CN114046505A - Device and method for directly burning high-water-content coal gasification ash - Google Patents
Device and method for directly burning high-water-content coal gasification ash Download PDFInfo
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- CN114046505A CN114046505A CN202111496300.XA CN202111496300A CN114046505A CN 114046505 A CN114046505 A CN 114046505A CN 202111496300 A CN202111496300 A CN 202111496300A CN 114046505 A CN114046505 A CN 114046505A
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- 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
- F23G5/006—General arrangement of incineration plant, e.g. flow sheets
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- 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
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
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- 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
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/04—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment drying
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- 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
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- 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
- F23G5/46—Recuperation of heat
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
- F23L15/04—Arrangements of recuperators
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/30—Solid combustion residues, e.g. bottom or flyash
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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Abstract
The invention belongs to the technical field of coal gasification ash combustion, and particularly relates to a device and a method for directly combusting high-water-content coal gasification ash, wherein the device comprises a dehydration device, an incinerator, an air preheating device, a heat recovery device and the like; the air preheating device provided by the invention can flexibly adjust the temperature of air entering the incinerator; the gasification ash is converted into usable steam by the incinerator, so that the carbon residue in the ash is effectively utilized, and certain economic benefit is brought; meanwhile, a landfill slag yard and supporting facilities thereof which are required by environmental protection standards are not required to be arranged, so that land resources are saved, the investment cost of landfill is saved, and the environment is protected.
Description
Technical Field
The invention belongs to the technical field of coal gasification ash combustion, and particularly relates to a device and a method for directly combusting high-water-content coal gasification ash.
Background
Coal gasification plays an important role in coal chemical industry, and is an important way and means for clean utilization of coal resources. In a coal gasification technical system, coal and oxygen are subjected to partial oxidation reaction in a gasification furnace to generate high-pressure crude synthesis gas and gasification ash, the gasification ash is divided into gasification crude slag and gasification fine slag (or slag slurry), the gasification crude slag is discharged through a lock hopper system of a gasification device, the carbon content is generally 5-20% (weight ratio, dry basis), the water content is 40-60% (weight ratio), and the particle size of the whole particle is larger; the gasified fine slag (or slag slurry) is discharged through a black water flash evaporation settling system, the carbon content is 15-40% (weight ratio, dry basis) generally, the water content is 80-95% (weight ratio), and the particle size of the whole particles is smaller. The gasified ash leaves the production device and is generally subjected to landfill treatment, the ash landfill also needs to be matched with a landfill slag yard according to environmental protection standards and requirements, the slag yard is complex in design, large in occupied area and high in investment, and because the gasified ash contains a large amount of water (generally 31-55% by weight), and a small amount of pollutants including ammonia nitrogen, COD and the like inevitably exist in the water, the problem of reprocessing of the leachate in the slag yard also needs to be considered, and secondary pollution is easily caused by the landfill treatment; the gasified ash contains a certain amount of carbon residue, and the carbon resource is wasted due to the landfill treatment. Because the gasified ash contains a large amount of water (generally 31-55 wt%), the gasified ash cannot be directly combusted, in the prior art, in order to fully utilize carbon resources through combustion, the gasified ash is subjected to filter pressing and dehydration, and then is dried and dehydrated to be below 30% through hot air, but the hot air drying and dehydration needs to consume a large amount of heat, so that the production cost is high.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a device and a method for directly burning high-water-content coal gasification ash, and the method has the characteristics of high water content of the burning gasification ash, low heat consumption, low production cost, environmental friendliness and the like.
In order to achieve the purpose, the technical scheme of the invention is as follows:
the utility model provides a device of high moisture coal gasification lime-ash direct combustion, includes dewatering device, burns burning furnace, air preheater, dewatering device includes fine sediment dewatering device and coarse sediment dewatering device, and coarse sediment dewatering device's import is passed through the dragveyer and is connected with the coarse sediment pond, and fine sediment dewatering device import is connected with the black water buffer tank through the fine sediment delivery pump, coarse sediment dewatering device export and fine sediment dewatering device export all are connected to the inlet of premixing storehouse through lime-ash delivery device, and the outlet of premixing storehouse communicates with the inlet of feeding storehouse, and the outlet of feeding storehouse passes through batcher and burns burning furnace intercommunication, burns burning furnace hot exhanst gas outlet and chimney intercommunication, sets up air preheater on the passageway that burns burning furnace hot exhanst gas outlet and chimney and be connected, said air preheater with burn inside intercommunication of burning furnace.
Further, the coarse slag dehydration device adopts a vibration screen to filter and dehydrate or adopts a rotary drying kiln to dehydrate; the fine slag dewatering device is any one of a plate-and-frame filter press, a centrifugal dehydrator and a vacuum bag filter.
Furthermore, a plurality of heated panels are arranged in the hearth of the incinerator and used for storing or releasing heat; the heated panel is vertical to the inner wall of the incinerator and is parallel to the flowing direction of the flue gas.
Furthermore, the air preheating device comprises an air preheating device a, an air preheating device b and an induced draft fan, an air inlet of the air preheater a is communicated with an outlet of the induced draft fan, an outlet of the air preheater a is communicated with an air inlet of the air preheater b, and an air outlet of the air preheater b is communicated with an air inlet of the incinerator; and a cut-off valve a is arranged on a channel connected with an air inlet of the air preheating device b, the air preheating device b is provided with a bypass pipeline, and the cut-off valve b is arranged on the bypass pipeline.
