JP2005164205A - Combustion method for combustion equipment, and combustion equipment - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a combustion method for combustion equipment, and combustion equipment that can improve high efficiency combustion/heat recovery efficiency and reduce NOx generated from combustion by producing high concentration oxygen by means of heat of combustion exhaust gas and using a mixture of the oxygen and the combustion exhaust gas as a combustion oxidizer. <P>SOLUTION: The combustion equipment produces oxygen by a thermal swing adsorption method (TSA 3) that uses heat of heat-recovered exhaust gas from fuel combustion in a combustion part 1 to desorb oxygen from an adsorbent for adsorbing oxygen in air selectively; and supplies a mixture of the produced oxygen and part of the heat-recovered exhaust gas to a combustion furnace 1a as a combustion oxidizer. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

  The present invention uses an oxidant that is a mixture of oxygen and exhaust gas generated by using combustion exhaust gas for combustion in a combustion facility, suppresses nitrogen oxides generated by combustion, and achieves high efficiency combustion, heat The present invention relates to a combustion method for a combustion facility capable of improving recovery efficiency and the facility.

  Conventionally, in a combustion apparatus such as a boiler using fossil fuel or an incinerator for burning waste, etc., as shown in the flow of the conventional combustion system in FIG. 4, the combustion apparatus 100 (boiler, incinerator, etc.) is used. The fuel and oxidant are supplied to perform combustion, and the generated exhaust gas is discharged from the chimney 102 after the exhaust gas treatment facility 101 removes dust and removes acidic gas. Although air is mainly used as the combustion oxidant, oxygen-enriched air mixed with oxygen to increase the oxygen concentration or pure oxygen for the purpose of improving heat recovery efficiency by reducing the amount of exhaust gas May be used.

  In general, waste incinerators use air as a combustion oxidant for combustion, but a part of combustion exhaust gas is circulated from the viewpoint of low pollution and effective use of energy such as suppression of NOx generation accompanying combustion. Exhaust gas recirculation method used as an oxidant by mixing with oxygen, and oxygen-enriched combustion method used as a main oxidant by increasing the oxygen concentration with an oxygen-enriched membrane or the like. However, the exhaust gas recirculation method has problems such as an increase in the size of the furnace / exhaust gas treatment equipment due to an increase in the amount of passing gas and a decrease in the combustion chamber temperature. There are problems such as increased NOx and high running cost of the oxygen generator. As a means to solve these problems, the exhaust gas treatment equipment is circulated, mixed with oxygen and used as a combustion oxidant to reduce the size of the exhaust gas treatment facility, and the amount of oxygen to be mixed A technique for facilitating control of the combustion state such as the furnace temperature is disclosed in Patent Document 1.

  Further, when oxygen is used as part of a combustion oxidant in a combustion furnace (for example, an incinerator), a pressure swing adsorption type oxygen production apparatus is generally used as a supply source of the oxygen. In addition to the pressure swing adsorption method, a heat swing adsorption method can be adopted. For example, Patent Document 2 discloses technical information about an apparatus that separates and manufactures a gas body selected from air related to the thermal swing adsorption type.

JP 11-159731 A JP 2003-175111 A

  As disclosed in Patent Document 1, when oxygen is used as a part of the combustion oxidant, the pressure swing adsorption type oxygen production apparatus is used as the oxygen supply source in the adsorbent regeneration or adsorption process. And a vacuum pump, the energy consumption per unit generated oxygen volume is high, and the acceptability is low from the viewpoint of running cost and energy saving. In addition, this pressure swing adsorption type oxygen production apparatus uses an adsorbent that selectively adsorbs nitrogen that occupies 79% of the air and separates it from oxygen, which requires a large amount of adsorbent. Thus, there is a problem that the initial cost is increased, such as an increase in the volume of the adsorption tower.

  Further, in the case of the thermal swing adsorption type, as seen in Patent Document 2, the purge gas for heating and desorption is heated by using a separate heat source, and the electric heater is also used in other general thermal swing adsorption types. However, there is a problem that the running energy increases due to an increase in heat energy (power consumption) required for the heating.

  The present invention has been made to solve such problems. In a combustion facility, high-concentration oxygen is obtained by using the heat of the combustion exhaust gas, and the oxygen and the combustion exhaust gas are mixed and burned. Combustion that is used as an oxidant to improve combustion efficiency and heat recovery efficiency, and to provide a combustion method in a combustion facility that can suppress NOx generated by combustion, and to achieve the object The purpose is to provide equipment.

