WO2003093728A1 - Procede d'exploitation d'un incinerateur de dechets et incinerateur de dechets correspondant - Google Patents

Procede d'exploitation d'un incinerateur de dechets et incinerateur de dechets correspondant Download PDF

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Publication number
WO2003093728A1
WO2003093728A1 PCT/JP2003/002623 JP0302623W WO03093728A1 WO 2003093728 A1 WO2003093728 A1 WO 2003093728A1 JP 0302623 W JP0302623 W JP 0302623W WO 03093728 A1 WO03093728 A1 WO 03093728A1
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WO
WIPO (PCT)
Prior art keywords
temperature
gas
waste incinerator
waste
combustion
Prior art date
Application number
PCT/JP2003/002623
Other languages
English (en)
Japanese (ja)
Inventor
Minoru Suzuki
Teruo Tatefuku
Satoshi Matsui
Takashi Noto
Masaaki Nishino
Original Assignee
Jfe Engineering Corporation
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
Priority claimed from JP2002237022A external-priority patent/JP3995237B2/ja
Priority claimed from JP2002237023A external-priority patent/JP3989333B2/ja
Priority claimed from JP2002237024A external-priority patent/JP2004077014A/ja
Application filed by Jfe Engineering Corporation filed Critical Jfe Engineering Corporation
Priority to EP03710255A priority Critical patent/EP1500875A4/fr
Priority to KR1020047017549A priority patent/KR100660757B1/ko
Publication of WO2003093728A1 publication Critical patent/WO2003093728A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/50—Control or safety arrangements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/101—Arrangement of sensing devices for temperature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/103—Arrangement of sensing devices for oxygen