Furthermore, a cyclone separation device, a heat recovery device, a denitration device, a dust removal device and a desulfurization device are further arranged on a channel connecting the hot flue gas outlet of the incinerator and the chimney, the inlet of the cyclone separation device is communicated with the hot flue gas outlet of the incinerator, and the bottom of the cyclone separator is communicated with the inside of the incinerator through a material returning device and a material returning fan.
Further, the denitration device comprises a selective non-catalytic reduction denitration device and a selective catalytic reduction denitration device, and an inlet of the selective non-catalytic reduction denitration device is communicated with an outlet of the cyclone separation device.
Further, the heat recovery device comprises a high-temperature heat recovery device and a low-temperature heat recovery device, the inlet of the high-temperature heat recovery device is communicated with the outlet of the selective non-catalytic reduction denitration device, the outlet of the high-temperature heat recovery device is communicated with the inlet of the air preheater b, the outlet of the air preheater b is communicated with the inlet of the low-temperature heat recovery device, the outlet of the low-temperature heat recovery device is communicated with the inlet of the selective catalytic reduction denitration device, the outlet of the selective catalytic reduction denitration device is communicated with the inlet of the air preheater a, and the outlet of the air preheater a is communicated with the chimney through a dust removal device and a desulfurization device.
A method for directly burning coal gasification ash slag with high water content is characterized in that: the method comprises the following steps:
(1) the method comprises the following steps of (1) dehydrating gasified coarse slag and gasified fine slag respectively through a coarse slag dehydration device and a fine slag dehydration device, mixing the dehydrated gasified coarse slag and the dehydrated fine slag to obtain mixed ash slag, wherein the mixed ash slag contains 31-55% of water by weight and has a heat value of 700-2500 kcal/kg;
(2) feeding the mixed ash into an incinerator through a feeder to be combusted with hot air, obtaining high-temperature flue gas and slag after the mixed ash is combusted, discharging the slag from the bottom of the incinerator, enabling part of incompletely combusted ash carried in the high-temperature flue gas to flow out of the top of the incinerator, and enabling the temperature of the hot air to be 300-500 ℃;
(3) the ash and slag which are not fully combusted in the high-temperature flue gas are separated out and then returned to the incinerator for full combustion, and the high-temperature flue gas from which the ash and slag which are not fully combusted are removed is discharged from a chimney after denitration, heat recovery, heat exchange with air, dust removal and desulfurization.
Further, the temperature of the bottom of the incinerator is 800-950 ℃, and the temperature of the top of the incinerator is 750-900 ℃.
Furthermore, the temperature of the steam produced by heat recovery is 220-560 ℃, and the pressure is 2.0-9.8 MPa.
Has the advantages that:
1. according to the invention, the air preheating device is arranged, the heating panels with the heat storage or release functions are arranged in the hearth of the incinerator, and air is preheated and then sent into the incinerator, so that 31-55 wt% of high-water-content gasified ash can be directly combusted, the problem that the high-water-content gasified ash is difficult to directly combust is solved, hot air drying dehydration is avoided, the heat consumption is reduced, and the production cost is reduced.
2. The air preheating device comprises an air preheating device a and an air preheating device b, the air preheating device a and the air preheating device b are connected in series to operate, the temperature of air entering the incinerator can be effectively guaranteed, the temperature of the air entering the incinerator can be flexibly adjusted by arranging a bypass in the air preheating device b, the arranged air preheating device b can fully recover heat in low-temperature flue gas, and the heat generated by burning coal gasification ash can be fully recovered.
3. The invention directly burns the gasified ash slag through the incinerator to produce steam with the temperature of 220-560 ℃ and the pressure of 2.0-9.8 MPa for the use in the factory, converts the gasified ash slag into usable steam, effectively utilizes the carbon residue in the ash slag and brings certain economic benefit.
4. The gasification ash is directly combusted by the incinerator to produce steam, a landfill slag field and supporting facilities thereof which are in environmental protection standards and requirements are not required to be arranged, land resources are saved, and the investment cost of landfill gasification ash is saved; meanwhile, the gasified ash slag is prevented from being splashed on the road surface in the process of automobile hauling, and the environmental pollution is avoided.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 1-fine slag dewatering device; 2-a coarse slag dewatering device; 3-a pre-mixing bin; 4-a feeding bin; 5-incinerator; 6-a cyclone separation device; a 7-selective non-catalytic reduction denitration device; 8-a high temperature heat recovery unit; 9-air preheating device b; 10-a low temperature heat recovery unit; 11-a selective catalytic reduction denitration device; 12-air preheating device a; 13-a dust removal device; 14-a desulfurization unit; 15-a chimney; 16-a draught fan; 17-a shut-off valve a; 18-shut off valve b.
Detailed Description
According to the technical scheme, when the vehicle is started, fuels such as natural gas, fuel oil and coal are used as ignition materials, and 31-55 wt% of high-water-content gasification ash residues are ignited in the incinerator 5 and then withdrawn.
Example 1
Referring to fig. 1, in order to enable 31% water-containing gasified ash to be directly combusted, avoid the gasified ash from being dehydrated to below 30% and consume a large amount of heat, simultaneously reduce the production cost of enterprises, improve the utilization rate of the gasified ash and avoid environmental pollution, the device for directly combusting high water-containing gasified ash comprises a dehydration device, an incinerator 5 and an air preheating device, wherein the dehydration device comprises a fine slag dehydration device 1 and a coarse slag dehydration device 2, the inlet of the coarse slag dehydration device 2 is connected with a coarse slag pool through a slag dragging machine, the inlet of the fine slag dehydration device 1 is connected with a black water buffer tank through a fine slag conveying pump, the outlet of the coarse slag dehydration device 2 and the outlet of the fine slag dehydration device 1 are both connected to the inlet of a premixing bin 3 through an ash conveying device, the outlet of the premixing bin 3 is communicated with the inlet of a feeding bin 4, and the outlet of the feeding bin 4 is communicated with the incinerator 5 through a feeder, the ash conveying device is a tubular belt or a horizontal belt, the premixing bin 3 and the feeding bin 4 are both provided with a blockage removing machine, a hot flue gas outlet of the incinerator 5 is communicated with a chimney 15, and an air preheating device is arranged on a channel connecting the hot flue gas outlet of the incinerator 5 with the chimney 15 and is communicated with the inside of the incinerator 5; and a slag cooler and a belt slag extractor are arranged at the bottom of the incinerator 5.
