CN114719267B - Recycling harmless treatment device and method for extracting tar from low-calorific-value fuel - Google Patents
Recycling harmless treatment device and method for extracting tar from low-calorific-value fuel Download PDFInfo
- Publication number
- CN114719267B CN114719267B CN202210402412.2A CN202210402412A CN114719267B CN 114719267 B CN114719267 B CN 114719267B CN 202210402412 A CN202210402412 A CN 202210402412A CN 114719267 B CN114719267 B CN 114719267B
- Authority
- CN
- China
- Prior art keywords
- inlet
- coal gangue
- outlet
- solid
- coal
- Prior art date
- Legal status (The legal status 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 status listed.)
- Active
Links
Images
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
- 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
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
-
- 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
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention discloses a low-calorific-value fuel tar extraction recycling harmless treatment device and a method, wherein coal gangue is ground into powder, the powder is conveyed into a tubular gas-solid two-phase flow coal gangue powder heater by a fan, coal tar is separated out through high-temperature heating, after gas-solid separation, solid coke enters a fluidized bed heat insulation incinerator for combustion, flue gas enters a cooler for stepwise cooling and recycling the coal tar, the high-temperature flue gas carries out convection heat exchange with the tubular gas-solid two-phase flow coal gangue powder heater and an air preheater, then the flue gas enters a bag-type dust remover, after dust removal, the flue gas is pressurized by a powder conveying fan, then enters a coal gangue grinder for drying and carries coal gangue powder to enter the tubular gas-solid two-phase flow heater, and ash generated after combustion is used for mining area soil improvement and building blending.
Description
Technical Field
The invention belongs to the technical field of low-calorific-value fuel treatment, and particularly relates to a low-calorific-value fuel tar-extraction recycling harmless treatment device and method.
Background
The coal gangue is solid waste discharged in the coal mining process and the coal washing process, and is a black and gray rock which has lower carbon content and is harder than coal and is associated with a coal bed in the coal forming process. Through investigation, in northern Shaanxi, inner Mongolia and Shanxi and other mining areas, the coal gangue with the heat value higher than 1500kcal/kg is basically used for power generation or combined heat and power generation, while the low-heat-value coal gangue with the heat value lower than 1500kcal/kg is mainly treated by means of burying pits and mining area accumulation after open-air mining or is mixed with high-heat-value fuel for power generation, and the amount of the low-heat-value coal gangue is further increased along with the progress of mining and coal washing engineering. By 2019, according to incomplete statistics, the accumulated stacking amount of coal gangue in China exceeds 60 hundred million tons, 1500-1700 coal gangue hills are formed, the occupied area reaches more than 20 ten thousand mu, and the emission amount of about 5 hundred million-8 hundred million tons per year is increased year by year, so that the problems of local atmospheric environmental pollution, soil pollution, land resource occupation, ecological damage and the like are caused.
At present, the comprehensive utilization technology of coal gangue in China comprises coal gangue power generation, paving, building material production, chemical raw material production, agricultural application and the like, good application effects are obtained, but the comprehensive utilization rate of the coal gangue is less than 30%, most of the coal gangue is still disposed in an accumulation mode, and therefore, the large-scale industrial comprehensive treatment technology is still the problem of low-calorific-value coal gangue treatment which needs to be solved urgently.
When coal gangue (coal slime) is used as a boiler fuel for power generation, a circulating fluidized bed boiler is adopted, but low-calorific-value coal gangue and coal slime have low calorific value and high ash content and are difficult to use for power generation, and power generation enterprises face the problem of disposal of slag and coal ash. The existing coal gangue comprehensive treatment technology cannot completely treat coal gangue generated in the development process of the coal industry, open stacking is still the main treatment mode of the coal gangue and coal slime, and from the aspects of double-carbon policy, environment, energy, land resources, waste-free city construction and the like, the industrial industry urgently needs a low-calorific-value solid fuel treatment technology for the coal gangue, the coal slime and the like, which can be produced in a large scale and is recycled and harmless.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a recycling harmless treatment device and method for extracting tar from low-calorific-value fuel, so that the recycling and harmless treatment of the low-calorific-value fuel such as coal gangue, coal slime and the like are realized, the solid waste treatment cost of coal production enterprises is reduced, and the extra income of the enterprises is increased.