In order to achieve the above object, a combustion method in a combustion facility according to the first invention comprises:
It is obtained by using the heat of exhaust gas after recovering heat by burning fuel in a combustion facility, and desorbing oxygen from an adsorbent that selectively adsorbs oxygen in the air by a thermal swing adsorption method. Oxygen is mixed with a part of the exhaust gas after heat recovery and supplied to the combustion furnace as a combustion oxidant.

A combustion facility that uses the combustion method according to the second aspect of the invention comprises:
In combustion equipment, heat-recovered exhaust gas is used as a heating source of the temperature rising purge gas of the heat swing adsorption oxygen production apparatus, and oxygen obtained in the oxygen production apparatus and a part of the exhaust gas after heat recovery are mixed, It is configured to be supplied as a combustion oxidant in the combustion section.

  In the second aspect of the invention, the exhaust gas after the acid gas component and dust are removed in the combustion exhaust gas treatment section is used as a heating source for the temperature rising purge gas of the thermal swing adsorption type oxygen production apparatus, and a part thereof is mixed. It is good to mix with the oxygen produced | generated with the thermal swing adsorption type oxygen manufacturing apparatus, and to make it a combustion oxidizing agent (3rd invention).

  In the second or third aspect of the invention, a control valve is provided in a branch path for mixing a part of the combustion exhaust gas with oxygen generated by a thermal swing adsorption oxygen production apparatus, and the exhaust gas and oxygen It is preferable that the mixing ratio is controlled (the fourth invention).

  In the inventions 2 to 4, it is preferable to provide a dehumidifier or a heater in the supply line for the exhaust gas mixed with oxygen (fifth invention).

  In the second invention, the combustion facility may be a waste incinerator (sixth invention).

  Furthermore, in the second invention, the combustion facility may be a gasification facility such as coal or biomass (seventh invention).

  According to the combustion method of the first aspect of the present invention, a thermal swing adsorption type oxygen production apparatus is provided in the combustion facility, and the exhaust gas after heat recovery is used for heating the purge gas of the thermal swing adsorption type oxygen production apparatus. By mixing a part and supplying it as a combustion oxidant to the combustion part, since the oxidant does not contain nitrogen, the production of NOx can be suppressed. Further, by mixing a part of the exhaust gas with oxygen as an oxidant, the temperature of the combustion chamber can be adjusted, and the combustion efficiency can be improved by preventing the furnace body from being damaged. Furthermore, there is an advantage that the amount of exhaust gas as a combustion facility can be reduced to the same extent as pure oxygen combustion.

  According to the combustion equipment of the 2nd invention, there exists the same operation effect as the 1st invention. Further, since the partial pressures of carbon dioxide and moisture (water vapor) in the combustion gas are high, the radiation performance is high even at the same temperature, and the heat recovery efficiency is high. Therefore, the boiler as the heat recovery device can be made compact. In addition, since the oxygen generator (oxygen production device) is a heat swing adsorption type, the heat of exhaust gas after heat recovery by a boiler can be used, and a high pressure blower like the pressure swing type generally used conventionally. Alternatively, there is an advantage that power equipment such as a compressor and a vacuum pump is not necessary, equipment cost and operation cost can be reduced, and an economic effect can be enhanced.

  According to the third aspect of the present invention, after the exhaust gas from the combustion chamber is heat-recovered, dust such as dust is removed by the dust removing device, so that the heater of the temperature-up purge gas of the heat swing adsorption type oxygen production device As a heat source, a clean gas can be obtained, and the flow inhibition of the pipe line or the like in the mixing process can be eliminated, and the clean gas can be finally supplied as a combustion oxidant.

  Further, by adopting the configuration of the fourth invention, the amount of exhaust gas for diverting the oxygen concentration of the obtained combustion oxidant can be controlled and changed by a control valve (flow rate control valve), so that oxygen enriched combustion can be achieved. It can be used to perform proper combustion, and the combustion efficiency can be improved.

  In addition, by adopting the configuration of the fifth invention, it is possible to prevent moisture in the exhaust gas from being condensed when oxygen and a part of the exhaust gas are mixed.