The coarse slag dewatering device 2 adopts a vibrating screen to filter and dewater, and the fine slag dewatering device 1 is a plate-and-frame filter press.
The incinerator 5 is characterized in that a plurality of heated panels are arranged in a hearth and used for storing or releasing heat, the heated panels are perpendicular to the inner wall of the incinerator and parallel to the flowing direction of flue gas, and the heated panels provide part of heat sources for direct combustion of water-containing gasification ash slag with the weight ratio of 31%, so that the gasification ash slag can be stably combusted in the hearth.
The air preheating device comprises an air preheating device a12, an air preheating device b9 and an induced draft fan 16, wherein an air inlet of the air preheater a is communicated with an outlet of the induced draft fan 16, an outlet of the air preheater a is communicated with an air inlet of the air preheater b, and an air outlet of the air preheater b is communicated with an air inlet of the incinerator 5; and a channel connected with an air inlet of the air preheating device b9 is provided with a stop valve a17, the air preheating device b9 is provided with a bypass pipeline, and the bypass pipeline is provided with a stop valve b 18.
A channel for connecting a hot flue gas outlet of the incinerator 5 with a chimney 15 is also provided with a cyclone separation device 6, a heat recovery device, a denitration device, a dust removal device 13 and a desulfurization device 14, an inlet of the cyclone separation device 6 is communicated with the hot flue gas outlet of the incinerator 5, and the bottom of the cyclone separation device is communicated with the inside of the incinerator 5 through a material returning device and a material returning fan.
The denitration device comprises a selective non-catalytic reduction denitration device 7 and a selective catalytic reduction denitration device 11, wherein an inlet of the selective non-catalytic reduction denitration device 7 is communicated with an outlet of the cyclone separation device 6.
The heat recovery device comprises a high-temperature heat recovery device 8 and a low-temperature heat recovery device 10, the inlet of the high-temperature heat recovery device 8 is communicated with the outlet of the selective non-catalytic reduction denitration device 7, the outlet of the high-temperature heat recovery device 8 is communicated with the inlet of the air preheater b, the outlet of the air preheater b is communicated with the inlet of the low-temperature heat recovery device 10, the outlet of the low-temperature heat recovery device 10 is communicated with the inlet of the selective catalytic reduction denitration device 11, the outlet of the selective catalytic reduction denitration device 11 is communicated with the inlet of the air preheater a, and the outlet of the air preheater a is communicated with the chimney 15 through a dust removal device 13 and a desulfurization device 14.
A method for directly burning high-water-content coal gasification ash comprises the following steps:
(1) the method comprises the following steps of (1) dehydrating gasified coarse slag and gasified fine slag respectively through a coarse slag dehydration device 2 and a fine slag dehydration device 1, conveying the dehydrated gasified coarse slag and the dehydrated fine slag into a premixing bin 3 by an ash conveying device, and mixing to obtain mixed ash, wherein the mixed ash contains 31% of water by weight and has a heat value of 700 kcal/kg; the mixed ash and slag in the premixing bin are conveyed into the feeding bin 4, and the mixed ash and slag are buffered in the feeding bin 4 so as to be continuously conveyed into the incinerator 5 for combustion;
(2) the mixed ash in the feeding bin 4 is fed into the incinerator 5 through a feeder to be combusted with hot air, high-temperature flue gas and slag are obtained after the mixed ash is combusted, the slag is discharged from the bottom of the incinerator 5 and is conveyed to a slag loading system through a belt slag cooler after being cooled, part of the insufficiently combusted ash carried in the high-temperature flue gas flows out of the top of the incinerator 5, the temperature of the hot air entering the incinerator 5 is controlled to be 300 ℃, the temperature of the bottom of the incinerator 5 is controlled to be 800 ℃, and the temperature of the top of the incinerator 5 is controlled to be 750 ℃;
(3) the ash residue which is not fully combusted in the high-temperature flue gas is separated out in the cyclone separation device 6 and then returns to the incinerator 5 for full combustion through a material returning device and a material returning fan from the bottom of the cyclone separation device 6, the high-temperature flue gas without the fully combusted ash residue enters the high-temperature heat recovery device 8 after being subjected to first denitration through the selective non-catalytic reduction denitration device 7, steam with the pressure of 2.0MPa and the temperature of 220 ℃ is generated in the high-temperature heat recovery device 8 and is sent to a steam pipe network system, the high-temperature flue gas enters the air preheater b after being cooled in the high-temperature heat recovery device 8, air is preheated to 300 ℃ and then is sent to the incinerator 5 through controlling the regulating valve a and the regulating valve b, the high-temperature flue gas flows out of the air preheater b after being cooled in the air preheater b, at the moment, the high-temperature flue gas is changed into medium-temperature flue gas, the medium-temperature flue gas enters the low-temperature heat recovery device 10 to be further cooled and recover heat to produce hot water, the hot water is used for water supplement of the high-temperature heat recovery device 8 or water supply of a heat exchanger device in a plant, medium-temperature flue gas flows out of the low-temperature heat recovery device 10 and then is changed into low-temperature flue gas, the low-temperature flue gas enters the selective catalytic reduction denitration device for secondary denitration, the low-temperature flue gas after secondary denitration enters the air preheating device a12 for heat exchange with air, and the air enters the air preheating device b9 for secondary heating after primary heat exchange; the low-temperature flue gas enters the dust removal device 13 and the desulfurization device 14 after being cooled by the air preheating device a12, and is discharged from the chimney 15 after dust removal and sulfur removal.