In order to achieve the purpose, the invention adopts the following technical scheme:
a low calorific value fuel tar extraction recycling harmless treatment device comprises a coal gangue powder grinding system, wherein an outlet of the coal gangue powder grinding system is connected with an inlet of a tubular gas-solid two-phase flow coal gangue powder heater, an outlet of the tubular gas-solid two-phase flow coal gangue powder heater is connected with a separation system, a gas outlet of the separation system is connected with a cooling system for separating a coal tar product, and the tail end of the cooling system is connected with a cold chimney;
the solid outlet of the separation system is connected with the fuel inlet of the fluidized bed heat-insulation incinerator, the hearth outlet of the fluidized bed heat-insulation incinerator is connected with a horizontal flue, the horizontal flue is connected with a vertically arranged tail flue, the tail flue is connected with a bag-type dust remover, the tail end of the bag-type dust remover is connected with a powder feeding fan and a hot flue, and the powder feeding fan is connected with a coal gangue powder grinding system;
the lower part of the fuel inlet of the fluidized bed adiabatic incinerator is provided with a hearth, the bottom of the fluidized bed adiabatic incinerator is provided with a primary air inlet, the upper part of the fuel inlet is provided with a secondary air inlet, an inlet pipeline of the fuel inlet is provided with a feeding air port, and the primary air inlet, the secondary air inlet and the feeding air port are connected with an air feeder.
The invention also has the following technical characteristics:
preferably, the coal gangue powder grinding system comprises a coal feeder, an outlet of the coal feeder is connected with an inlet of a descending dryer, an inlet of the descending dryer is further connected with an outlet of a blower, an outlet of the descending dryer is connected with an inlet of a coal mill, an outlet of the coal mill is connected with an inlet of a coarse powder separator, and an inlet of the coarse powder separator is connected with an inlet of a tubular gas-solid two-phase flow coal gangue powder heater.
Preferably, the separation system comprises a cyclone separator, the inlet of the cyclone separator is connected with the outlet of the tubular gas-solid two-phase flow coal gangue powder heater, the gas outlet of the cyclone separator is connected to the inlet of a metal filter cartridge bag type separator, the gas outlet of the metal filter cartridge bag type separator is connected to the inlet of the cooling system, and the solid outlets of the cyclone separator and the metal filter cartridge bag type separator are connected to the fuel inlet of the fluidized bed heat-insulating incinerator.
Further, the cooling system comprises a primary heat exchanger with an inlet connected with a gas outlet of the metal filter cartridge bag type separator, a gas outlet of the primary heat exchanger is connected with an inlet of a secondary heat exchanger, an outlet of the secondary heat exchanger is connected with an inlet of a final cooler, and an outlet of the final cooler is connected with a cold chimney;
and coal tar collecting chambers are arranged at the bottoms of the primary heat exchanger, the secondary heat exchanger and the final cooler.
Further, an air outlet of the air feeder is connected with an air preheating system;
the air preheating system comprises an air preheater arranged at the tail end inside the tail flue, an outlet of the air preheater is connected with a heat exchange tube inlet of the secondary heat exchanger, a heat exchange tube outlet of the secondary heat exchanger is connected with a heat exchange tube inlet of the primary heat exchanger, and a heat exchange tube outlet of the primary heat exchanger is connected with a primary air inlet, a secondary air inlet and a feeding air port.
Furthermore, the tubular gas-solid two-phase flow coal gangue powder heater is arranged at the upper part of the air preheater in the tail flue.
Preferably, the bottom of the tail flue is provided with a cold ash hopper and a flue ash outlet;
the bottom of the bag-type dust collector is provided with an ash outlet.
Preferably, a furnace chamber outlet of the fluidized bed adiabatic incinerator is provided with a flame folding angle;
the fluidized bed heat insulation incinerator is characterized in that a slag chamber is arranged at the bottom of the fluidized bed heat insulation incinerator, and a slag outlet is formed in the bottom of the slag chamber.