  Furthermore, in the sixth invention, by using this invention for a waste incinerator, it is possible to reduce the scale of the incidental equipment, and there is an effect that the equipment cost and the running cost can be reduced.

  In the seventh invention, the present invention can be used for gasification equipment such as coal or biomass, whereby the calorific value per unit gas amount of the obtained gas can be increased.

  Next, a combustion method for a combustion facility according to the present invention and a combustion facility for carrying out the combustion method will be described with reference to the drawings of the embodiment.

  FIG. 1 is a block diagram showing a flow of a combustion method according to the present invention. FIG. 2 shows a schematic diagram of a combustion facility according to the present invention, and FIG. 3 shows a schematic diagram of a thermal swing adsorption type oxidizer manufacturing apparatus using combustion exhaust gas.

  As shown in FIG. 1, the combustion facility 10 of the present embodiment is configured such that combustion exhaust gas generated by combustion with the fuel gas and combustion oxidant supplied to the combustion furnace 1 a in the combustion unit 1 is generated by the exhaust gas treatment facility 2. Acid gas components, dust, and other solid components in the exhaust gas are separated and removed, and the treated exhaust gas is sent to the heating unit 34 of the heat swing adsorption oxygen production apparatus 3 to use the exhaust heat, and the heat swing adsorption oxygen production It is used to heat a part of desorbed oxygen used as a temperature rising purge gas in the apparatus 3, and the exhaust gas is sent to the chimney 5 to be diffused into the atmosphere. On the other hand, in the thermal swing adsorption type oxygen production apparatus 3, oxygen is adsorbed and separated from the supplied air by an adsorption bed, oxygen is taken out, mixed with a part of the exhaust gas sent to the chimney 5, and burned as a combustion oxidant It is configured to be supplied to the furnace 1a.

  As the combustion unit 1, for example, a boiler 1b is applied. In this boiler 1b, LPG (for example, propane gas) is used as fuel in the combustion furnace 1a, and an air-fuel mixture of oxygen, heat recovery, and exhaust gas after exhaust gas treatment, which will be described later, is used as a combustion oxidant. The steam obtained by recovering heat with the boiler 1b is sent to a target location by a known means. The combustion exhaust gas generated in the combustion furnace 1a is sent to the next exhaust gas treatment facility 2 where acid gas component removal and dust removal are performed.

  The exhaust gas treatment facility 2 for treating the combustion exhaust gas is provided with a device for performing a temperature reduction process for reducing the exhaust gas temperature and a dust removal process. All of these are of a known configuration (the specific configuration is omitted), and the exhaust gas recovered by heat is guided to the temperature reduction treatment tower 22 to be cooled, so that the dust removal operation in the next step is possible. Reduced to temperature.

  The exhaust gas subjected to the temperature reduction treatment is sent to, for example, a bag filter 23 for dust removal treatment, and soot and dust held by the bag filter 23 are removed. The exhaust gas thus removed is sent to a thermal swing adsorption type oxygen production apparatus 3 which is the next step, and is used for heating the temperature rising purge gas. The solid content removed in the dust removal process is taken out from the lower part of the bag filter 23 and is carried to the collection position by the conveyor 24 for processing.

  As the thermal swing type oxygen production apparatus 3, for example, an apparatus as shown in FIG. 3 is adopted. This thermal swing type oxygen production apparatus 3 (hereinafter referred to as TSA3) includes a moisture absorption bed 32 for removing moisture in the air from the air sent by the blower 31, three adsorption towers 33a, 33b, and 33c, A heater 34 for the warm purge gas, an exhaust gas dehumidifier 52 for removing excess moisture in the exhaust gas branched for mixing, which will be described later, a buffer tank 51 for receiving the generated concentrated oxygen, and a mixture for making a combustion oxidant It is comprised with the container 54 and the pipe line which connects them.

  The moisture-absorbing bed 32 has a configuration in which air at normal temperature is introduced and cooled by heat exchange means using, for example, cooling water to remove moisture in the air. From the outlet of the moisture absorbing bed 32, a branch line 41 connects to the lower inlets 33 'of the three adsorption towers 33a, 33b, 33c.