Example 2
Referring to fig. 1, in order to enable water-containing gasified ash with a weight ratio of 40% to be directly combusted, avoid the gasified ash from being dehydrated to below 30% and consume a large amount of heat, simultaneously reduce the production cost of enterprises, improve the utilization rate of the gasified ash and avoid environmental pollution, the device for directly combusting high water-containing gasified ash comprises a dehydration device, an incinerator 5 and an air preheating device, wherein the dehydration device comprises a fine slag dehydration device 1 and a coarse slag dehydration device 2, the inlet of the coarse slag dehydration device 2 is connected with a coarse slag pool through a slag dragging machine, the inlet of the fine slag dehydration device 1 is connected with a black water buffer tank through a fine slag conveying pump, the outlet of the coarse slag dehydration device 2 and the outlet of the fine slag dehydration device 1 are both connected to the inlet of a premixing bin 3 through an ash conveying device, the outlet of the premixing bin 3 is communicated with the inlet of a feeding bin 4, and the outlet of the feeding bin 4 is communicated with the incinerator 5 through a feeding machine, the ash conveying device is a tubular belt or a horizontal belt, the premixing bin 3 and the feeding bin 4 are both provided with a blockage removing machine, a hot flue gas outlet of the incinerator 5 is communicated with a chimney 15, and an air preheating device is arranged on a channel connecting the hot flue gas outlet of the incinerator 5 with the chimney 15 and is communicated with the inside of the incinerator 5; and a slag cooler and a belt slag extractor are arranged at the bottom of the incinerator 5.
The coarse slag dewatering device 2 adopts a vibration screen to filter and dewater, and the fine slag dewatering device 1 is a centrifugal dehydrator.
The incinerator 5 is characterized in that a plurality of heated panels are arranged in a hearth and used for storing or releasing heat, the heated panels are perpendicular to the inner wall of the incinerator and parallel to the flowing direction of flue gas, and the heated panels provide partial heat sources for direct combustion of water-containing gasification ash slag with the weight ratio of 40%, so that the gasification ash slag can be stably combusted in the hearth.
The air preheating device comprises an air preheating device a12, an air preheating device b9 and an induced draft fan 16, wherein an air inlet of the air preheater a is communicated with an outlet of the induced draft fan 16, an outlet of the air preheater a is communicated with an air inlet of the air preheater b, and an air outlet of the air preheater b is communicated with an air inlet of the incinerator 5; and a channel connected with an air inlet of the air preheating device b9 is provided with a stop valve a17, the air preheating device b9 is provided with a bypass pipeline, and the bypass pipeline is provided with a stop valve b 18.
A channel for connecting a hot flue gas outlet of the incinerator 5 with a chimney 15 is also provided with a cyclone separation device 6, a heat recovery device, a denitration device, a dust removal device 13 and a desulfurization device 14, an inlet of the cyclone separation device 6 is communicated with the hot flue gas outlet of the incinerator 5, and the bottom of the cyclone separation device is communicated with the inside of the incinerator 5 through a material returning device and a material returning fan.
The denitration device comprises a selective non-catalytic reduction denitration device 7 and a selective catalytic reduction denitration device 11, wherein an inlet of the selective non-catalytic reduction denitration device 7 is communicated with an outlet of the cyclone separation device 6.
The heat recovery device comprises a high-temperature heat recovery device 8 and a low-temperature heat recovery device 10, the inlet of the high-temperature heat recovery device 8 is communicated with the outlet of the selective non-catalytic reduction denitration device 7, the outlet of the high-temperature heat recovery device 8 is communicated with the inlet of the air preheater b, the outlet of the air preheater b is communicated with the inlet of the low-temperature heat recovery device 10, the outlet of the low-temperature heat recovery device 10 is communicated with the inlet of the selective catalytic reduction denitration device 11, the outlet of the selective catalytic reduction denitration device 11 is communicated with the inlet of the air preheater a, and the outlet of the air preheater a is communicated with the chimney 15 through a dust removal device 13 and a desulfurization device 14.