The invention also protects a low-calorific-value fuel tar extraction recycling harmless treatment method adopting the device, coal gangue is ground into coal gangue powder with the particle size of below 150 mu m by a coal gangue powder grinding system, the coal gangue powder is conveyed into a tubular gas-solid two-phase flow coal gangue powder heater by a powder conveying fan, and the coal gangue powder is subjected to heat insulation in the tubular gas-solid two-phase flow coal gangue powder heater by air to 450-580 ℃ to separate out volatile matters and then enters a separation system;
the coke particles separated out of the coal tar by the separation system enter a fluidized bed heat insulation incinerator at the temperature of 300-450 ℃, and hot air is introduced for combustion;
the furnace temperature of the fluidized bed heat insulation incinerator is 800-900 ℃;
the high-temperature flue gas generated by the combustion of the fluidized bed heat insulation incinerator exchanges heat with the tubular gas-solid two-phase flow coal gangue powder heater and the air preheating system in a convection manner, then enters the bag-type dust remover, is pressurized by the powder feeding fan after dust removal, and then enters the tubular gas-solid two-phase flow heater as a medium for drying and conveying coal gangue powder through the coal gangue powder grinding system;
the temperature of hot air entering the fluidized bed adiabatic incinerator through an air preheating system is 150-250 ℃;
the ash produced after combustion is used for mining area soil improvement and building parameter materials.
Preferably, the circulation ratio of the fluidized-bed adiabatic incinerator is 1.
Compared with the prior art, the invention has the following technical effects:
the invention aims at the recycling and harmless treatment device and method of fuels such as coal gangue, coal slime and the like with low calorific value, the method extracts coal tar in the fuels with low calorific value such as coal gangue by utilizing partial heat energy in the fuels with low calorific value, improves the soil of a mining area by utilizing ash content of the coal tar, realizes the recycling and harmless treatment of energy-containing solid wastes, does not need to additionally input high calorific value fuels in the whole treatment process, and produces good economic benefit by the produced tar and the produced ash content;
in the gasification process of the coal gangue powder, the method avoids the mixing of ash and coke, simultaneously improves the temperature of the fuel entering the combustion furnace, and achieves the purpose of stable combustion of the fluidized bed heat insulation combustion furnace;
the gas-solid two-phase flow gangue powder heater and the air preheater are both arranged in the tail flue, and the flue gas is used as a heat exchange agent of the gas-solid two-phase flow gangue powder heater, the air preheater, the primary heat exchanger, the secondary heat exchanger and the heat exchange tube of the cooler, so that the full utilization of combustion heat is realized, and the energy conservation and the environmental protection are realized;
the low-calorific-value fuel tar extraction recycling harmless treatment device is suitable for large-scale treatment of coal gangue.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
the meaning of each reference number in the figures is: 1-a coal gangue powder grinding system, 2-a tubular gas-solid two-phase flow coal gangue powder heater, 3-a cold chimney, 4-a fluidized bed adiabatic incinerator, 5-a fuel inlet, 6-a hearth outlet, 7-a horizontal flue, 8-a tail flue, 9-a bag-type dust remover, 10-a powder feeding fan, 11-a hot chimney, 12-a hearth, 13-a primary air inlet, 14-a secondary air inlet, 15-a feeding air inlet, 16-a blower, 17-a cyclone separator, 18-a metal filter cartridge bag-type separator, 19-a primary heat exchanger, 20-a secondary heat exchanger, 21-a final cooler, 22-a coal tar collecting chamber, 23-an air preheater, 24-a cold ash bucket, 25-a flue ash outlet, 26-an ash outlet, 27-a flame folding angle, 28-an ash chamber and 29-an ash outlet; 101-feeder, 102-drop dryer, 103-pulverizer, 104-coarse separator.
Detailed Description
The following detailed description of the present invention is provided in connection with the accompanying drawings.