  Each of the three adsorption towers 33a, 33b, and 33c has an adsorption bed (not shown) formed therein, and the dry adsorbed moisture passes from the lower part toward the upper part by the filled adsorbent. Oxygen is selectively adsorbed, and other gas components (mainly nitrogen) are discharged out of the system through the upper outlet 33 ″. The adsorbent filled as the adsorbent bed has an adsorption selectivity of oxygen / nitrogen. The adsorbent may be in the form of granules or pellets, and is stored in a uniformly dispersed state on a honeycomb or fin-like support. As the adsorbent, for example, a metal complex adsorbent, zeolite or the like is employed.

  In addition to the air supply pipe 41, a concentrated oxygen separation pipe 42 is connected to the lower inlet 33 'of each of the adsorption towers 33a, 33b, 33c thus formed. Valve portions 35a, 35b, and 35c are provided at the respective portions. Further, valves 36a, 36b, and 36c are provided at the branch portions of the pipe line 42, respectively. Further, the lower inlet 33 ′ is connected to a discharge pipe 43 for the residual air in the tower, and valves 37 a, 37 b, and 37 c are provided at the connections to the pipe 43, respectively.

  On the other hand, a purge gas supply pipe 45 is branched and connected to the upper outlets 33 ″ of the adsorption towers 33a, 33b, and 33c. Valves 38a, 38b, and 38c are arranged in the branched pipes. Valves 39a, 39b, and 39c are also disposed in the exhaust pipe 44 for a gas such as nitrogen that is a difficult-to-adsorb component that is selectively separated and removed by the adsorption tower 33 (generally 33). The exhaust pipe 44 is provided with a valve 46, and the exhaust pipe 43 is provided with a check valve 47.

  The generated oxygen is boosted by a booster 55 provided in the pipe line 42 and sent to the buffer tank 51, and a part of oxygen is used as a purge gas sent to the adsorption tower 33, and is branched from the oxygen take-out pipe line 42. A heater 34 is disposed in the purge gas supply pipe 45, and the exhaust gas treated by the exhaust gas treatment facility 2 is supplied as a heating medium of the heater 34. Since a part of the generated oxygen is used as the purge gas, a control valve 48 'is provided in the pipe 45, and a valve is provided in the oxygen extraction pipe 42 to the buffer tank 51 for storing the generated oxygen. 48 are respectively provided.

  The secondary combustion exhaust gas pipe 49 of the heater 34 is branched into a discharge pipe to the chimney 5 and a pipe 49 'for use as an air-fuel mixture. The pipe 49' has a control damper 53 and A dehumidifying device 52 and a recirculating fan 57 are provided and connected to the mixer 54. The oxygen stored in the buffer tank 51 is connected to the mixer 54 by a pipe 59, and a control valve 58 for adjusting the amount of oxygen is provided in the pipe 59. In the mixer 54, the concentrated oxygen and a part of the exhaust gas supplied through the pipe line 49 'are received and mixed, and supplied to the combustion furnace as a combustion oxidant.

  In the combustion facility of the present embodiment configured as described above, after the combustion exhaust gas generated in the combustion section 1 is recovered by heat, it is introduced into the temperature reducing tower 22 in the exhaust gas treatment facility 2 and the next step of dust removal treatment is performed. Reduced to possible temperature. The temperature-reduced exhaust gas is sent into a bag filter 23 which is a dust removing device to collect solid contents such as dust contained therein and sent to the next process. The exhaust gas thus processed in the exhaust gas treatment facility 2 is sent to the heater 34 in the TSA 3 as a heat medium and used to heat the temperature-up purge gas.

  In TSA3, as shown in FIG. 3, normal temperature air is sent to the moisture absorption bed 32 by the blower 31, and the dry air from which moisture contained in the air is removed is sent to the adsorption towers 33a, 33b, 33c. In this TSA3, first, the valve 35a of the pipe line 41 is opened, and the dry air is sent into the inner and lower parts of the first adsorption tower 33a. The air that is fed in comes into contact with the adsorbent in the adsorption bed while ascending the inside of the adsorption tower, and oxygen is selectively adsorbed. Nitrogen, which is a difficult adsorbent, is opened in the valve 39a of the adsorption tower upper outlet 33 ″. To the outside through the pipe 44. In the tower of the first adsorption tower 33a, the rising air adsorbs oxygen by the adsorbent in the adsorption bed, the adsorbent reaches oxygen adsorption saturation, and the adsorption tower outlet 33 ″. Immediately before the oxygen concentration increases, the upper valve 39a and the lower valve 35a are closed.