A method for directly burning high-water-content coal gasification ash comprises the following steps:
(1) the method comprises the following steps of (1) dehydrating gasified coarse slag and gasified fine slag respectively through a coarse slag dehydration device 2 and a fine slag dehydration device 1, conveying the dehydrated gasified coarse slag and the dehydrated fine slag into a premixing bin 3 by an ash conveying device, and mixing to obtain mixed ash, wherein the mixed ash contains 40% of water by weight and has a heat value of 1500 kcal/kg; the mixed ash and slag in the premixing bin are conveyed into the feeding bin 4, and the mixed ash and slag are buffered in the feeding bin 4 so as to be continuously conveyed into the incinerator 5 for combustion;
(2) the mixed ash in the feeding bin 4 is fed into the incinerator 5 through a feeder to be combusted with hot air, high-temperature flue gas and slag are obtained after the mixed ash is combusted, the slag is discharged from the bottom of the incinerator 5 and is conveyed to a slag loading system through a belt slag cooler after being cooled, part of the insufficiently combusted ash carried in the high-temperature flue gas flows out of the top of the incinerator 5, the temperature of the hot air entering the incinerator 5 is controlled to be 350 ℃, the temperature of the bottom of the incinerator 5 is controlled to be 850 ℃, and the temperature of the top of the incinerator 5 is controlled to be 800 ℃;
(3) the ash residue which is not fully combusted in the high-temperature flue gas is separated out in the cyclone separation device 6 and then returns to the incinerator 5 for full combustion through a material returning device and a material returning fan from the bottom of the cyclone separation device 6, the high-temperature flue gas without the fully combusted ash residue enters the high-temperature heat recovery device 8 after being subjected to first denitration through the selective non-catalytic reduction denitration device 7, steam with the pressure of 4.5MPa and the temperature of 350 ℃ is generated in the high-temperature heat recovery device 8 and is sent to a steam pipe network system, the high-temperature flue gas enters the air preheater b after being cooled in the high-temperature heat recovery device 8, air is preheated to 350 ℃ and then is sent to the incinerator 5 through controlling the regulating valve a and the regulating valve b, the high-temperature flue gas flows out of the air preheater b after being cooled in the air preheater b, at the moment, the high-temperature flue gas is changed into medium-temperature flue gas, the medium-temperature flue gas enters the low-temperature heat recovery device 10 to be further cooled and recover heat to produce hot water, the hot water is used for water supplement of the high-temperature heat recovery device 8 or water supply of a heat exchanger device in a plant, medium-temperature flue gas flows out of the low-temperature heat recovery device 10 and then is changed into low-temperature flue gas, the low-temperature flue gas enters the selective catalytic reduction denitration device for secondary denitration, the low-temperature flue gas after secondary denitration enters the air preheating device a12 for heat exchange with air, and the air enters the air preheating device b9 for reheating after primary heat exchange; the low-temperature flue gas enters the dust removal device 13 and the desulfurization device 14 after being cooled by the air preheating device a12, and is discharged from the chimney 15 after dust removal and sulfur removal.
Example 3
Referring to fig. 1, in order to enable 50% water-containing gasified ash to be directly combusted, avoid the gasified ash from being dehydrated to below 30% and consume a large amount of heat, simultaneously reduce the production cost of enterprises, improve the utilization rate of the gasified ash and avoid environmental pollution, the device for directly combusting high water-containing gasified ash comprises a dehydration device, an incinerator 5 and an air preheating device, wherein the dehydration device comprises a fine slag dehydration device 1 and a coarse slag dehydration device 2, the inlet of the coarse slag dehydration device 2 is connected with a coarse slag pool through a slag dragging machine, the inlet of the fine slag dehydration device 1 is connected with a black water buffer tank through a fine slag conveying pump, the outlet of the coarse slag dehydration device 2 and the outlet of the fine slag dehydration device 1 are both connected to the inlet of a premixing bin 3 through an ash conveying device, the outlet of the premixing bin 3 is communicated with the inlet of a feeding bin 4, and the outlet of the feeding bin 4 is communicated with the incinerator 5 through a feeder, the ash conveying device is a tubular belt or a horizontal belt, the premixing bin 3 and the feeding bin 4 are both provided with a blockage removing machine, a hot flue gas outlet of the incinerator 5 is communicated with a chimney 15, and an air preheating device is arranged on a channel connecting the hot flue gas outlet of the incinerator 5 with the chimney 15 and is communicated with the inside of the incinerator 5; and a slag cooler and a belt slag extractor are arranged at the bottom of the incinerator 5.
The coarse slag dewatering device 2 adopts a rotary drying kiln to dewater, and the fine slag dewatering device 1 is a vacuum bag type filter.
The incinerator 5 is characterized in that a plurality of heated panels are arranged in a hearth and used for storing or releasing heat, the heated panels are perpendicular to the inner wall of the incinerator and parallel to the flowing direction of flue gas, and the heated panels provide partial heat sources for direct combustion of water-containing gasified ash residues with the weight ratio of 50%, so that the gasified ash residues can be stably combusted in the hearth.
The air preheating device comprises an air preheating device a12, an air preheating device b9 and an induced draft fan 16, wherein an air inlet of the air preheater a is communicated with an outlet of the induced draft fan 16, an outlet of the air preheater a is communicated with an air inlet of the air preheater b, and an air outlet of the air preheater b is communicated with an air inlet of the incinerator 5; and a channel connected with an air inlet of the air preheating device b9 is provided with a stop valve a17, the air preheating device b9 is provided with a bypass pipeline, and the bypass pipeline is provided with a stop valve b 18.
A channel for connecting a hot flue gas outlet of the incinerator 5 with a chimney 15 is also provided with a cyclone separation device 6, a heat recovery device, a denitration device, a desulfurization device 14 and a dust removal device 13, an inlet of the cyclone separation device 6 is communicated with the hot flue gas outlet of the incinerator 5, and the bottom of the cyclone separation device is communicated with the inside of the incinerator 5 through a material returning device and a material returning fan.
The denitration device comprises a selective non-catalytic reduction denitration device 7 and a selective catalytic reduction denitration device 11, wherein an inlet of the selective non-catalytic reduction denitration device 7 is communicated with an outlet of the cyclone separation device 6.
The heat recovery device comprises a high-temperature heat recovery device 8 and a low-temperature heat recovery device 10, the inlet of the high-temperature heat recovery device 8 is communicated with the outlet of the selective non-catalytic reduction denitration device 7, the outlet of the high-temperature heat recovery device 8 is communicated with the inlet of the air preheater b, the outlet of the air preheater b is communicated with the inlet of the low-temperature heat recovery device 10, the outlet of the low-temperature heat recovery device 10 is communicated with the inlet of the selective catalytic reduction denitration device 11, the outlet of the selective catalytic reduction denitration device 11 is communicated with the inlet of the air preheater a, and the outlet of the air preheater a is communicated with the chimney 15 through a dust removal device 13 and a desulfurization device 14.