As shown in fig. 1, the present embodiment provides a low calorific value fuel tar extraction recycling harmless treatment device, which includes a coal gangue powder grinding system 1, an outlet of the coal gangue powder grinding system 1 is connected to an inlet of a tubular gas-solid two-phase flow coal gangue powder heater 2, an outlet of the tubular gas-solid two-phase flow coal gangue powder heater 2 is connected to a separation system, a gas outlet of the separation system is connected to a cooling system for separating coal tar products, and a tail end of the cooling system is connected to a cold chimney 3; the particle diameter of the coal gangue powder ground by the coal gangue powder grinding system 1 is below 150 um; the coal gangue powder is isolated from air and heated to 450-580 ℃ in a tubular gas-solid two-phase flow coal gangue powder heater 2 to separate out volatile components;
a solid outlet of the separation system is connected with a fuel inlet 5 of the fluidized bed heat-insulation incinerator 4, a hearth outlet 6 of the fluidized bed heat-insulation incinerator 4 is connected with a horizontal flue 7, the horizontal flue 7 is connected with a vertically arranged tail flue 8, the tail flue 8 is connected with a bag-type dust remover 9, the tail end of the bag-type dust remover 9 is connected with a powder feeding fan 10 and a hot chimney 11, and the powder feeding fan 10 is connected with the coal gangue powder grinding system 1; the coke particles separated out of the coal tar by the separation system enter a fluidized bed adiabatic incinerator 4 to be combusted at the temperature of 300-450 ℃;
the lower part of a fuel inlet 5 of the fluidized bed adiabatic incinerator 4 is provided with a hearth 12, the bottom of the fluidized bed adiabatic incinerator 4 is provided with a primary air inlet 13, the upper part of the fuel inlet 5 is provided with a secondary air inlet 14, an inlet pipeline of the fuel inlet 5 is provided with a feeding air port 15, the primary air inlet 13, the secondary air inlet 14 and the feeding air port 15 are connected with a blower 16, the furnace temperature of the fluidized bed adiabatic incinerator 4 is 800-900 ℃, and the circulation rate of the fluidized bed adiabatic incinerator 4 is 1.
The coal gangue powder grinding system 1 comprises a coal feeder 101, an outlet of the coal feeder 101 is connected with an inlet of a descending dryer 102, an inlet of the descending dryer 102 is further connected with an outlet of a blower 16, an outlet of the descending dryer 102 is connected with an inlet of a coal mill 103, an outlet of the coal mill 103 is connected with an inlet of a coarse powder separator 104, and an inlet of the coarse powder separator 104 is connected with an inlet of a tubular gas-solid two-phase coal gangue powder heater 2. The flue gas for conveying the coal gangue powder in the tubular gas-solid two-phase flow coal gangue powder heater 2 does not contain air.
The separation system comprises a cyclone separator 17 with an inlet connected with an outlet of the tubular gas-solid two-phase flow coal gangue powder heater 2, a gas outlet of the cyclone separator 17 is connected to an inlet of a metal filter cartridge bag type separator 18, a gas outlet of the metal filter cartridge bag type separator 18 is connected to an inlet of the cooling system, and solid outlets of the cyclone separator 17 and the metal filter cartridge bag type separator 18 are connected to a fuel inlet of the fluidized bed heat-insulating incinerator 4.
The cooling system comprises a primary heat exchanger 19, the inlet of which is connected with the gas outlet of the metal filter cartridge bag type separator 18, the gas outlet of the primary heat exchanger 19 is connected with the inlet of a secondary heat exchanger 20, the outlet of the secondary heat exchanger 20 is connected with the inlet of a final cooler 21, and the outlet of the final cooler 21 is connected with the cold chimney 3;
the primary heat exchanger 19, the secondary heat exchanger 20 and the final cooler 21 are cooled step by step to separate out coal tar; the coal tar collecting chambers 22 are arranged at the bottoms of the coal tar collecting chambers;
the heat exchange tubes of the final cooler 21 are fed with a cooling medium.
An air outlet of the air blower 16 is connected with an air preheating system;
the air preheating system comprises an air preheater 23 arranged at the tail end in the tail flue 8, the outlet of the air preheater 23 is connected with the inlet of a heat exchange tube of the secondary heat exchanger 20, the outlet of the heat exchange tube of the secondary heat exchanger 20 is connected with the inlet of a heat exchange tube of the primary heat exchanger 19, and the outlet of the heat exchange tube of the primary heat exchanger 19 is connected with a primary air inlet 13, a secondary air inlet 14 and a feeding air inlet 15; the temperature of hot air entering the fluidized bed adiabatic incinerator 4 through the air preheating system is 150-250 ℃;
the tubular gas-solid two-phase flow coal gangue powder heater 2 is arranged at the upper part of an air preheater 23 in the tail flue 8.
