KR20080069970A - Process and apparatus for low-nox combustion - Google Patents

Abstract

The invention relates to a process and an apparatus for low-NOx combustion with at least one burner (5) using fuel and oxidizing agent and/or furnace off-gases and/or carbon dioxide and/or steam. The low-NOx combustion according to the invention can be used in conventional melting and holding furnaces, in particular in aluminium holding furnaces or rotary drum furnaces and glass-melting furnaces, with the potential for considerable economies to be made.

Description

Process and apparatus for low-nitrogen oxide combustion {PROCESS AND APPARATUS FOR LOW-NOx COMBUSTION}

The present invention relates to a process and apparatus for low-nitrogen oxide combustion using fuels and oxidants and / or waste gases and / or carbon dioxide and / or steam.

In known low-nitrogen oxide combustion, the furnace waste gas sucked by the blower surrounds the burner flames, thereby lowering the flame temperature and consequently reducing the heat release of the nitrogen oxides.

However, this prior art has a big drawback that the waste gas recycled in the furnace installation is not perfectly mixed with the oxidant, and as a result, additional costs are required to realize the nitrogen oxide emission standard in the waste gas.

The use of known low-nitrogen oxide combustion leads to high investment costs and incurs additional costs for the maintenance of the installation (especially high load blowers and pipes). In addition, external energy is required for blower operation.

Accordingly, it is an object of the present invention to provide a process and apparatus capable of economically low pollution (low nitrogen oxide) combustion in a conventional furnace installation.

This object is achieved by a process having the construction of claim 1 and by a device having the construction of claim 13.

Advantageous improvements of the invention are set out in the sub-claims.

According to the invention, the mixture of oxidant and / or waste gas and / or carbon dioxide and / or steam is combusted with the fuel using a burner, the fuel is supplied separately from the mixture and the burner is placed in a burner block in the fire resistant lining of the furnace installation. do.

For this purpose, the oxidant is fed to the injector at a pressure of 0.2 to 40 bar, advantageously heated to 20 to 900 ° C. using waste gas in a heat exchanger. The oxidant may also be fed directly to the injector without heating.

The oxidant that expands while flowing out of the nozzle (possibly axially at the flow end of the injector) forms a gas jet at a velocity of 20 to 660 m / s, thereby reducing the pressure in the injector. The reduced pressure suction operation draws one of the superheated steam produced from the water through heat exchange with the furnace waste gas and / or carbon dioxide and / or the furnace waste gas into the oxidant jet, which mixture is then injected at temperature equilibrium. It is supplied to the burner in the line connecting the and burners.

Instead of an injector, which is advantageously arranged inside the stack provided for releasing furnace waste gas from the combustion chamber of the furnace installation, conventional blower nozzles or some other equivalent technical means can also be used.

By replacing the oxidant, it is also possible to supply fuel gas to the injector at a pressure of 0.2 to 40 bar. In this case, the oxidant is added to the burner.

The mixture of oxidant and / or waste gas and / or carbon dioxide and / or vapor fed to the burner at a rate of 5 to 70 m / s at a temperature of 20 ° C. to 1600 ° C., preferably 900 ° C., is at least 5% by volume. It has an oxygen content rate.

For example, a burner placed back in the burner block may have two coaxially arranged substantially coaxial with each other to supply fuel and oxidant and / or waste gas and / or carbon dioxide and / or vapor to the burner mouse. It is advantageous to be a parallel flow burner with tubes (inner tube and outer tube). The fuel or oxidant mixture is delivered to the burner mouse through the inner tube or outer tube.

The oxidant used is an oxygen containing medium having an oxygen content of at least 10% by volume.

The fuel used is any conventional gaseous or liquid fuel, in particular natural gas.

Advantageously, the injector operated with oxidant is equipped with an axially displaceable nozzle to control the intake, concentration and temperature of the mixture fed to the burner. This makes it unnecessary to supply external energy to the injector at additional cost.

A heat exchanger, which is used to heat oxygen, carbon dioxide and water and which is advantageously placed in a stack which releases the waste gas from the combustion chamber of the furnace plant, is advantageously a conventional recuperator or regenerator. .

The burner used is preferably a conventional parallel flow burner having at least one oxidant supply and at least one fuel supply and preferably comprising two tubes arranged coaxially.