A method for directly burning high-water-content coal gasification ash comprises the following steps:
(1) the method comprises the following steps of (1) dehydrating gasified coarse slag and gasified fine slag respectively through a coarse slag dehydration device 2 and a fine slag dehydration device 1, conveying the dehydrated gasified coarse slag and the dehydrated fine slag into a premixing bin 3 by an ash conveying device, and mixing to obtain mixed ash, wherein the mixed ash contains 50% of water by weight and has a heat value of 2000 kcal/kg; the mixed ash and slag in the premixing bin are conveyed into the feeding bin 4, and the mixed ash and slag are buffered in the feeding bin 4 so as to be continuously conveyed into the incinerator 5 for combustion;
(2) the mixed ash in the feeding bin 4 is fed into the incinerator 5 through a feeder to be combusted with hot air, high-temperature flue gas and slag are obtained after the mixed ash is combusted, the slag is discharged from the bottom of the incinerator 5 and is conveyed to a slag loading system through a belt slag cooler after being cooled, part of the insufficiently combusted ash carried in the high-temperature flue gas flows out of the top of the incinerator 5, the temperature of the hot air entering the incinerator 5 is controlled to be 450 ℃, the temperature of the bottom of the incinerator 5 is controlled to be 900 ℃, and the temperature of the top of the incinerator 5 is controlled to be 850 ℃;
(3) the ash residue which is not fully combusted in the high-temperature flue gas is separated out in the cyclone separation device 6 and then returns to the incinerator 5 for full combustion through a material returning device and a material returning fan from the bottom of the cyclone separation device 6, the high-temperature flue gas without the fully combusted ash residue enters the high-temperature heat recovery device 8 after being subjected to first denitration through the selective non-catalytic reduction denitration device 7, steam with the pressure of 7.5MPa and the temperature of 450 ℃ is generated in the high-temperature heat recovery device 8 and is sent to a steam pipe network system, the high-temperature flue gas enters the air preheater b after being cooled in the high-temperature heat recovery device 8, air is preheated to 450 ℃ and then is sent to the incinerator 5 through controlling the regulating valve a and the regulating valve b, the high-temperature flue gas flows out of the air preheater b after being cooled in the air preheater b, at the moment, the high-temperature flue gas is changed into medium-temperature flue gas, the medium-temperature flue gas enters the low-temperature heat recovery device 10 to be further cooled and recover heat to produce hot water, the hot water is used for water supplement of the high-temperature heat recovery device 8 or water supply of a heat exchanger device in a plant, medium-temperature flue gas flows out of the low-temperature heat recovery device 10 and then is changed into low-temperature flue gas, the low-temperature flue gas enters the selective catalytic reduction denitration device for secondary denitration, the low-temperature flue gas after secondary denitration enters the air preheating device a12 for heat exchange with air, and the air enters the air preheating device b9 for secondary heating after primary heat exchange; the low-temperature flue gas enters the dust removal device 13 and the desulfurization device 14 after being cooled by the air preheating device a12, and is discharged from the chimney 15 after dust removal and sulfur removal.
Example 4
Referring to fig. 1, in order to enable 55% by weight of hydrous gasified ash to be directly combusted, avoid the gasified ash from being dehydrated to below 30% and consume a large amount of heat, simultaneously reduce the production cost of enterprises, improve the utilization rate of the gasified ash and avoid environmental pollution, the device for directly combusting the hydrous gasified ash comprises a dehydration device, an incinerator 5 and an air preheating device, wherein the dehydration device comprises a fine slag dehydration device 1 and a coarse slag dehydration device 2, the inlet of the coarse slag dehydration device 2 is connected with a coarse slag pool through a slag dragging machine, the inlet of the fine slag dehydration device 1 is connected with a black water buffer tank through a fine slag conveying pump, the outlet of the coarse slag dehydration device 2 and the outlet of the fine slag dehydration device 1 are both connected to the inlet of a premixing bin 3 through an ash conveying device, the outlet of the premixing bin 3 is communicated with the inlet of a feeding bin 4, and the outlet of the feeding bin 4 is communicated with the incinerator 5 through a feeder, the ash conveying device is a tubular belt or a horizontal belt, the premixing bin 3 and the feeding bin 4 are both provided with a blockage removing machine, a hot flue gas outlet of the incinerator 5 is communicated with a chimney 15, and an air preheating device is arranged on a channel connecting the hot flue gas outlet of the incinerator 5 with the chimney 15 and is communicated with the inside of the incinerator 5; and a slag cooler and a belt slag extractor are arranged at the bottom of the incinerator 5.
The coarse slag dewatering device 2 adopts a rotary drying kiln for dewatering, and the fine slag dewatering device 1 is a diaphragm presser.
The incinerator 5 is characterized in that a plurality of heated panels are arranged in a hearth and used for storing or releasing heat, the heated panels are perpendicular to the inner wall of the incinerator and parallel to the flowing direction of flue gas, and the heated panels provide partial heat sources for direct combustion of 55 wt% of water-containing gasified ash, so that the gasified ash can be stably combusted in the hearth.
The air preheating device comprises an air preheating device a12, an air preheating device b9 and an induced draft fan 16, wherein an air inlet of the air preheater a is communicated with an outlet of the induced draft fan 16, an outlet of the air preheater a is communicated with an air inlet of the air preheater b, and an air outlet of the air preheater b is communicated with an air inlet of the incinerator 5; and a channel connected with an air inlet of the air preheating device b9 is provided with a stop valve a17, the air preheating device b9 is provided with a bypass pipeline, and the bypass pipeline is provided with a stop valve b 18.