The bottom of the tail flue 8 is provided with a cold ash hopper 24 and a flue ash outlet 25;
the wall surfaces of the horizontal flue 7 and the tail flue 8 are heat insulation wall surfaces.
An arc-shaped flow plate is arranged at the connecting included angle between the horizontal flue 7 and the tail flue 8, so that dust deposition dead corners are prevented from being formed, and overtemperature is prevented.
The outer side of the top end of a tubular gas-solid two-phase flow coal gangue powder heater 2 arranged in a tail flue 8 is provided with a wear-resistant armor, the inner wall of a pipe is provided with a wear-resistant lining, and a thickened wear-resistant material is arranged at a bent pipe; the wear-resistant armor, the wear-resistant lining and the thickened wear-resistant material are used for protecting the pipeline of the tubular gas-solid two-phase flow coal gangue powder heater 2 and prolonging the service life.
The bottom of the bag-type dust collector 9 is provided with an ash outlet 26.
The hearth outlet 6 of the fluidized bed heat insulation incinerator 4 is provided with a flame folding angle 27; the height at the flare angle 27 should be such that the fuel reaches the flare angle 27 and is burned out.
The bottom of the fluidized bed heat insulation incinerator 4 is provided with a slag chamber 28, and the bottom of the slag chamber 28 is provided with a slag outlet 29.
Specific examples are given below for a resource harmless treatment method for extracting tar from low-calorific-value fuel:
example 1: the calorific value of solid fuels such as coal gangue or coal slime is more than or equal to 800kcal
Coal gangue (coal slime and other solid low-calorific-value fuels) is ground into powder with the particle size of below 150 mu m by a coal gangue powder grinding system 1 under the drying of flue gas, the powder can be fluidized by pneumatic conveying, pressurized by a powder conveying fan 10 and conveyed into a tubular gas-solid two-phase flow coal gangue powder heater 2 for heating, and heated to 450-580 ℃ for heat resolution to obtain coal tar. The separated mixture of coal tar, flue gas and coke particles sequentially enters a cyclone separator 17 and a metal filter cartridge bag type separator 18 for gradual separation, and the separated gas (the dust content is lower than 10 mg/m) 3 ) The flue gas enters a primary heat exchanger 19, a secondary heat exchanger 20 and a final cooler 21 to be cooled and condensed step by step to form coal tar, the flue gas enters a cold chimney 3 to be discharged into the atmosphere, the separated high-temperature coke particles enter a fluidized bed heat-insulation incinerator 4, meanwhile, the air preheated by an air preheater 23, the primary heat exchanger 19 and the secondary heat exchanger 20 enters the fluidized bed heat-insulation incinerator 4, the high-temperature coke particles and the air are stably combusted in the fluidized bed heat-insulation incinerator 4, the combusted coke particles are burnt out in a hearth, the generated high-temperature flue gas enters a tail flue 8 to exchange heat with a tubular gas-solid two-phase flow coal gangue powder heater 2 and the air preheater 23, and the low-temperature flue gas and ash with the temperature lower than 200 ℃ enter a bag-type dust collector 9 to be dedusted. The flue gas after dust removal is used as a medium for drying and conveying the coal gangue powder, the medium is pressurized by a powder conveying fan 10 and then enters a coal gangue powder grinding system 1, and the ash content is conveyed to an ash yard for further soil improvement and building blending.
Example 2: the calorific value of solid fuels such as coal gangue or coal slime is less than 800kcal
The coal gangue (solid low-heat-value fuels such as coal slime) has a low heat value, and when the heat value of the coal gangue cannot meet the stable combustion requirement of the incinerator, high-heat-value fuels are mixed according to the stable combustion requirement. Grinding coal gangue into powder with particle diameter below 150 μm by coal gangue grinding system 1, and feeding into tubular air by powder feeding fanHeating the coal gangue powder in the solid-phase flow coal gangue powder heater 2 to 450-580 ℃ to separate out coal tar. The separated mixture of coal tar, flue gas and coke particles sequentially enters a cyclone separator 17 and a metal filter cartridge bag type separator 18 for step-by-step separation, and the separated gaseous substances (the dust content is lower than 10 mg/m) 3 ) The coal tar is gradually cooled and condensed out after entering a primary heat exchanger 19, a secondary heat exchanger 20 and a final cooler 21, the smoke enters a cold chimney 3 and is discharged into the atmosphere, the separated high-temperature coke particles enter a fluidized bed heat-insulation incinerator 4, meanwhile, the air preheated by an air preheater 23, the primary heat exchanger 19 and the secondary heat exchanger 20 enters the fluidized bed heat-insulation incinerator 4, the high-temperature smoke generated by combustion enters a tail flue 8 to exchange heat with a tubular gas-solid two-phase flow coal gangue powder heater 2 and the air preheater 23, and the smoke with the temperature lower than 200 ℃ enters a bag-type dust remover 9 to remove dust. The flue gas after dust removal is used as a medium for drying and conveying powder such as coal gangue and the like, the medium is pressurized by a powder feeding fan 10 and then enters a coal gangue powder grinding system 1, and ash is conveyed to an ash yard to be used as further soil improvement and building blending materials.