  Next, the valve 35b of the lower inlet 33 'side pipe 41 of the second adsorption tower 33b is opened to introduce air into the tower, and the adsorption separation operation is performed in the same manner as in the first adsorption tower 33a. Make it. Thus, when the adsorption separation operation by the second adsorption tower 33b is started, the first adsorption tower 33a shifts to a heating process. In the steady state, a part of oxygen desorbed by the temperature rise is sent to the heater 34 through the pipes 42 and 45, and heat exchange is performed with the combustion exhaust gas treated in the exhaust gas treatment process so that the oxygen is heated and heated. Oxygen is fed into the adsorption tower 33a that has been completely adsorbed by opening the valve 38a at the top of the adsorption tower, and the temperature rising purge process is started. At the time of start-up, an oxygen cylinder or the like is sent to the heater 34 through the valve 56 'and heated to be introduced into the adsorption tower 33a. At this time, the concentrated oxygen remaining in the buffer tank 51 may be used by opening the valves 56 and 56 '. In the heater 34, an exhaust gas of about 150 to 300 ° C. can be used as a heat source as the treated combustion exhaust gas.

  In the temperature rising purge process, since residual air exists in the adsorption tower 6a in the initial stage, the valve 37a disposed at the lower part of the adsorption tower 33a is opened while the residual air is pushed out from the start of the purge. It is discharged out of the system from the pipe 44 via a check valve 47 provided in the path 43. Thus, when pushing out of the remaining air is completed, the valve 37a is closed and the valve 36a of the oxygen take-out pipeline 42 is opened to introduce the desorbed oxygen into the buffer tank 51. At this time, a valve 48 ′ provided in the purge gas pipe 45 is adjusted so that a part of the oxygen obtained for the partially heated purge is sent to the heater 34.

  The concentrated oxygen obtained in this way is given sensible heat at the time of desorption by the temperature rising purge gas heated in the heater 34, taken out at a temperature of about 60 to 120 ° C., and stored in the buffer tank 51. .

  After the temperature raising purge process of the first adsorption tower 33a is completed, the process proceeds to the cooling regeneration process, the second adsorption tower 33b moves to the temperature raising purge process, and the third adsorption tower 33c enters the adsorption process. enter. The operations in the second and third adsorption towers 33b and 33c are the same as the operations in the first adsorption tower 33a. In the cooling regeneration process in the first adsorption tower 33a, since oxygen used for the temperature raising purge remains, the valve 39a is opened at the initial stage of the cooling regeneration process, and the valve 36a is opened to open the third stage. The air or nitrogen that has passed through the adsorption tower 33c is introduced into the tower to push out residual oxygen. When this extrusion operation is completed, the valve 36a is closed, the valve 35a is opened, dry air is introduced into the tower, and the adsorption bed is cooled and regenerated.

  In parallel with this operation, in the second adsorption tower 33b in the temperature raising purge process, the valves 35b and 39b are closed, the valves 38b and 37b are opened, and the extrusion of the residual air in the tower is started. When the pushing out of the residual air is completed, the valve 37b is closed and the valve 36b is opened, and the process proceeds to the temperature rising purge step with the above capacity. Thereafter, this operation is sequentially repeated in each of the first to third adsorption towers 33a, 33b, and 33c to continuously perform oxygen enrichment generation.

  In this manner, in the TSA 3, the three adsorption towers 33a, 33b, and 33c can be operated repeatedly, and oxygen generation can be performed without interruption. The oxygen thus obtained is stored in the buffer tank 51 and supplied to the combustion furnace 1a as a fuel oxidant. However, since only oxygen is high-temperature combustion, it is mixed with the treated combustion exhaust gas and supplied. .

  A mixer 54 is used to mix the treated flue gas with the oxygen produced by TSA3. As the mixer 54, for example, a tank for dividing the tank into a plurality of compartments and having a plurality of small-diameter through holes formed in the partition walls, a pipe for supplying oxygen and the combustion exhaust gas are supplied. Both gas bodies are opened in parallel with a pipe to be opened, once flowed into one of the compartments, opened, passed through the partition wall and into the other compartment. Mixing in a turbulent state by repeated compression-release and then discharging through a small diameter tube is effective to speed up the mixing.