Definitions

  • the present invention relates to a method for operating a waste incinerator for incinerating waste such as general waste, industrial waste, and sewage sludge, and a method for operating this waste incinerator. It relates to a waste incinerator suitable for implementation.
  • BACKGROUND ART Grate or fluidized bed waste incinerators are widely used as incinerators for incinerating waste such as municipal solid waste.
  • Figure 1 shows a typical example.
  • the waste 32 put into the hopper 31 is sent to a drying strike 33 through a chute, dried by air from below and radiant heat in the furnace, and heated to ignite.
  • the refuse 32 that has ignited and started burning is sent to a combustion stove 34 where it is pyrolyzed and gasified by combustion air sent from below, and part of it is burned. In addition, the unburned components in the waste are completely burned by the post-combustion force of 35. The ash remaining after the combustion is taken out of the main ash chute 36.
  • the combustion takes place in the combustion chamber 37, and the generated combustion gas is discharged separately to the main flue 39 and the secondary flue 40 due to the presence of the intermediate ceiling 38.
  • Exhaust gas passing through the main flue 39 contains little flammable gas and contains about 10 or more oxygen.
  • the flue gas passing through the secondary flue 40 contains about 8 combustible gases. These gases are mixed in the secondary combustion chamber 41, secondary combustion is performed, and the combustible gas power is completely burned.
  • the exhaust gas from the secondary combustion chamber 41 is sent to a waste heat poiler 43, and after being subjected to heat exchange, is discharged outside through a cooling tower, a bag filter and the like.
  • Japanese Patent Application Laid-Open No. 11-211044 discloses a method in which a high-temperature gas generated by a regenerative burner is blown into a combustion chamber or a secondary combustion chamber of an incinerator.
  • Japanese Patent Application Laid-Open No. 11-223323 discloses a method in which a high-temperature gas generated by a regenerative burner is blown into a furnace at a temperature of 800 ° C. or more. -All of these technologies are aimed at reducing flammable gases and harmful substances containing large amounts of CO and aromatic carbon in exhaust gas generated in incinerators.
  • the ratio (air ratio) obtained by dividing the actual air amount by the theoretical air amount required for waste combustion is about 1.7 to 2.0. This is larger than the air ratio required for normal combustion: 1.05-: L.2.
  • the reason for this is that the waste has a large amount of non-combustible and non-homogeneous materials, so a large amount of air is required for combustion.
  • the air ratio increases, the amount of exhaust gas also increases, and a larger exhaust gas treatment facility is required compared to a normal combustion furnace.
  • the air ratio is reduced, the amount of exhaust gas will be reduced, and the exhaust gas treatment equipment will be compact, As a result, the entire waste incineration facility can be reduced in size and equipment costs can be reduced. Also, the amount of chemicals used for exhaust gas treatment can be reduced, so that operating costs can be reduced. Furthermore, since the amount of heat lost due to heat recovery cannot be reduced, the heat recovery rate of the waste heat poiler can be improved, and the power generation efficiency of waste power generation can be increased accordingly.
  • the present invention relates to a method of operating a waste incinerator in which high-temperature gas is blown into a combustion chamber, particularly an operation method capable of sufficiently reducing harmful substances such as ⁇ and CO while performing low air ratio combustion, and an operation method thereof.
  • the purpose is to provide a waste incinerator suitable for performing.
  • This object is achieved by the following methods of operating a waste incinerator i) to: Lv).
  • High-temperature gas containing at least one of carbon dioxide and water vapor and oxygen and having a temperature of 200 ° C or more and satisfying the following equation (2) is burned by a waste incinerator.
  • a method for operating a waste incinerator comprising a step of injecting a high-temperature gas having a temperature T [° C] satisfying the following expression (4) into the combustion chamber of the waste incinerator.
  • FIG. 1 is a diagram showing an example of a conventional waste incinerator.
  • FIG. 2 is a diagram showing the relationship between the temperature of the high-temperature gas blown into the furnace and the oxygen concentration.
  • FIG. 3 is a diagram showing one example of the waste incinerator of the present invention.
  • FIG. 4 is a diagram showing a partial cross section of FIG.
  • FIG. 5 is a diagram showing an example of an exhaust gas circulation system in the waste incinerator of the present invention.
  • FIG. 6 is a diagram showing another example of the exhaust gas circulation system in the waste incinerator of the present invention.
  • FIG. 7 is a diagram showing the relationship between the temperature of the high-temperature gas blown into the furnace and the oxygen concentration.
  • FIG. 8 is a diagram showing the relationship between the temperature of the high-temperature gas blown into the furnace and the oxygen concentration.
  • FIG. 9 is a diagram showing the relationship between the temperature of the high-temperature gas blown into the furnace and the oxygen concentration.
  • the inventors investigated the relationship between the CO and NOx generated in the combustion chamber, the oxygen concentration in the high-temperature gas blown into the combustion chamber, and the temperature of the high-temperature gas in the waste incinerator. That As a result, as shown in Fig. 2, if the oxygen concentration in the hot gas and the temperature of the hot gas are controlled in the region surrounded by the A, B, and C lines, CO and NOx in the exhaust gas can be reduced at the same time. I found what I could do.