It should be noted that the above embodiments are not all embodiments of the present invention, and those skilled in the art can make various changes, substitutions and alterations without departing from the spirit of the present invention.
Claims (10)
1. A low-calorific-value fuel tar extraction recycling harmless treatment device is characterized by comprising a coal gangue powder grinding system (1), wherein an outlet of the coal gangue powder grinding system (1) is connected with an inlet of a tubular gas-solid two-phase flow coal gangue powder heater (2), an outlet of the tubular gas-solid two-phase flow coal gangue powder heater (2) is connected with a separation system, a gas outlet of the separation system is connected with a cooling system for separating a coal tar product, and the tail end of the cooling system is connected with a cold chimney (3);
the solid outlet of the separation system is connected with a fuel inlet (5) of the fluidized bed heat-insulating incinerator (4), a hearth outlet (6) of the fluidized bed heat-insulating incinerator (4) is connected with a horizontal flue (7), the horizontal flue (7) is connected with a vertically arranged tail flue (8), the tail flue (8) is connected with a bag-type dust remover (9), the tail end of the bag-type dust remover (9) is connected with a powder feeding fan (10) and a hot flue (11), and the powder feeding fan (10) is connected with the coal gangue powder grinding system (1); the tubular gas-solid two-phase flow coal gangue powder heater (2) is arranged in the tail flue (8);
the fluidized bed adiabatic incinerator is characterized in that a hearth (12) is arranged on the lower portion of a fuel inlet (5) of the fluidized bed adiabatic incinerator (4), a primary air inlet (13) is formed in the bottom of the fluidized bed adiabatic incinerator (4), a secondary air inlet (14) is formed in the upper portion of the fuel inlet (5), a feeding air port (15) is formed in an inlet pipeline of the fuel inlet (5), and the primary air inlet (13), the secondary air inlet (14) and the feeding air port (15) are connected with an air feeder (16).
2. The low heating value fuel tar extraction recycling harmless treatment device according to claim 1, wherein the coal gangue powder grinding system (1) comprises a coal feeder (101), an outlet of the coal feeder (101) is connected with an inlet of a descending dryer (102), an inlet of the descending dryer (102) is further connected with an outlet of a blower (16), an outlet of the descending dryer (102) is connected with an inlet of a coal mill (103), an outlet of the coal mill (103) is connected with an inlet of a coarse powder separator (104), and an inlet of the coarse powder separator (104) is connected with an inlet of a tubular gas-solid two-phase coal gangue powder heater (2).
3. The low-heating-value fuel tar extraction recycling harmless treatment device according to claim 1, wherein the separation system comprises a cyclone separator (17) with an inlet connected with an outlet of the tubular gas-solid two-phase coal gangue powder heater (2), a gas outlet of the cyclone separator (17) is connected to an inlet of the metal filter cartridge bag separator (18), a gas outlet of the metal filter cartridge bag separator (18) is connected to an inlet of the cooling system, and solid outlets of the cyclone separator (17) and the metal filter cartridge bag separator (18) are connected to a fuel inlet of the fluidized bed adiabatic incinerator (4).