  In addition, the mixer may be configured to pass through a chamber partitioned by a number of baffle plates for mixing.

  The oxygen mixed by the mixer 54 and the combustion exhaust gas as described above have a constant excess air ratio with respect to the fuel supplied to the combustion chamber 1 by the control valve 58 with respect to the amount of oxygen extracted from the buffer tank 51. By controlling the amount of exhaust gas to be mixed by the control damper 53 in the pipe 49 'as described above, the combustion temperature in the combustion furnace 1a can be adjusted to an appropriate range. In addition, if the moisture contained in the exhaust gas is large and it is necessary to avoid draining if the moisture contained in the exhaust gas before mixing is operated by operating the dehumidifying device 52 provided in the pipe line 49 ′, It is effective. Moreover, it is good also as a heater instead of a dehumidifier.

  If the combustion method of this embodiment is adopted, the heat of combustion exhaust gas can be used effectively, and the amount of exhaust gas finally discharged from the chimney should be reduced to the same extent as when burning with pure oxygen. Is possible. In addition, when the combustibles are miscellaneous such as waste, the generation of harmful gas components and dust should be removed in the exhaust gas treatment facility to remove the acidic gas components and dust, and the exhaust gas used thereafter. To. In this case, although it is trace amount, components other than oxygen, carbon dioxide, and moisture are also present. When the combustion product (fuel) contains a nitrogen component, NOx production can be suppressed by performing two-stage combustion in a combustion furnace. Therefore, it can be applied to an incinerator.

  Moreover, according to this invention, it is possible to raise the emitted-heat amount per unit gas amount of the product gas obtained by applying to the partial combustion gasification part in coal and biomass gasification facilities.

  In addition, since the combustion oxidant in the combustion section is generated as a combustion facility by a heat swing adsorption type oxygen production apparatus using the combustion exhaust gas, the energy required for oxygen production can be reduced, and the equipment cost and running cost can be reduced. There is an advantage that it can be remarkably reduced. Further, the nitrogen separated and removed in the oxygen production apparatus can be commercialized as nitrogen gas in addition to the atmospheric emission. When commercialized, the effect as a secondary product can be obtained.

The block diagram showing the flow of the combustion method concerning this invention Overview of combustion equipment according to the present invention Schematic diagram of thermal swing adsorption oxidizer manufacturing equipment that uses combustion exhaust gas Flow chart of conventional combustion system

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Combustion furnace 1a Combustion part 1b Heat recovery part 2 Exhaust gas treatment equipment 3 Thermal swing adsorption type oxygen production apparatus (TSA)
5 Chimney 33 Adsorption tower 34 Heater 51 Buffer tank 54 Mixer

Claims (7)

  It is obtained by using the heat of exhaust gas after recovering heat by burning fuel in a combustion facility, and desorbing oxygen from an adsorbent that selectively adsorbs oxygen in the air by a thermal swing adsorption method. A combustion method for a combustion facility, wherein oxygen is mixed with a part of exhaust gas after heat recovery and supplied to a combustion furnace as a combustion oxidant.   In combustion equipment, heat-recovered exhaust gas is used as a heating source of the temperature rising purge gas of the heat swing adsorption oxygen production apparatus, and oxygen obtained in the oxygen production apparatus and a part of the exhaust gas after heat recovery are mixed, A combustion facility configured to be supplied as a combustion oxidant in a combustion section.   Exhaust gas after removing acid gas components and dust in the flue gas treatment section is used as a heating source for the temperature rising purge gas of the thermal swing adsorption type oxygen production device, and then a part of it is sent to the mixer for thermal swing adsorption. The combustion equipment according to claim 2, wherein the combustion oxidant is mixed with oxygen produced by the oxygen generator.   A branch valve for mixing a part of the combustion exhaust gas with oxygen generated by a thermal swing adsorption type oxygen production apparatus is provided with a control valve, and is configured to control a mixing ratio of the exhaust gas and oxygen. Item 4. The combustion facility according to Item 2 or 3.   The combustion equipment according to any one of claims 2 to 4, wherein a dehumidifier or a heater is provided in a supply pipe for exhaust gas mixed with oxygen.   The combustion facility according to claim 2, wherein the combustion facility is a waste incinerator.   The combustion facility according to claim 2, wherein the combustion facility is a gasification facility such as coal or biomass.

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