A channel for connecting a hot flue gas outlet of the incinerator 5 with a chimney 15 is also provided with a cyclone separation device 6, a heat recovery device, a denitration device, a dust removal device 13 and a desulfurization device 14, an inlet of the cyclone separation device 6 is communicated with the hot flue gas outlet of the incinerator 5, and the bottom of the cyclone separation device is communicated with the inside of the incinerator 5 through a material returning device and a material returning fan.
The denitration device comprises a selective non-catalytic reduction denitration device 7 and a selective catalytic reduction denitration device 11, wherein an inlet of the selective non-catalytic reduction denitration device 7 is communicated with an outlet of the cyclone separation device 6.
The heat recovery device comprises a high-temperature heat recovery device 8 and a low-temperature heat recovery device 10, the inlet of the high-temperature heat recovery device 8 is communicated with the outlet of the selective non-catalytic reduction denitration device 7, the outlet of the high-temperature heat recovery device 8 is communicated with the inlet of the air preheater b, the outlet of the air preheater b is communicated with the inlet of the low-temperature heat recovery device 10, the outlet of the low-temperature heat recovery device 10 is communicated with the inlet of the selective catalytic reduction denitration device 11, the outlet of the selective catalytic reduction denitration device 11 is communicated with the inlet of the air preheater a, and the outlet of the air preheater a is communicated with the chimney 15 through a dust removal device 13 and a desulfurization device 14.
A method for directly burning high-water-content coal gasification ash comprises the following steps:
(1) the method comprises the following steps of (1) dehydrating gasified coarse slag and gasified fine slag respectively through a coarse slag dehydration device 2 and a fine slag dehydration device 1, conveying the dehydrated gasified coarse slag and the dehydrated fine slag into a premixing bin 3 by a slag conveying device, and mixing to obtain mixed slag, wherein the mixed slag contains 55% of water by weight and has a heat value of 2500 kcal/kg; the mixed ash and slag in the premixing bin are conveyed into the feeding bin 4, and the mixed ash and slag are buffered in the feeding bin 4 so as to be continuously conveyed into the incinerator 5 for combustion;
(2) the mixed ash in the feeding bin 4 is fed into the incinerator 5 through a feeder to be combusted with hot air, high-temperature flue gas and slag are obtained after the mixed ash is combusted, the slag is discharged from the bottom of the incinerator 5 and is conveyed to a slag loading system through a belt slag cooler after being cooled, part of the insufficiently combusted ash carried in the high-temperature flue gas flows out of the top of the incinerator 5, the temperature of the hot air entering the incinerator 5 is controlled to be 500 ℃, the temperature of the bottom of the incinerator 5 is controlled to be 950 ℃, and the temperature of the top of the incinerator 5 is controlled to be 900 ℃;
(3) the ash residue which is not fully combusted in the high-temperature flue gas is separated out in the cyclone separation device 6 and then returns to the incinerator 5 for full combustion through a material returning device and a material returning fan from the bottom of the cyclone separation device 6, the high-temperature flue gas without the fully combusted ash residue enters the high-temperature heat recovery device 8 after being subjected to first denitration through the selective non-catalytic reduction denitration device 7, steam with the pressure of 9.8MPa and the temperature of 560 ℃ is generated in the high-temperature heat recovery device 8 and is sent to a steam pipe network system, the high-temperature flue gas is cooled in the high-temperature heat recovery device 8 and then enters the air preheater b, the air is preheated to 500 ℃ and then is sent to the incinerator 5 through controlling the regulating valve a and the regulating valve b, the high-temperature flue gas is cooled in the air preheater b and then flows out of the air preheater b, at the moment, the high-temperature flue gas is changed into medium-temperature flue gas, the medium-temperature flue gas enters the low-temperature heat recovery device 10 to be further cooled and recover heat to produce hot water, the hot water is used for water supplement of the high-temperature heat recovery device 8 or water supply of a heat exchanger device in a plant, medium-temperature flue gas flows out of the low-temperature heat recovery device 10 and then is changed into low-temperature flue gas, the low-temperature flue gas enters the selective catalytic reduction denitration device for secondary denitration, the low-temperature flue gas after secondary denitration enters the air preheating device a12 for heat exchange with air, and the air enters the air preheating device b9 for secondary heating after primary heat exchange; the low-temperature flue gas enters the dust removal device 13 and the desulfurization device 14 after being cooled by the air preheating device a12, and is discharged from the chimney 15 after dust removal and sulfur removal.
Another embodiment differs from embodiment 1 in that: the weight ratio of water contained in the mixed ash is 55%, the heat value is 700 kcal/kg, and the temperature of hot air entering the incinerator 5 is 300 ℃.
Another embodiment differs from embodiment 1 in that: the weight ratio of water contained in the mixed ash is 55%, the heat value is 700 kcal/kg, and the temperature of hot air entering the incinerator 5 is 500 ℃.
Another embodiment differs from embodiment 4 in that: the mixed ash contains 31 percent of water by weight, has the heat value of 2500kcal/kg, and has the temperature of 300 ℃ when entering the incinerator 5.
The working principle of the invention is as follows: the invention arranges a plurality of heated panels with the function of storing or releasing heat and an air preheating device in a hearth of an incinerator 5, and preheats air to 300-500 ℃; the heat stored by the heated panel, the heat carried by air at 300-500 ℃ and the heat generated by the combustion of 31-55 wt% of the water-containing gasification ash are used as a heat source for the combustion start of 31-55 wt% of the water-containing gasification ash which enters the hearth of the incinerator 5 later, so that the water-containing gasification ash with the weight ratio of 31-55 wt% can be continuously and stably directly combusted in the incinerator 5 and the heat is released, and the released heat is recycled by a heat recovery device to produce steam; and meanwhile, the gasified ash can be treated, so that the pollution of the gasified ash to the environment by the hauling and landfill of an automobile is avoided.