4. The low-heating-value fuel tar extraction resource harmless treatment device according to claim 3, wherein the cooling system comprises a primary heat exchanger (19) with an inlet connected with a gas outlet of the metal filter cartridge bag separator (18), a gas outlet of the primary heat exchanger (19) is connected with an inlet of a secondary heat exchanger (20), an outlet of the secondary heat exchanger (20) is connected with an inlet of a final cooler (21), and an outlet of the final cooler (21) is connected with the cold chimney (3);
and coal tar collecting chambers (22) are arranged at the bottoms of the primary heat exchanger (19), the secondary heat exchanger (20) and the final cooler (21).
5. The low heating value fuel tar extraction recycling harmless treatment device according to claim 4, characterized in that an air outlet of the blower (16) is connected with an air preheating system;
the air preheating system comprises an air preheater (23) arranged at the inner tail end of a tail flue (8), the outlet of the air preheater (23) is connected with the heat exchange tube inlet of a secondary heat exchanger (20), the heat exchange tube outlet of the secondary heat exchanger (20) is connected with the heat exchange tube inlet of a primary heat exchanger (19), and the heat exchange tube outlet of the primary heat exchanger (19) is connected with a primary air inlet (13), a secondary air inlet (14) and a feed air inlet (15).
6. The low heating value fuel tar extraction recycling harmless treatment device as claimed in claim 5, wherein the tubular gas-solid two-phase flow coal gangue powder heater (2) is arranged at the upper part of an air preheater (23) in the tail flue (8).
7. The low-heating-value fuel tar extraction recycling harmless treatment device as recited in claim 1, wherein a cold ash hopper (24) and a flue ash outlet (25) are arranged at the bottom of the tail flue (8);
an ash outlet (26) is arranged at the bottom of the bag-type dust collector (9).
8. The low-heating-value fuel tar-extraction resource harmless treatment device according to claim 1, characterized in that a furnace outlet (6) of the fluidized bed heat-insulation incinerator (4) is provided with a flame-folding angle (27);
the bottom of the fluidized bed heat insulation incinerator (4) is provided with an ash chamber (28), and the bottom of the ash chamber (28) is provided with an ash outlet (29).
9. A low heating value fuel tar extraction recycling harmless treatment method adopting the device of any one of claims 1-8, characterized in that coal gangue is ground into coal gangue powder with the particle size of below 150um by a coal gangue powder grinding system (1), the coal gangue powder is conveyed into a tubular gas-solid two-phase flow coal gangue powder heater (2) by a powder conveying fan (10), and the coal gangue powder is isolated from air in the tubular gas-solid two-phase flow coal gangue powder heater (2) and heated to 450 to 580 ℃ to separate out volatile matters and then enters a separation system;
the coke particles separated out of the coal tar by the separation system enter a fluidized bed adiabatic incinerator (4) at the temperature of 300 to 450 ℃, and hot air is introduced for combustion;
the furnace temperature of the fluidized bed adiabatic incinerator (4) is 800 to 900 ℃;
the high-temperature flue gas generated by combustion of the fluidized bed heat insulation incinerator (4) exchanges heat with the tubular gas-solid two-phase flow coal gangue powder heater (2) and the air preheating system in a convection manner, then enters the bag-type dust remover (9), is pressurized by the powder feeding fan (10) after dust removal, and then enters the tubular gas-solid two-phase flow coal gangue powder heater (2) as a medium for drying and conveying coal gangue powder through the coal gangue powder grinding system (1);
the temperature of hot air entering the fluidized bed adiabatic incinerator (4) through an air preheating system is 150 to 250 ℃;
the ash generated after combustion is used for mining area soil improvement and building additive materials.