The design of the burner according to the invention allows the mixture of oxidant and / or furnace waste gas and / or carbon dioxide and / or steam to flow out of the burner mouse of the burner at a rate of 0.3 to 4 times faster than the fuel, so that the total motion based on the burner output It is ensured that the total momentum flux is 1.5 to 8 N / MW and the kinetic flux density ratio of the mixture of oxidant and the waste gas to the fuel is 0.8 to 31, and as a result, the power density at the outlet of the burner block is 0.2 to It reaches 0.5KW / mm2.

The outlet velocity of oxidant and / or furnace waste gas and / or carbon dioxide and / or vapor is 20 to 80 m / s in burner mice.

The burner is also arranged on the waste gas side of the furnace plant, preferably inside a stack that emits furnace waste gas from the furnace chamber of the furnace plant, or any other suitable for its intended use within the furnace wall surrounding the furnace chamber. May be placed in position.

The injector and heat exchanger may be arranged inside the burner. This type of injector / heat exchanger arrangement is used when the furnace waste gas is extracted through the annular gap around the burner mouse, for example in the case of a rotary drum furnace, in particular when the burner is installed on the waste gas side of the furnace. It is advantageous. In this case, the mixture of oxidant and / or furnace waste gas and / or carbon dioxide and / or steam is heat-exchanged by the furnace waste gas.

The lines for transporting oxidants, waste gases, carbon dioxide and steam are made of heat and corrosion resistant NiCr or ODS alloys and provide thermal barriers to ensure the required thermal protection from the inside and / or outside and are preferably ceramic fibers. The burner block comprising the burner preferably has a cylindrical opening.

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

The mixture of oxidant and / or furnace waste gas and / or carbon dioxide and / or steam fed to the burner according to the invention reduces the combustion reaction rate. This is because the reaction of oxygen with the fuel is interrupted by carbon dioxide and / or water molecules.

By mixing the oxidant with the waste gas and / or carbon dioxide and / or steam, a high-volume and bulky combustion flame of carbon dioxide and steam is formed. Increased volumes of flame and increased concentrations of carbon dioxide and / or vapor in the burner flame, as compared to by known combustion, significantly increase the gas emissions of carbon dioxide and / or vapor that occur in the spectral region of the radiation band. The material to be treated is then heated to a flame temperature which lowers the concentration of nitrogen oxides in the waste gas. Suitable radiation zones for carbon dioxide are in the region of 2.4 to 3 μm, 4 to 4.8 μm, 12.5 to 16.4 μm, and suitable for steam are the regions of 1.7 to 2 μm, 2.2 to 3 μm and 12 to 30 μm.

As a result of the highly viscous mixture of oxidant and / or waste gas and / or carbon dioxide and / or steam being fed to the burner at a temperature of 20 ° C to 1600 ° C, preferably 900 ° C, the mixture is It is mixed with fuel in burner mice that occur at temperatures between 2 ° C. and 2700 ° C., which significantly reduces the thermal NOx off-gas potential of the furnace plant.

The mixture of oxidants and / or furnace waste gases and / or carbon dioxide and / or steam supplied to the burners as well as the burners used according to the invention is characterized by the fact that the fuel is in excess of fuel in the burner flame in the burner's fuel tube and Cause at least partially self-carburizing in the center. Self-carburization or decomposition occurs at temperatures greater than 1000 ° C. in the oxygen-free zone in the case of hydrocarbons, forming soot. The heating of the soot particles in the burner flame leads to continuous spinning in the 0.2-20 μm region and thus the flame is cooled, resulting in a lower nitrogen oxide waste gas concentration from the furnace installation.

Another advantage is to improve the heating of lower layers, for example in a glass melting bath, since the liquid glass is translucent for wavelengths in the region of 0.3 to 4 μm.

The nitrogen oxide waste gas concentration is preferably lowered by using a low-nitrogen oxidant mixture and fuel.

The circulating furnace gas causes nitrogen oxides present in the combustion chamber of the furnace installation to be supplied to the burner flame, which then reduces the production of nitrogen (N ₂ ) in the excess fuel region of the burner flame.

The very long and soft visible flames produced in the furnace chamber of the furnace plant are particularly advantageous for enabling low-nitrogen oxide combustion in aluminum holding furnaces and rotary drum furnaces.

In addition, the combustion according to the invention is stable and low in noise. The noise level is 50 to 80 dB.