  • the temperature of the hot gas that achieves both low NOx and low CO is in the range of 280-500.
  • the temperature of the hot gas that achieves both low NOx and low CO is in the range of 200 to 330 ° C.
  • the space where 400 or more and flammable gas exists is the area where the thermal decomposition of waste is promoted or the area where the thermal decomposition of waste is completed. This is the area where gas is generated and the cap flame exists.
  • thermal decomposition of paper waste starts at about 250 ° C and completes at about 400 ° C. Pyrolysis of plastic waste begins at about 400 and is completed at about 500 ° C.
  • the blowing region of the high-temperature gas is 400 ° C. or more, and the space is where the flammable gas exists.
  • high-temperature gas is preferably injected into the area where a large amount of flammable gas is present. From the combustion start area to the main combustion area.
  • the combustion start region is a region in which combustible gas is generated by thermal decomposition or partial oxidation of the waste, and combustion of the waste starts.
  • the main combustion area is the area in which waste is thermally decomposed, partially oxidized and burned, generates flammable gas, and burns with a flame, and the combustion with the flame is completed. This is the area up to the point (burnout point). Therefore, it is preferable to set the high-temperature gas blowing region from the combustion start region to the main combustion region.
  • the combustion start area is the space above the dry grate
  • the main combustion area is the space above the combustion grate.
  • the primary air is the combustion air blown from the wind box below the grate in the case of a grate furnace, or the air box below the fluidized bed in the case of a fluidized bed furnace.
  • the amount of high-temperature gas blown be 10 to 70% of the amount of primary air for the following reasons. If the amount of high-temperature gas injected is less than 10 times the amount of primary air, the momentum required for stirring the gas in the furnace is not provided, and the effect of high-temperature gas injection may not be fully exerted.
  • the air volume is 10 to 70. The theoretical air volume is determined based on the nature of the waste.
  • Combustible gases generated from waste usually flow upward. Therefore, when the hot gas is injected in the upward direction, the flow of the combustible gas and the flow of the hot gas have the same velocity component in the same direction, and the effect of stirring and the effect of retaining the flow of the combustible gas are small. Summer Thus, the effect of hot gas injection is reduced. On the other hand, if the blowing direction of the high-temperature gas is horizontal or downward, the rising flammable gas and high-temperature gas are well stirred, and the flow of the flammable gas can be retained. The blowing effect can be further enhanced.
  • the stirring effect can be enhanced, and the blowing effect of high-temperature gas can be further enhanced.
  • injecting the hot gas as a swirl flow means that the hot gas itself flowing out of the outlet is a swirl flow or the flow of the hot gas flowing out of a plurality of outlets is a composite. Including swirling flow.
  • the above-described method for operating a waste incinerator according to the present invention includes an exhaust gas circulating device that circulates exhaust gas into the furnace and blows the exhaust gas into the furnace. Grate or fluidized bed waste incinerator equipped with a device that adjusts the properties of oxygen and adjusts the oxygen concentration and temperature in the high-temperature gas blown from the combustion start zone in the furnace to the main combustion zone. Therefore, it can be easily realized.
  • combustion chamber height is the height of the space in which the main combustion takes place, and refers to the height from the grate or fluidized bed to the furnace ceiling or the position where the secondary combustion air is blown.
  • FIG. 3 shows an example of the waste incinerator of the present invention.
  • a hopper 2 for charging the waste 3 into the combustion chamber 1 On one side of the combustion chamber 1 (on the left side in FIG. 3), a hopper 2 for charging the waste 3 into the combustion chamber 1 is provided.
  • a grate (storage force) for burning the waste 3 while moving the waste 3 is provided so as to be inclined downward as the distance from the hopper 2 increases.
  • This grate has two steps and is divided into three parts. These three grate, from the side closer to the hopper 2, the dry strike 4, the combustion strike 5, and after It is called the combustion strike power 6.
  • drying strike 4 drying and ignition of waste 3 are mainly performed.
  • combustion strike 5 waste 3 is mainly burned, but waste 3 is burned and thermally decomposed, and combustible gas is released together with the combustion gas.
  • the combustion of the waste 3 is substantially completed in the combustion strike 5.
  • the combustion residue after complete combustion is discharged from the main ash chute
  • each grate there is provided a wind box 8 connected to a supply pipe for supplying combustion air.
  • a main flue 9 and a secondary flue 10 are provided below and above the combustion chamber 1 on the opposite side of the hopper 2, a main flue 9 and a secondary flue 10 are provided. These include a waste heat boiler that is part of the gas cooling system; A combustion chamber 12 is provided connected. In the combustion chamber 1, a barrier (intermediate ceiling) 13 for dividing the combustion gas is provided near the exit of the combustion chamber 1, and the flow of the combustion gas is divided into a main flue 9 and a sub-flue 10. Shedding.