10. The method for recycling and harmlessly processing low-heating-value fuel tar as claimed in claim 9, wherein the circulation ratio of the fluidized-bed adiabatic incinerator (4) is 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210402412.2A CN114719267B (en) | 2022-04-18 | 2022-04-18 | Recycling harmless treatment device and method for extracting tar from low-calorific-value fuel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210402412.2A CN114719267B (en) | 2022-04-18 | 2022-04-18 | Recycling harmless treatment device and method for extracting tar from low-calorific-value fuel |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114719267A CN114719267A (en) | 2022-07-08 |
| CN114719267B true CN114719267B (en) | 2023-01-03 |
Family
ID=82243475
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210402412.2A Active CN114719267B (en) | 2022-04-18 | 2022-04-18 | Recycling harmless treatment device and method for extracting tar from low-calorific-value fuel |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114719267B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19513832A1 (en) * | 1995-04-12 | 1996-10-17 | Noell Dbi Energie Entsorgung | Utilising residues and waste material |
| CN1415891A (en) * | 2001-10-31 | 2003-05-07 | 清华大学 | Combustion method and device for denitration by refueling pyrolysis gas of biomass |
| CN106753489A (en) * | 2016-11-25 | 2017-05-31 | 华能国际电力股份有限公司 | A kind of pyrolysis of coal steam based on coal-powder boiler, burnt oil and gas co-generation system and technique |
| CN112082151A (en) * | 2020-09-01 | 2020-12-15 | 中国科学院工程热物理研究所 | Multi-pollutant collaborative removing and burning device and method for circulating fluidized bed boiler |
-
2022
- 2022-04-18 CN CN202210402412.2A patent/CN114719267B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19513832A1 (en) * | 1995-04-12 | 1996-10-17 | Noell Dbi Energie Entsorgung | Utilising residues and waste material |
| CN1415891A (en) * | 2001-10-31 | 2003-05-07 | 清华大学 | Combustion method and device for denitration by refueling pyrolysis gas of biomass |
| CN106753489A (en) * | 2016-11-25 | 2017-05-31 | 华能国际电力股份有限公司 | A kind of pyrolysis of coal steam based on coal-powder boiler, burnt oil and gas co-generation system and technique |
| CN112082151A (en) * | 2020-09-01 | 2020-12-15 | 中国科学院工程热物理研究所 | Multi-pollutant collaborative removing and burning device and method for circulating fluidized bed boiler |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114719267A (en) | 2022-07-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP2008516183A (en) | How to improve the quality of high moisture content using system heat source | |
| CN101117584A (en) | Integral process for oil shale retorting oil refining and coal-char combustion power generation | |
| CN102433142B (en) | Quality-improving technique combining low-rank coal pneumatic drying with multi-tube revolving dry distillation and system for same | |
| CN103242869A (en) | Device and method for pyrolyzing and carbonizing biomass at low temperature by utilizing boiler flue gas | |
| CN102952558B (en) | Integral process for oil shale drying, heating, refining and semicoke burning | |
| CN102840593A (en) | Fume dried lignite medium speed mill powder-making system | |
| CN101289621B (en) | Process for preparing carbocoal, coke tar and coal gas by treating bovey coal by suspending pyrogenation device | |
| CN105314812A (en) | Sludge treatment system and treatment method thereof | |
| CN102798134A (en) | Furnace smoke drying and water recycling warehouse-type fan mill hot air powder supplying and making system | |
| CN102061211B (en) | Integral purified integration system and process of lignite in cement production through catalytic mild pyrolysis | |
| CN102329628A (en) | Large-size low-temperature destructive distillation system for low-order lignite | |
| CN102533296A (en) | Oil shale rotary kiln dry distillation and circulating fluidized bed combustion process | |
| CN101100607A (en) | Coking technique using coal external burning to replace gas fuel burning | |
| CN106439892A (en) | Mixed powder preparation system with coal and sludge coupling combustion power generation | |
| CN101289622A (en) | Process for raise quality of bovey coal by solid thermal-loading suspending pyrogenation device of bovey coal | |
| CN205170639U (en) | Sludge treatment system | |
| CN114719267B (en) | Recycling harmless treatment device and method for extracting tar from low-calorific-value fuel | |
| CN202132966U (en) | Smoke-predrying fan mill direct blowing type powder making system for brown coal | |
| CN106838917A (en) | The anoxybiotic pyrolysis treatment systems and method of a kind of rubbish | |
| CN201053005Y (en) | Low-temperature pyrolysis combination producing device for furnace slag and coal powder | |
| CN201033772Y (en) | Integral system for oil shale retorting oil refining and coal-char combustion power generation | |
| CN106010610A (en) | Low-order pulverized coal hydrogenated and pressurized fast low-temperature carbonization process and device | |
| CN202132967U (en) | Direct blowing power making system of smoke pre-drying lignite steel ball mill | |
| CN108977250A (en) | A kind of waste tire of automobile and agricultural stalk fuel combination processing unit and method | |
| CN114963188A (en) | Adiabatic incinerator of coal gangue tar extraction fluidized bed |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |