The mixture of oxidant and steam flows out of the burner port 16 at a speed of 20 to 80 m / s.

  The burner block 4 preferably has a cylindrical opening.

  The burner is equipped with a UV light detector for flame monitoring.

  If the furnace off-gas contains dust or other aggressive or pro-oxidant substances, the furnace apparatus shown schematically in FIG. 3 is used. The furnace apparatus comprises a furnace inner layer 1 that surrounds a combustion chamber, has an off-gas opening 19 and an exhaust stack 2, which is designed to discharge the off-gas in the furnace, comprises a heat exchanger 8, and a burner 5 The burner 5 has a burner block 4, and the burner 5 is connected to the injector 6 and to the heat exchanger 8 by a pipeline 7.

  The exhaust gas flowing from the combustion chamber through the off-gas opening 19 is cooled when flowing around the heat exchanger 8 to which carbon dioxide is supplied, and then flows out from the furnace device through the exhaust pipe 2.

  The liquid or preferably gaseous carbon dioxide supplied through the inlet 9 of the heat exchanger 8 is heated to 20 ° C. to 900 ° C. by heat exchange with the furnace off-gas flowing around the heat exchanger 8. And flows through the outlet 10 to the injector 6 at position 13.

  Gaseous oxygen used as an oxidant at a temperature of −20 to 40 ° C. and a pressure of 0.2 to 40 bar is supplied to the injector 6 through the inlet 11. Oxygen flowing through the injector 6 expands as it exits the injector outlet nozzle 12, so that its flow rate rises to 20-340 m / s, resulting in a decompression at position 13 in the injector 6 and its The suction action of the reduced pressure sucks carbon dioxide into the oxygen jet, and the carbon dioxide is mixed in the pipeline 7 designed as a mixing portion of length x while balancing the temperature with the oxygen jet, and then oxygen and carbon dioxide. The mixture flows at a temperature of 20 to 1600 ° C. through the connecting part 14 to the burner 5, and natural gas as gaseous fuel is supplied to the burner via a further connecting part 15.

  The pipeline through which oxygen and carbon dioxide flow is made of heat-resistant and corrosion-resistant NiCr or ODS alloy, with a heat protection material inside and / or a heat insulation material on the outside, For example, it has a ceramic fiber.

  The burner 5 used as a co-current burner advantageously has an inner tube and an outer tube, and natural gas used as gaseous fuel has a fuel tube 18 arranged as an inner tube at the burner port 16. The mixture of oxygen and carbon dioxide is fed through a burner port 16 through an outer tube containing a fuel tube 18 and designed as an annular gap 21 and has a temperature of 800-2700 ° C. A long, smooth, visible burner flame is created in the combustion chamber of the furnace apparatus for heating the material being processed.

  Partial self-carbonization of the fuel occurs in the fuel tube 18 of the burner 5 by heat transfer heat exchange between the oxidant and carbon dioxide mixture.

The burner design according to the present invention allows a mixture of oxidant and carbon dioxide to exit from the burner outlet 16 at a rate 0.3 to 4 times faster than the fuel, and as a result, based on the burner output. Ensure a total momentum flux of 1.5-8 N / MW and a ratio of 0.8-31 oxidant and carbon dioxide mixture to fuel momentum flux density, resulting in 0 at the outlet of the burner block 4 A power density of ^{2 to} 0.5 KW / mm ² is reached.

  The mixture of the oxidizing agent and carbon dioxide flows out from the burner port 16 at a speed of 20 to 80 m / s.

  The burner block 4 preferably has a cylindrical opening.

  The burner is equipped with a UV light detector 20 for flame monitoring.

The figure which shows the furnace apparatus which has a combustion apparatus typically. The figure which shows typically the other furnace apparatus which has a combustion apparatus. The figure which shows the 3rd furnace apparatus which has a combustion apparatus typically.

Explanation of symbols

  DESCRIPTION OF SYMBOLS 1 ... Furnace inner layer, 2 ... Exhaust pipe (furnace offgas), 3 ... Pipeline (furnace offgas), 4 ... Burner block, 5 ... Burner, 6 ... Injector, 7 ... Pipeline, 8 ... Heat exchanger, DESCRIPTION OF SYMBOLS 9 ... Injection port (8), 10 ... Outflow port (8), 11 ... Inflow port (6), 12 ... Outflow nozzle, 13 ... Position (6), 14 ... Connection part (5), 15 ... Connection part (5 ), 16 ... burner port, 17 ... burner flame, 18 ... fuel tube, 19 ... offgas opening, 20 ... UV photodetector, 21 ... annular gap

Claims (27)

Fuel, as well as using an oxidizing agent and / or furnace off-gas and / or carbon dioxide and / or steam, a method for low NO _x combustion by at least one burner (5).   The method according to claim 1, characterized in that the oxidant and / or furnace off-gas and / or carbon dioxide and / or steam are fed to the burner (5) as a mixture.   The oxidant and / or furnace off-gas and / or carbon dioxide and / or steam fed to the burner (5) is preferably produced using at least one injector (6). Item 3. The method according to Item 1 or 2.   4. A method according to one of the preceding claims, characterized in that the injector (6) is operated preferably with the oxidant or fuel.   2. An oxidant having an oxygen content of at least 5% by volume and / or said mixture of furnace off-gas and / or carbon dioxide and / or steam is fed to said burner (5). The method according to one of -4.   The oxidant and / or furnace off-gas and / or carbon dioxide and / or steam mixture fed to the burner (5) is at a temperature between 20 ° C and 1600 ° C. The method according to one item.   7. The oxidizing agent used is an oxygen-containing medium containing oxygen at a temperature of -20 to 40 [deg.] C. at a pressure of 0.2 to 40 bar or at least 10% by volume of oxygen. The method according to item.   The method according to one of claims 1 to 7, characterized in that the combustion is carried out at a flame temperature of 800C to 2700C. _2. The rate at which the mixture of oxidant and / or furnace off-gas and / or carbon dioxide (CO2) and / or steam is produced at the burner port (16) is 20 to 80 m / s. The method according to one of ˜8. a) oxidizing agent and / or furnace off-gas and / or carbon dioxide (CO ₂₎ and / or the mixture of steam, banner port of the burner 0.3-4 times faster than the fuel (5) (16 )
b) Achieve a total momentum flux of 1.5-8 N / MW based on the burner output,
c) the ratio of the momentum flux densities of the oxidant to the fuel and / or furnace off-gas and / or carbon dioxide (CO ₂₎ and / or the mixture of steam is 0.8 to 31,
d) Method according to one of the preceding claims, characterized in that a power density of 0.2 to 0.5 KW / mm ² is reached at the outlet of the burner block (4). Partial self-carbonization of the fuel is transferred in the fuel tube (18) of the burner (5) with the mixture of oxidant and / or furnace off-gas and / or carbon dioxide (CO ₂ ) and / or steam. 11. A method according to one of the preceding claims, which takes place by recuperative heat exchange.   The method according to one of claims 1 to 11, characterized in that the oxidant and fuel flow out from the outflow nozzle (12) of the injector (6) at a speed of 20 to 660 m / s. Disposed within the burner block of the furnace wall surrounding the combustion chamber, an apparatus for performing the low NO _x combustion by at least one burner oxidant and fuel is supplied, the burner (5) is a line ( 7) A device characterized in that it is connected to the injector (6) and the heat exchanger (8) by 7).   14. Device according to claim 13, characterized in that the injector (6) has an outflow nozzle (12) movable in the axial direction.   15. A device according to claim 13 or 14, characterized in that the heat exchanger (8) is preferably arranged in an exhaust stack (2) for discharging furnace off-gas from the combustion chamber.   The device according to claim 15, characterized in that the heat exchanger (8) is designed as a heat transfer heat exchanger or a heat storage heat exchanger.   17. Device according to one of claims 13 to 16, characterized in that the injector (6) is arranged in the pipeline (7).   18. Device according to one of claims 13 to 17, characterized in that the injector (6) and / or the heat exchanger (8) are arranged in the burner (5).   14. The burner (5) has at least one connection (14) for supplying the oxidant mixture and at least one connection (15) for supplying the fuel. 18. The apparatus according to item 18.   20. Method according to claim 19, characterized in that the fuel supply path and / or the oxidant mixture supply path (18, 21) of the burner (5) are provided essentially coaxially with respect to each other. .   21. Device according to claim 19 or 20, characterized in that the burner (5) is arranged on the opposite side of the offgas opening (19).   22. The burner (5) according to one of claims 13 to 21, characterized in that the burner (5) is arranged on the off-gas side of the furnace device, preferably in the off-gas opening (19) or the exhaust stack (2). The device described.   The apparatus according to one of claims 13 to 22, wherein the medium conveying line is made of heat-resistant and corrosion-resistant NiCr or ODS alloy.   21. The device according to claim 20, wherein the medium conveying line has an insulation on the outside and / or a heat protection on the inside, which preferably consists of ceramic fibers or ceramic blocks.   25. Device according to one of claims 13 to 24, characterized in that the burner block (4) with the burner (5) preferably has a cylindrical opening.   26. Device according to one of claims 13 to 25, characterized in that the burner (5) comprises a UV photodetector (20) for flame monitoring.   The apparatus according to one of claims 13 to 26 and one of 1 to 12, in a melting furnace or soaking furnace, preferably in an aluminum soaking furnace or a rotary drum furnace or a glass melting furnace. Use of the described method.

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