  • the waste 3 is put into the combustion chamber 1 from the hopper 2, and the combustion air is supplied to the waste 3 moving on the grate through the supply pipes and the wind box 8, and the waste 3 is dried. Burn.
  • a nozzle 14 is provided on the side wall of the combustion chamber 1, and a high-temperature gas at a temperature of 200 ° C. or more and satisfying the above formula (1) is blown into the combustion chamber 1 from the nozzle 14.
  • the nozzle 14 is installed at the upper part of the drying stove 4 and at the upper left of the combustion stove 5.
  • waste 3 is incinerated, first, water evaporates, followed by thermal decomposition and partial oxidation.
  • the thermal decomposition reaction occurs at a temperature of about 200, and is almost completed when the temperature reaches about 400 ° C.
  • Nozzles 14 are provided at the part of the drying stove 4 (the latter part) and the former part of the combustion stove 5 to blow hot gas.
  • the pyrolysis reaction can be completed at a higher temperature.
  • a nozzle 14 may be provided downstream (right side in the figure) from the position shown in FIG. preferable.
  • the nozzle 14 is preferably provided at a height not exceeding 1/2 of the height of the combustion chamber.
  • the hot gas is blown into the area where the secondary flue gas containing a large amount of combustible gas and the main flue gas are mixed, that is, above the intermediate ceiling 13 and into the entrance of the secondary combustion chamber 12. May be provided at the side wall, ceiling, intermediate ceiling 13, and entrance to the secondary combustion chamber 12.
  • the amount of high-temperature gas blown should be as small as possible in consideration of exhaust gas treatment. However, if the injection amount is small, CO is likely to be generated, and complete combustion cannot be achieved. For this reason, as described above, it is preferable that the amount of primary air blown from the wind box 8 be 10 to 70 times. As a result, the generation of CO can be suppressed to an acceptable level. Therefore, it is preferable to control the amount of CO and NOX emitted while adjusting the amount of air blown within the range of 10 to 70 times the amount of primary air. In particular, depending on the type of waste 3, the amount of primary air injected may be less than the theoretical amount of air required to burn waste 3, in which case a large amount of hot gas is injected.
  • the amount of primary air to be injected is small, as mentioned above, the amount of hot gas to be injected should be in the range of 10 to 70% of the theoretical air amount required to burn waste 3. You may make it become.
  • the nozzle 14 When the nozzle 14 is provided horizontally or downward, the flow of the flammable gas in which the high-temperature gas ejected from the nozzle rises can be retained, and the combustion of the flammable gas can be promoted. In order to promote the stagnation effect, it is preferable to set the nozzle downward.However, if the angle is too large, the high-temperature gas will not reach the entire furnace width direction. It is particularly preferred to do so.
  • FIG. 4 to show the arrangement of the nozzles in FIG. 3, A- A 'cross-sectional view (horizontal cross-section: Figure 4A, Figure 4B), BB' of FIG. 3 a cross-sectional view (vertical cross-section: Figure 4 C) shows a.
  • FIG. 4 structures not related to the present invention are omitted.
  • FIG. 4A high-temperature gas 19 is ejected from a pair of nozzles 14 provided in the width direction of the furnace wall 17 and collides with each other at the center of the furnace. Therefore, the movement of the gas in the furnace is slow and a stagnant stagnation region 15 is formed at the center of the furnace, so that combustion is stably performed.
  • FIG. 4B shows another example, in which the nozzles 14 are oriented such that their central axes are parallel to each other.
  • the hot gases 19 are separated by a predetermined distance at the center of the furnace and pass each other at a predetermined distance. Therefore, a swirl zone 20 is formed in the center of the furnace.
  • a stagnation region 15 or a swirl region 20 is formed in the center of the furnace when viewed in plan. Therefore, as described above, the flame is stabilized and the mixing of the gases is promoted.
  • the size of the stagnation region 15 can be controlled by changing the flow velocity of the hot gas ejected from the two nozzles 14 in the same manner. Further, by providing a difference in the flow velocity of the high-temperature gas ejected from both nozzles 14, the position of the furnace in the stagnation region 15 in the left-right direction can be changed. Further, by changing the direction of the nozzle 14 in the same direction as the furnace length direction, the position of the stagnation region 15 in the furnace length direction can be changed.
  • FIG.4C the vertical cross section of the furnace is shown, but the hot gas 19 blown out from the nozzles 14 provided downward on the furnace walls 17 on both sides collides with the rising combustible gas 21 to form a stagnation region 15. Is shown. In the stagnation region 15, stable combustion is performed as a result of stable combustion. As a result, unlike the prior art, even in the low air ratio combustion, the combustion instability in the combustion start region is not amplified, soot generation is suppressed, and uniform and stable combustion can be expected.
  • blowing the high-temperature gas to sufficiently stir the gas near the furnace side wall also has the effect of stabilizing the combustion