Modifications and variations of the present invention, which are familiar to the inventor, are within the scope of the invention, and are not limited to the embodiments described.
Claims (10)
1. The utility model provides a device of high moisture coal gasification lime-ash direct combustion, includes dewatering device, dewatering device includes thin sediment dewatering device and thick sediment dewatering device, and thick sediment dewatering device's import is passed through the dragveyer and is connected with thick sediment pond, and the import of thin sediment dewatering device is connected its characterized in that through thin sediment delivery pump and black water buffer tank: still including burning furnace, air preheating device, coarse residue dewatering device export and the export of thin sediment dewatering device all are connected to the import of premixing storehouse through lime-ash conveyor, and the export of premixing storehouse communicates with the feed bin import, and the feed bin export is through batcher and burning furnace intercommunication, burns burning furnace hot exhanst gas outlet and chimney intercommunication, sets up air preheating device on the passageway that burns burning furnace hot exhanst gas outlet and chimney connection, said air preheating device with burn inside intercommunication of burning furnace.
2. The apparatus for directly combusting high water content coal gasification ash according to claim 1, wherein: the coarse slag dehydration device adopts a vibration screen to filter and dehydrate or a rotary drying kiln to dehydrate; the fine slag dewatering device is any one of a plate-and-frame filter press, a centrifugal dehydrator, a vacuum bag filter and a diaphragm presser.
3. The apparatus for directly combusting high water content coal gasification ash according to claim 1, wherein: a plurality of heated panels are arranged in a hearth of the incinerator and used for storing or releasing heat; the heated panel is vertical to the inner wall of the incinerator and is parallel to the flowing direction of the flue gas.
4. The apparatus for directly combusting high water content coal gasification ash according to claim 1, wherein: the air preheating device comprises an air preheating device a, an air preheating device b and an induced draft fan, wherein an air inlet of the air preheating device a is communicated with an outlet of the induced draft fan, an outlet of the air preheating device a is communicated with an air inlet of the air preheating device b, and an air outlet of the air preheating device b is communicated with an air inlet of the incinerator; and a cut-off valve a is arranged on a channel connected with an air inlet of the air preheating device b, the air preheating device b is provided with a bypass pipeline, and the cut-off valve b is arranged on the bypass pipeline.
5. The apparatus of claim 1, wherein a cyclone separator, a heat recovery device, a denitration device, a dedusting device and a desulfurization device are further disposed on a channel connecting the hot flue gas outlet of the incinerator and the chimney, the inlet of the cyclone separator is communicated with the hot flue gas outlet of the incinerator, and the bottom of the cyclone separator is communicated with the inside of the incinerator through a material returning device and a material returning fan.
6. The apparatus for directly combusting high water content coal gasification ash according to claim 3, wherein: the denitration device comprises a selective non-catalytic reduction denitration device and a selective catalytic reduction denitration device, and an inlet of the selective non-catalytic reduction denitration device is communicated with an outlet of the cyclone separation device.
7. The apparatus for directly combusting high water content coal gasification ash according to claim 3, wherein: the heat recovery device comprises a high-temperature heat recovery device and a low-temperature heat recovery device, the inlet of the high-temperature heat recovery device is communicated with the outlet of the selective non-catalytic reduction denitration device, the outlet of the high-temperature heat recovery device is communicated with the inlet of the air preheater b, the outlet of the air preheater b is communicated with the inlet of the low-temperature heat recovery device, the outlet of the low-temperature heat recovery device is communicated with the inlet of the selective catalytic reduction denitration device, the outlet of the selective catalytic reduction denitration device is communicated with the inlet of the air preheater a, and the outlet of the air preheater a is communicated with the chimney through a dust removal device and a desulfurization device.
8. A method for directly burning coal gasification ash slag with high water content is characterized in that: the method comprises the following steps:
(1) the method comprises the following steps of (1) dehydrating gasified coarse slag and gasified fine slag respectively through a coarse slag dehydration device and a fine slag dehydration device, mixing the dehydrated gasified coarse slag and the dehydrated fine slag to obtain mixed ash slag, wherein the mixed ash slag contains 31-55% of water by weight and has a heat value of 700-2500 kcal/kg;
(2) feeding the mixed ash into an incinerator through a feeder to be combusted with hot air, obtaining high-temperature flue gas and slag after the mixed ash is combusted, discharging the slag from the bottom of the incinerator, enabling part of incompletely combusted ash carried in the high-temperature flue gas to flow out of the top of the incinerator, and enabling the temperature of the hot air to be 300-500 ℃;
(3) the ash and slag which are not fully combusted in the high-temperature flue gas are separated out and then returned to the incinerator for full combustion, and the high-temperature flue gas from which the ash and slag which are not fully combusted are removed is discharged from a chimney after denitration, heat recovery, heat exchange with air, dust removal and desulfurization.
9. The method for directly combusting high water content coal gasification ash according to claim 8, wherein the method comprises the following steps: the temperature of the bottom of the incinerator is 800-950 ℃, and the temperature of the top of the incinerator is 750-900 ℃.
10. The method for directly combusting high water content coal gasification ash according to claim 8, wherein the method comprises the following steps: the temperature of the steam produced by heat recovery is 220-560 ℃, and the pressure is 2.0-9.8 MPa.
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