With the use of low-nitrogen oxide combustion according to the invention, flame spinning in the visible region (unlike with known flame-free combustion) is advantageous for increasing heat exchange to the material to be treated.

The high concentration and volume of carbon dioxide / water vapor in the burner flame further increases the gas emissions of carbon dioxide and / or water vapor that occur in the spectral region of the radiation band, in this way (for example when melting glass). Heat transfer is reliably increased with the material being treated.

In addition, turbulence and vortex during combustion are reduced, which has a splitting effect when the dust-containing product is injected.

Insertion of injectors significantly reduces the wear and maintenance costs of furnace equipment, for example, resulting from blowers made of expensive heat resistant materials that have been used up to now. In addition, the supply of external energy, which has so far been required for blower operation, is no longer needed.

Furthermore, the oxidant and the waste gas and / or carbon dioxide and / or vapor are mixed to lower the temperature of the medium to be transported, thereby reducing the heat load and thus the wear to the pipe tube.

In addition, by preheating the oxygen and / or carbon dioxide and / or steam used as oxidant by the waste gas in the heat exchanger, it is possible to save major energy, thus further reducing the operating cost of the furnace equipment.

Low-nitrogen oxide combustion according to the present invention is any conventional furnace installation, with a uniform temperature distribution at low temperatures (burner flames) in the combustion chamber and with a significantly reduced nitrogen oxide waste gas potential thereby. It can be used in, and is particularly advantageous in aluminum thermal furnaces and glass melting furnaces.

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

The invention is described in greater detail below based on the exemplary embodiments described in the drawings.

1 schematically shows a furnace installation with a combustion device.

Figure 2 schematically shows another furnace installation with a combustion device.

3 schematically shows a third furnace installation with a combustion device.

The furnace installation shown in FIG. 1 comprises refractory linings 1, surrounding the combustion chamber, comprising a waste gas opening 19, a stack 2 for releasing furnace waste gas, a pipeline 3, and a burner. (5, burner) has a burner block (4), the burner (5) is connected to a heat exchanger (8) arranged in the injector (6) and the stack (2) by a pipeline (7).

The furnace waste gas exiting the combustion chamber through the waste gas opening 19 is cooled while flowing around the heat exchanger 8 and then exits from the furnace installation through the stack 2.

Gas in the gaseous state, which is used as an oxidant at a temperature of -20 ° C to 40 ° C and a pressure of 0.2 to 40bar, enters the heat exchanger 8 through the inlet 9.

Oxygen flowing through a heat exchanger (8) designed as a recuperator or regenerator is heated by furnace gas flowing around the heat exchanger (8), to a temperature of 20 to 900 ° C. It enters the injector 6 through the outlet 10 of the heat exchanger 8 and the injector inlet 11.

Oxygen exiting the outflow nozzle 12 of the injector 6 at a speed of 20 to 660 m / s expands to produce an oxygen jet that flows at a speed of 20 to 660 mm / s.

The high speed flow of oxygen jet is reduced in pressure at position 13 in the injector 6, and the suction operation of the reduced pressure sucks the furnace waste gases out of the combustion chamber, allowing oxygen jet, length x, to flow through the pipeline 3 It is introduced into a pipeline 7 designed as a mixing section. The waste gases are mixed with the oxygen jet at temperature equilibrium, and then the mixture of oxygen and furnace waste gases is supplied to the burner 5 through the connection 14 at a temperature of 20 to 1600 ° C., and natural gas is supplied as gaseous fuel. It is fed to the burner 5 via another connection 15.

The pipeline for transporting the oxygen and the waste gas consists of a heat resistant NiCr or ODS alloy and includes, for example, ceramic fibers or ceramic blocks, with thermal protection on the inside and / or heat shield on the outside.

The burner 5 used as a parallel flow burner advantageously has an inner tube and an outer tube, and the natural gas used as gaseous fuel is burner mouse 16 through a fuel tube 18 arranged as an inner tube. Furnace and a mixture of oxygen and furnace waste gas are flowed to the burner mouth 16 through an outer tube designed to receive the fuel tube 18 and designed as an annular gap 21, thereby heating the material to be treated. Creates a long, soft and visible burner flame 17 in the combustion chamber.

Partial self-carburization of the fuel takes place in the fuel tube 18 of the burner 5 via heat recovery heat exchange with a mixture of oxidant and waste gas.