  • the flame in the furnace when the high-temperature gas is not blown is a bright flame, but when the high-temperature gas is blown into the furnace properly as described above, the flame in the furnace becomes a transparent flame, and the furnace wall Strike). This is considered to be due to the slow burning of combustible f raw gas due to the injection of high-temperature gas. Therefore, it is also possible to observe the transparency of the flame in the furnace and use it as a criterion for determining whether or not the high-temperature gas is properly blown.
  • the above embodiment is effective in reducing trace harmful substances such as CO, NOx, and dioxin.
  • FIG. 3 shows a furnace having an intermediate ceiling 13
  • the present invention can be applied to a furnace without such an intermediate ceiling.
  • high-temperature gas is blown into the combustion chamber 1
  • high-temperature gas may be blown into the secondary combustion chamber 12.
  • the hot gas may be blown from one side of the furnace. It can also be blown from the middle ceiling or ceiling, rather than from the side of the furnace.
  • Recirculated exhaust gas is a part of the exhaust gas discharged from a waste incinerator, and returning it to the combustion chamber has the effect of reducing harmful substances and reducing the amount of exhaust gas.
  • the circulating exhaust gas satisfies the conditions of the high-temperature gas of the present invention, it may be blown into the furnace as it is, but if the temperature is lower than 200 ° C and the oxygen concentration is low, a high-temperature air production device or hot air High-temperature air is produced by the furnace, mixed with the circulating exhaust gas, and blown into the furnace as a high-temperature gas satisfying the conditions of the present invention.
  • the temperature of the exhaust gas from the secondary combustion chamber 12 is sufficiently high and the oxygen concentration is high, it is used as a substitute for high-temperature air without using a high-temperature air production device, and is mixed with air. You can also blow it. Further, if the temperature of the exhaust gas from the secondary combustion chamber 12 is 200 ° C. or higher and the relationship between the oxygen concentration and the temperature satisfies the above equation (1), the exhaust gas is directly injected into the furnace. You may blow it.
  • filter type There are two types of filter type, one using a filter cloth and the other using a ceramic filter.However, when the exhaust gas temperature is high, the ceramic type filter is more excellent in durability and heat resistance. ing. Filter cloth processed with metal fibers is also effective depending on the operating temperature. In addition, a moving bed type dust remover can be used. The place where dust is removed is preferably as close as possible to the outlet because the piping before dust removal becomes shorter.
  • a heat storage burner As the high-temperature air producing apparatus, a heat storage burner, an apparatus for mixing air or oxygen with a combustion gas from a combustion burner of a hot air stove, a recuperator, or the like can be used.
  • the heat storage burner prepares a pair of heat storage bodies, heats the first heat storage body with the high-temperature exhaust gas from the combustion parner, heats the second heat storage body that has already been heated and stored, and heats it.
  • This is a device that can switch between heating of the heat storage element by high-temperature exhaust gas and heating of air by the heat storage element.
  • the high-temperature air is mixed by an ejector and blown into the furnace.
  • special moving parts such as fans for sucking the circulating exhaust gas can be used. Since no equipment is required, the device configuration is simplified and dust troubles are reduced.
  • Table 1 shows the properties of the high-temperature gas (oxygen concentration and temperature) blown into the furnace when the high-temperature gas is adjusted by mixing the burner combustion gas, dilution air, and circulating exhaust gas of the hot-blast furnace and blowing into the furnace.
  • the following shows the correspondence between operating factors and operating methods for improving the properties of the high-temperature gas blown into the furnace when it deviates from the scope of the present invention.
  • the oxygen concentration is within the scope of the present invention.
  • the combustion amount of the combustion burner is increased to increase the temperature of the high-temperature gas to be blown, the exhaust gas circulation amount is reduced, and the dilution air amount (high-temperature gas Is increased so as to be within the scope of the present invention.
  • the oxygen concentration is lower than the range of the present invention and the temperature is higher than the range of the present invention, the oxygen concentration is increased by increasing only the dilution air amount.
  • FIG. 5 shows an example of an exhaust gas circulation system in the waste incinerator of the present invention.
  • the exhaust gas from the combustion chamber 1 is guided to the waste heat poirer 11, where it is subjected to secondary combustion in the secondary combustion chamber 12, which is a part of the exhaust heat.
  • the waste gas is cleaned by the exhaust gas treatment equipment 22 and released to the atmosphere from the chimney 23.
  • a part of the exhaust gas is sucked from the downstream side of the exhaust gas treatment facility by the blower 24 and guided to the gas mixing device 25.
  • a high-temperature combustion gas such as a burner gas is introduced into the gas mixing device 25 through a high-temperature combustion gas control valve 26, and the dilution air is diluted. Introduced via air control valve 27. Then, in the gas mixing device 25, the exhaust gas, the high-temperature combustion gas, and the dilution air are mixed to adjust the high-temperature gas. This high-temperature gas is blown into the combustion chamber 1.