The configuration of the burner according to the invention allows the mixture of oxidant and furnace waste gases to flow out of the burner mouse 16 of the burner at a rate of 0.3 to 4 times faster than the fuel, so that the total momentum flux based on the burner output is reduced. 1.5 to 8 N / MW and ensure that the kinetic flux density ratio of the mixture of oxidant and waste gas to fuel is 0.8 to 31, with the result that the power density at the outlet of burner block 4 is 0.2 to 0.5 KW / mm 2 Leads to

The oxidant and furnace waste gas mixture flows out of the burner mouse 16 at a rate of 20 to 80 m / s. The burner flame which burns the material to be treated in the combustion chamber has a flame temperature of 800 ° C to 2700 ° C.

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

The burners are advantageously equipped with an UV light receiver for flame monitoring.

The furnace plant shown schematically in FIG. 2 is advantageous when used in cases where the furnace waste gas contains dust or other erosive or high amounts of materials that promote oxidation. The furnace installation comprises a refractory lining 1 surrounding the combustion chamber of the furnace installation, a waste gas opening 19, a stack 2 which discharges the furnace waste gas and houses a heat exchanger 8, and a burner 5. Is provided with a burner block (4) and is connected to the injector (6) and the heat exchanger (8) by a pipeline (7).

The furnace waste gas flowing out of the combustion chamber through the waste gas opening 19 is cooled while flowing around the heat exchanger 8 to which water is supplied, and then out of the furnace installation through the stack 2.

When the waste gas flows through the heat exchanger 8, the water supplied to the heat exchanger through the inlet 9 is evaporated through heat exchange using the waste gas flowing around the heat exchanger 8, and then 20 to 900 ° C. Injector 6 is introduced into position 13 in a superheated vapor state at a temperature of.

Gas in the gaseous state, which is used as an oxidant at a temperature of −20 to 40 ° C. and a pressure of 0.2 to 40 bar, enters the injector 6 through the inlet 11. The oxygen jet expands as it flows out of the outlet nozzle 12 of the injector 6, increasing the flow rate to 20 to 340 m / s, resulting in a decrease in pressure at position 13 in the injector 6, The suction operation sucks the superheated steam into the oxygen jet flowing through the injector 6 at position 13 and the superheated steam is mixed with the oxygen jet in the pipeline 7 which is designed as a mixture of length x at a temperature equilibrium. The oxygen / vapor mixture is introduced into the burner 5 which is supplied with natural gas as a gaseous fuel through the connection portion 15 at a temperature of 20 to 1600 ° C. through the connection portion 14.

The pipelines that transport oxygen and steam are made of heat and corrosion resistant NiCr or ODS alloys and are designed to have thermal protection from the inside or thermal barrier from the outside, including, for example, ceramic fibers or ceramic blocks. The burner 5 used as a parallel flow burner advantageously has an inner tube and an outer tube, and the natural gas used as a gaseous fuel is burner mouse 16 through a fuel tube 18 arranged as an inner tube. Furnace and a mixture of oxygen and steam is flowed to the burner mouse 16 through an outer tube designed to receive the fuel tube 18 and design as an annular gap 21, through which a furnace apparatus for heating the material to be treated. Produces a long and soft visible burner flame 17 having a flame temperature of 800 to 2700 ° C. in its combustion chamber.

Partial self-carburization of the fuel occurs in the fuel tube 18 of the burner 5 via heat recoverable heat exchange with a mixture of oxidant and steam.

The configuration of the burner according to the present invention allows the mixture of oxidant and vapor to flow out of the burner mouse 16 of the burner at a rate of 0.3 to 4 times faster than the fuel, so that the total momentum based on the burner output is 1.5 to 8 N / MW. And ensure that the kinetic flux density ratio of the oxidant and the vapor mixture to the fuel is between 0.8 and 31, resulting in a power density of 0.2 to 0.5 KW / mm 2 at the outlet of the burner block 4.

The oxidant and vapor mixture flows out of the burner mouse 16 at a rate of 20 to 80 m / s.

The burner block 4 preferably has a cylindrical opening.

The burner is equipped with an UV light receiver for flame monitoring.

The furnace equipment shown schematically in FIG. 3 is used when the furnace waste gas contains a large amount of dust or other erosive or oxidizing substances. The furnace installation comprises a refractory lining 1 which surrounds the combustion chamber, a waste gas opening 19, a stack 2 which is designed to discharge the furnace waste gas and contains a heat exchanger 8, and a burner 5. Burner block (4) having a burner (5) is connected to the injector (6) and the heat exchanger (8) by a pipeline (7).

The exhaust gas flowing out of the combustion chamber through the waste gas opening 19 is cooled while flowing around the heat exchanger 8 to which carbon dioxide is supplied, and then out of the furnace equipment through the stack 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. via heat exchange with waste gas flowing around the heat exchanger 8, and the outlet It enters the injector 6 at position 13 via 10.

Gaseous oxygen, which is 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 flows out of the outlet nozzle 12 of the injector, increasing its flow rate to 20 to 340 m / s, resulting in a decrease in pressure at position 13 in the injector 6. . The reduced pressure suction operation sucks carbon dioxide into an oxygen jet and the carbon dioxide is mixed with oxygen at a temperature equilibrium in the pipeline 7 designed as a mixing section of length x. The mixture of oxygen and carbon dioxide then enters the burner 5, which is fed natural gas as a gaseous fuel via the connecting portion 15 at a temperature of 20 to 1600 ° C. via the connecting portion 14.

The pipeline for transporting oxygen and carbon dioxide consists of heat resistant and corrosion resistant NiCr or ODS alloys, and includes, for example, ceramic fibers, with an inner heat shield and / or an outer heat shield.

The burner 5 used as a parallel flow burner advantageously has an inner tube and an outer tube, and the natural gas used as a gaseous fuel is burner mouse 16 through a fuel tube 18 arranged as an inner tube. And a mixture of oxygen and carbon dioxide are flowed to the burner mouse 16 through an outer tube designed to accommodate the fuel tube 18 and designed as an annular gap 21, so as to heat the material to be treated. Produces a long, soft and visible burner flame 17 having a flame temperature of 800 to 2700 ° C. within.

Partial self-carburization of the fuel takes place in the fuel tube 18 of the burner 5 via heat recovery heat exchange with a mixture of oxidant and carbon dioxide.

The configuration of the burner according to the invention allows the mixture of oxidant and carbon dioxide to flow out of the burner mouse 16 of the burner at a rate of 0.3 to 4 times faster than the fuel, so that the total momentum based on the burner output is 1.5 to 8 N / MW. And ensure that the kinetic flux density ratio of the oxidant and carbon dioxide mixture to the fuel is between 0.8 and 31, resulting in an output density of 0.2 to 0.5 KW / mm 2 at the outlet of the burner block 4.

The mixture of oxidant and carbon dioxide flows out of the burner mouse 16 at a rate of 20 to 80 m / s.

The burner block 4 preferably has a cylindrical opening.

The burner is equipped with an UV light receiver for flame monitoring.

Reference list

1 fireproof lining

2 stacks (no waste gas)

3 pipelines (furnace waste gas)

4 burner blocks

5 burners

6 injector

7 pipeline

8 heat exchanger

9 Entrance (8)

10 exit (8)

11 entrance (6)

12 Outlet nozzles (6)

13 positions (6)

14 connections (5)

15 connections (5)

16 burner mouse

17 burner flame

18 fuel tubes

19 waste gas opening

20 UV light receiver

21 annular gap

Claims (27)

A low-nitrogen oxide combustion process utilizing at least one burner (5) utilizing fuel and oxidant and / or waste gas and / or carbon dioxide and / or steam. The method of claim 1, Low-nitrogen oxide combustion process, characterized in that an oxidant and / or a waste gas and / or carbon dioxide and / or steam are supplied to the burner (5) as a mixture. The method according to claim 1 or 2, An oxidant and / or furnace waste gas and / or carbon dioxide and / or vapor supplied to the burner (5) is preferably produced by at least one injector (6). The method according to any one of claims 1 to 3, Low-nitrogen oxide combustion process, characterized in that the injector (6) is preferably operated with oxidant or fuel. The method according to any one of claims 1 to 4, A low-nitrogen oxide combustion process, characterized in that a burner (5) is fed to a burner (5) with a mixture of oxidant and / or furnace waste gas and / or carbon dioxide and / or steam having an oxygen content of at least 5% of oxygen. The method according to any one of claims 1 to 5, Low-nitrogen oxide combustion process, characterized in that the mixture of oxidant and / or furnace waste gas and / or carbon dioxide and / or steam supplied to burner (5) is from 20 ° C to 1600 ° C. The method according to any one of claims 1 to 6, The oxidant used is a low-nitrogen oxide combustion process, characterized in that it is oxygen or an oxygen-containing medium containing at least 10% oxygen at a pressure of 0.2 to 40 bar and a temperature of -20 ° C to 40 ° C. The method according to any one of claims 1 to 7, Low nitrogen oxide combustion process characterized in that the combustion is carried out at a flame temperature of 800 ℃ to 2700 ℃. The method according to any one of claims 1 to 8, Low-nitrogen oxide combustion process, characterized in that the rate at which the mixture of oxidant and / or furnace waste gas and / or carbon dioxide and / or steam is released from the burner mouse (16) is 20 to 80 m / s. The method according to any one of claims 1 to 9, a) the oxidant and / or the furnace waste gas and / or the mixture of carbon dioxide and / or steam flows out of the burner mouse 16 of the burner 5 at a rate of 0.3 to 4 times faster than the fuel, b) the total momentum based on the burner output is formed at 1.5 to 8 N / MW, c) the kinetic flux density ratio of the mixture of oxidant and / or waste gas and / or carbon dioxide and / or steam to fuel is between 0.8 and 31, d) Low-nitrogen oxide combustion process, characterized in that at the outlet of burner block 4 the output density reaches 0.2 to 0.5 KW / mm 2. The method according to any one of claims 1 to 10, Low self-carburizing of fuel occurs in the fuel tube 18 of the burner 5 via heat recovery heat exchange with an oxidant and / or furnace waste gas and / or a mixture of carbon dioxide and / or steam. NOx combustion process. The method according to any one of claims 1 to 11, Low-nitrogen oxide combustion process, characterized in that an oxidant or fuel is withdrawn from the outlet nozzle (12) of the injector (6) at a speed of 20 to 660 m / s. A device for performing low-nitrogen oxide combustion with at least one burner, The burner is disposed in a burner block of the furnace wall surrounding the combustion chamber and is supplied with oxidant and fuel as described in any one of claims 1 to 12, The burner is connected to the injector (6) and the heat exchanger (8) by a line (7). The method of claim 13, Low-nitrogen oxide combustion apparatus, characterized in that the injector (6) has an outlet nozzle (12) that is axially disposed. The method according to any one of claims 13 to 14, Low-nitrogen oxide combustion apparatus, characterized in that the heat exchanger (8) is preferably arranged in a stack for releasing furnace waste gas from the combustion chamber. The method of claim 15, Low-nitrogen oxide combustion device, characterized in that the heat exchanger (8) is preferably designed as a heat recovery device or a regenerator. The method according to any one of claims 13 to 16, Low-nitrogen oxide combustion device, characterized in that the injector (6) is arranged in the pipeline (7). The method according to any one of claims 13 to 17, Low-nitrogen oxide combustion apparatus, characterized in that the injector (6) and / or heat exchanger (8) is arranged in the burner (5). The method according to any one of claims 13 to 18, The burner (5) has at least one connection (14) for supplying an oxidant mixture and at least one connection (15) for supplying fuel. The method of claim 19, Low-nitrogen oxide combustion apparatus, characterized in that the fuel feeder of the burner (5) and / or the oxidant mixture feeder (18,21) are arranged substantially coaxially with respect to each other. The method of claim 19 or 20, Burner (5) is disposed opposite the waste gas opening (19). The method according to any one of claims 13 to 21, The burner (5) is arranged on the waste gas side of the furnace installation, and is preferably arranged in the waste gas opening (19) or the stack (2). The method according to any one of claims 13 to 22, Low-nitrogen oxide combustion apparatus, characterized in that the medium transport line is made of heat resistant and corrosion resistant NiCr or ODS alloy. The method of claim 20, The medium transport line has a heat shield on the outside and / or a heat protector on the inside, and is preferably made of ceramic fibers or ceramic blocks. The method according to any one of claims 13 to 24, Low-nitrogen oxide combustion apparatus, characterized in that the burner block (4) comprising the burner (5) preferably has a cylindrical opening. The method according to any one of claims 13 to 25, Burner (5) is a low-nitrogen oxide combustion apparatus, characterized in that the UV light receiver 20 is provided for flame monitoring. Use of the apparatus and process according to any one of claims 1 to 26 in a melting furnace or insulator, preferably in an aluminum insulator or in a rotating drum or in a glass melting furnace.

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