  • the oxygen concentration in the high-temperature gas is adjusted by the oxygen concentration adjusting device 29.
  • the opening degree of the dilution air adjusting valve 27 is adjusted so that the oxygen concentration in the high-temperature gas becomes a predetermined concentration. Further, the temperature of the high-temperature gas is adjusted by the temperature adjusting device 28. In the temperature control device 28, the opening degree of the high-temperature combustion gas control valve 26 is adjusted so that the temperature of the high-temperature gas falls within the range represented by the above equation (1). -As described above, the function of adjusting the oxygen concentration and temperature in the hot gas blown into the combustion chamber can be maintained in an appropriate range. When it is desired to adjust the flow rate and flow velocity of the high-temperature gas to be blown, the rotational speed of the blower 24 may be adjusted.
  • FIG. 6 shows another example of the exhaust gas circulation system shown in FIG. This example differs from the example shown in FIG. 5 only in that the place where the exhaust gas is taken out is the outlet of the waste heat boiler 11.
  • the exhaust gas is taken out from the rear of the exhaust gas treatment equipment 22, so that the dust in the exhaust gas has been removed and the exhaust gas is clean. However, the temperature of the exhaust gas is decreasing.
  • the circulating exhaust gas is mixed with a high-temperature combustion gas such as a burner gas and diluted air, and the high-temperature air produced by the above-described high-temperature air production apparatus is mixed with the high-temperature combustion gas.
  • a gas combustion device instead of introducing and adjusting the dilution air into the gas mixing device, the oxygen concentration of the high-temperature gas can be adjusted by adjusting the amount of air introduced into the high-temperature air production device.
  • the present inventors have also proposed that as a method of operating a waste incinerator in which a high-temperature gas is blown into a combustion chamber, the high-temperature gas contains at least one of dioxide carbon and water vapor, such as NO X and CO. It has been found to be effective in sufficiently reducing harmful substances. This is because the emissivity of carbon dioxide and water vapor is higher than that of nitrogen or oxygen, and waste and combustible gas generated from waste can be efficiently produced by heat radiation from high-temperature gas containing these gases. This is because the fuel is heated, and as a result, stable combustion is performed even when performing low air ratio combustion.
  • the temperature of the hot gas that achieves both low ⁇ and low CO is in the range of 200 to 550 ° C.
  • the temperature of the hot gas that achieves both low NOx and low CO is in the range of 200 to 400 ° C.
  • exhaust gas discharged from a combustion furnace as a high-temperature gas containing at least one of carbon dioxide and water vapor.
  • the high-temperature gas blowing region is a space where the temperature is 400 ° C. or higher and a combustible gas is present, and it is preferable that the high-temperature gas blowing region be from the combustion start region to the main combustion region.
  • the sensible heat in the exhaust gas is used effectively. And increase thermal efficiency.
  • the operation method of the waste incinerator of the present invention can be realized by the waste incinerator shown in FIG. 3 described in the first embodiment.
  • the temperature is 200 ° C. or more, and the above equation (2) is satisfied Except for the high-temperature gas being blown into the combustion chamber 1, what has been described in the first embodiment can be applied as it is. -Embodiment 3
  • the temperature of the high-temperature gas blown into the combustion chamber was 200 ° C. or higher. We found that there are conditions that can suppress the generation of CO and dioxin even when the content is less than C.
  • the temperature at which thermal decomposition starts is generally 100 ° C or higher, so even if the temperature is lower than 200 ° C, thermal decomposition occurs and flammable gas is generated. Therefore, if the temperature and oxygen concentration of the hot gas are optimized, the effect of reducing CO and dioxins can be expected. In this case, the effect of reducing NOX is smaller than when the temperature of the high-temperature gas is 200 or more, but NOx can be reduced by installing denitration equipment.
  • Fig. 8 shows the relationship between the temperature and the oxygen concentration of the high-temperature gas.By blowing the high-temperature gas with the oxygen concentration and temperature in the region surrounded by lines A, B, and C into the combustion chamber, If the temperature is less than 200 ° C and the above equation (3) is satisfied, it is possible to promote the thermal decomposition of the waste and to stably stabilize the flame on the waste layer. Obviously. At this time, the mixed combustion of the combustible gas is promoted, so that uniform and stable combustion is performed, and the generation of harmful substances such as CO and dioxin can be reduced.
  • the reason why the oxygen concentration is set to 21 or less is that an oxygen enrichment device is required to make oxygen larger than 21, which is not preferable.
  • Embodiment 2 when the temperature of the high-temperature gas is lower than 200 ° C., as in Embodiment 2, Inclusion of at least one of carbon dioxide and water vapor in the hot gas is effective for suppressing the generation of CO and dioxin.
  • the temperature and oxygen concentration of the hot gas are controlled in the region surrounded by the D, E, and F lines, that is, when the temperature of the hot gas is less than 200, It is necessary to satisfy equation (4).

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Abstract

L'invention concerne un procédé d'exploitation d'un incinérateur de déchets, selon lequel il est prévu d'injecter par soufflage, dans la chambre de combustion d'un incinérateur de déchets ou similaire, un gaz haute température à 200 °C ou davantage, dont la température satisfait à exp(7,78-0,18C) ≤ T ≤ exp(7,45-0,11C). Dans la formule, C représente la concentration en oxygène ( % en volume) du gaz haute température. Ce procédé permet de réduire de manière satisfaisante la quantité de substances toxiques, comme Nox et CO, tout en procédant à une combustion à faible pourcentage d'air dans un incinérateur de déchets.
PCT/JP2003/002623 2002-05-02 2003-03-06 Procede d'exploitation d'un incinerateur de dechets et incinerateur de dechets correspondant WO2003093728A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP03710255A EP1500875A4 (fr) 2002-05-02 2003-03-06 Procede d'exploitation d'un incinerateur de dechets et incinerateur de dechets correspondant
KR1020047017549A KR100660757B1 (ko) 2002-05-02 2003-03-06 폐기물소각로의 조업방법 및 폐기물소각로

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JP2002130526 2002-05-02
JP2002-130526 2002-05-02
JP2002-237024 2002-08-15
JP2002237022A JP3995237B2 (ja) 2002-05-02 2002-08-15 廃棄物焼却炉の操業方法
JP2002-237023 2002-08-15
JP2002237023A JP3989333B2 (ja) 2002-08-15 2002-08-15 廃棄物焼却炉の操業方法
JP2002-237022 2002-08-15
JP2002237024A JP2004077014A (ja) 2002-08-15 2002-08-15 廃棄物焼却炉の操業方法

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WO2003093728A1 true WO2003093728A1 (fr) 2003-11-13

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KR101175296B1 (ko) * 2010-04-02 2012-08-20 이승우 폐기물 소각장치
KR101436067B1 (ko) * 2014-04-08 2014-09-12 (주)씨엠환경에너지 배출가스를 이용한 연소제어 기술이 내재된 소각로
CN105351944B (zh) * 2015-12-10 2017-12-08 重庆三峰卡万塔环境产业有限公司 一种改进的炉排炉垃圾焚烧装置

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EP0413104A1 (fr) * 1989-06-16 1991-02-20 Ebara Corporation Procédé pour le réglage de la combustion dans un chauffage
JPH04273910A (ja) * 1991-02-28 1992-09-30 Kobe Steel Ltd 流動床式焼却炉における燃焼用空気の供給方法及びその装置
JPH0517311U (ja) * 1991-08-16 1993-03-05 石川島播磨重工業株式会社 デイーゼル機関のＮＯｘ低減装置
JP2001241629A (ja) * 2000-03-01 2001-09-07 Mitsubishi Heavy Ind Ltd 廃棄物低公害燃焼装置
JP2002228130A (ja) * 2001-02-01 2002-08-14 Mitsubishi Heavy Ind Ltd 燃焼炉若しくは焼却炉、及びこれらの炉の排出ガス規制分低減方法

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EP0413104A1 (fr) * 1989-06-16 1991-02-20 Ebara Corporation Procédé pour le réglage de la combustion dans un chauffage
JPH04273910A (ja) * 1991-02-28 1992-09-30 Kobe Steel Ltd 流動床式焼却炉における燃焼用空気の供給方法及びその装置
JPH0517311U (ja) * 1991-08-16 1993-03-05 石川島播磨重工業株式会社 デイーゼル機関のＮＯｘ低減装置
JP2001241629A (ja) * 2000-03-01 2001-09-07 Mitsubishi Heavy Ind Ltd 廃棄物低公害燃焼装置
JP2002228130A (ja) * 2001-02-01 2002-08-14 Mitsubishi Heavy Ind Ltd 燃焼炉若しくは焼却炉、及びこれらの炉の排出ガス規制分低減方法

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See also references of EP1500875A4 *

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EP1500875A4 (fr) 2007-07-11
KR20040102200A (ko) 2004-12-03
KR100660757B1 (ko) 2006-12-26
EP1500875A1 (fr) 2005-01-26

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