CN102734791B - Process for activating grate-fired flying ash semi-coke and catalytically reducing nitric oxide in boiler - Google Patents
Process for activating grate-fired flying ash semi-coke and catalytically reducing nitric oxide in boiler Download PDFInfo
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- CN102734791B CN102734791B CN201210213117.9A CN201210213117A CN102734791B CN 102734791 B CN102734791 B CN 102734791B CN 201210213117 A CN201210213117 A CN 201210213117A CN 102734791 B CN102734791 B CN 102734791B
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Abstract
The invention discloses a process for activating grate-fired flying ash semi-coke and catalytically reducing nitric oxide in a boiler, and relates to the process for reducing nitric oxide in the boiler. The process solve the problems of large emission amount of NOx of a conventional grate-fired boiler and the lack of an economic and efficient NOx control technology. The device scheme adopted by the method is that: the grate-fired boiler is communicated with a selective gas-solid separator; the semi-coke outlet of the selective gas-solid separator is communicated with the semi-coke inlet of a semi-coke cabin; the semi-coke outlet of the semi-coke cabin is communicated with the semi-coke inlet of a humidifying activator; and a hot air pipe and/or a hot smoke pipe is communicated with the hot air and/or hot smoke inlet of the humidifying activator. The method comprises the following steps of: performing gas-solid separation on the coal-fired flue gas from the grate-fired boiler in the selective gas-solid separator, and performing humidifying activation reaction between the semi-coke and water vapor in the humidifying activator. By the device and the process, the low emission of NOx of the grate-fired boiler and the collaborative NOx control in a combustion process are realized.
Description
Technical field
The present invention relates to a kind of method that can realize grate firing boiler nitrogen oxide and reduce discharging.
Background technology
China's active service coal-burned industrial boiler about 54.6 ten thousand, accounts for 85% of current in-service Industrial Boiler sum, and every year with about 1.5% speed increase.Coal-burned industrial boiler year coal consumption 5-6 hundred million tons, accounts for whole nation year by 18% of coal total amount.The total energy consumption that Industrial Boiler is annual and disposal of pollutants all occupy national industrial trade second.
In the research of Industrial Boiler pollution reduction, SO
2carry out relatively early with the research of flue dust, and obtained many achievements in research, and industrial applications.Due to features such as Industrial Boiler low-temperature burnings, the NOx amount that it is generated compares less (400-700mg/Nm
3).So the NOx emission reduction work of Industrial Boiler is not subject to sufficient attention always.The environmental requirement of China in recent years improves year by year, and the NOx emission problem of Industrial Boiler is highlighted all the more.Particularly NOx in urban air environment to PM
2.5secondary source contribution rate receive publicity gradually.Therefore, the economical grate firing boiler low NOx combusting technology that exploitation is collaborative with combustion process, seems very urgent.
The current grate firing boiler coal of China still can not realize dynamic blending coals.The coal particle size distribution span used is very large, and the particle of below 3-5mm occupies very large ratio.This situation just result in containing a large amount of uncombusted semicoke in burning flying dust, and its domain size distribution is not from 0.1mm-2mm etc.This part of semicoke is the product of coal after preliminary pyrolysis or gasification, is directly taken away from fire grate enter dust-removing device for boiler by flue gas.If this part of semicoke optionally can be separated from flue gas, sent back to the suitable location of combustion chamber, under the prerequisite ensureing its after-flame, may be realized it to the effective reduction generating NO in combustion process.
Summary of the invention
The object of this invention is to provide the activation of a kind of grate firing flying dust semicoke and for the method for catalyzing and reducing nitrogen oxides in stove, large to solve current grate firing boiler NOx discharge, lack the problem of economical and efficient NOx control technology.
The present invention solves the problems of the technologies described above the technical scheme taked to be: a kind of grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove, described method is that the device based on the activation of grate firing flying dust semicoke and for catalyzing and reducing nitrogen oxides in stove realizes, described device comprises grate firing boiler, selective gas-solid separator, half coke bin, humidification activation device, first pipeline, blower fan, warm-air pipe and thermal chimney, left furnace wall and the right furnace wall of grate firing boiler have been arranged symmetrically with swirl injection device, the ash-laden gas of grate firing boiler is communicated with semicoke entrance point with the ash-laden gas of selective gas-solid separator by the first pipeline with the semicoke port of export, the top of selective gas-solid separator is provided with the ash-laden gas port of export, the semicoke port of export of selective gas-solid separator is communicated with the semicoke entrance point of half coke bin, the semicoke port of export of half coke bin is communicated with the semicoke entrance point of humidification activation device, humidification activation device is provided with water vapour entrance point, warm-air pipe is communicated with heat smoke entrance point with the hot-air of humidification activation device by blower fan with thermal chimney, the port of export of humidification activation device is communicated with two swirl injection devices,
Described method comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler 1 enters into selective gas-solid separator 2 and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin 3;
Step 2, half coke bin 3 transport semicoke in humidification activation device 4, now water vapour, hot-air and heat smoke are passed in humidification activation device 4, semicoke and water vapour carry out humidification activation reaction in humidification activation device 4, reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the hot-air in humidification activation device 4 is 110-160 DEG C, and the temperature being passed into the heat smoke in humidification activation device 4 is 80-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device 1-1 and by swirl injection device 1-1 clockwise or be rotated counterclockwise jet and enter into burner hearth by hot-air and heat smoke, time wherein in swirl injection device 1-1 is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
A kind of grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove, described method is that the device based on the activation of grate firing flying dust semicoke and for catalyzing and reducing nitrogen oxides in stove realizes, described device comprises grate firing boiler, selective gas-solid separator, half coke bin, humidification activation device, first pipeline, blower fan, warm-air pipe, left furnace wall and the right furnace wall of grate firing boiler have been arranged symmetrically with swirl injection device, the ash-laden gas of grate firing boiler 1 is communicated with semicoke entrance point with the ash-laden gas of selective gas-solid separator by the first pipeline with the semicoke port of export, the top of selective gas-solid separator is provided with the ash-laden gas port of export, the semicoke port of export of selective gas-solid separator is communicated with the semicoke entrance point of half coke bin 3, the semicoke port of export of half coke bin is communicated with the semicoke entrance point of humidification activation device, humidification activation device 4 is provided with water vapour entrance point, warm-air pipe is communicated with the hot-air inlets end of humidification activation device by blower fan, the port of export of humidification activation device 4 is communicated with two swirl injection devices,
Described method comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler enters into selective gas-solid separator and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin;
Step 2, half coke bin 3 transport semicoke in humidification activation device, now water vapour and hot-air are passed in humidification activation device, semicoke and water vapour carry out humidification activation reaction in humidification activation device, reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the hot-air in humidification activation device is 110-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device and by swirl injection device clockwise or be rotated counterclockwise jet and enter into burner hearth by hot-air, time wherein in swirl injection device is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
A kind of grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove, described method is that the device based on the activation of grate firing flying dust semicoke and for catalyzing and reducing nitrogen oxides in stove realizes, described device comprises grate firing boiler 1, selective gas-solid separator, half coke bin, humidification activation device, first pipeline, blower fan, thermal chimney, left furnace wall and the right furnace wall of grate firing boiler have been arranged symmetrically with swirl injection device, the ash-laden gas of grate firing boiler is communicated with semicoke entrance point with the ash-laden gas of selective gas-solid separator by the first pipeline with the semicoke port of export, the top of selective gas-solid separator is provided with the ash-laden gas port of export, the semicoke port of export of selective gas-solid separator is communicated with the semicoke entrance point of half coke bin, the semicoke port of export of half coke bin is communicated with the semicoke entrance point of humidification activation device, humidification activation device is provided with water vapour entrance point, thermal chimney is communicated with the heat smoke entrance point of humidification activation device by blower fan, the port of export of humidification activation device is communicated with two swirl injection devices,
Described method comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler 1 enters into selective gas-solid separator 2 and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin 3;
Step 2, half coke bin 3 transport semicoke in humidification activation device, now water vapour and heat smoke are passed in humidification activation device, semicoke and water vapour carry out humidification activation reaction in humidification activation device, reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the heat smoke in humidification activation device 4 is 80-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device and by swirl injection device clockwise or be rotated counterclockwise jet and enter into burner hearth by heat smoke, time wherein in swirl injection device is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
The present invention has following beneficial effect: 1, adopt selective semicoke gathering-device, it is greater than 95% to the arresting efficiency of more than 0.1mm particle, and SR is less than 500Pa, can realize efficiently being separated the lower resistance of semicoke; 2, semicoke contacts with steam after collecting, mixes in steam activation device, because the temperature of semicoke is higher, may present hot happy and harmonious state, therefore when 0.2-0.6MPa steam reacts to fashionable rapid generation as follows: C+H
2o → CO+H
2-132KJ, CO+H
2o → CO
2+ H
2+ 41KJ and C+CO
2→ 2CO-172KJ, simultaneously the pore structure of semicoke, specific area are enriched greatly.This reacts the abundanter contact area provided for semicoke transported substance in combustion space, for the catalytic reduction process strengthening NO provides condition.When your semicoke is given fashionable meeting catalysis, strengthened following course of reaction, and then realize the efficient reduction to NO: CO+NO → N
2+ CO
2; 3, semicoke class material accounts for the ratio of total furnace coal weight at about 0.5-1.5%, the collection of semicoke class material after-flame, can improve boiler combustion efficiency 0.5-1.5%.
Accompanying drawing explanation
Fig. 1 is the overall structure schematic diagram of apparatus of the present invention scheme, and Fig. 2 is the A-A sectional view of Fig. 1.
Detailed description of the invention
Detailed description of the invention one: composition graphs 1 and Fig. 2 illustrate present embodiment, the device of present embodiment comprises grate firing boiler 1, selective gas-solid separator 2, half coke bin 3, humidification activation device 4, first pipeline 5, blower fan 6, warm-air pipe and thermal chimney 7, the left furnace wall of grate firing boiler 1 and right furnace wall have been arranged symmetrically with swirl injection device 1-1, the ash-laden gas of grate firing boiler 1 is communicated with semicoke entrance point by the ash-laden gas of the first pipeline 5 with selective gas-solid separator 2 with the semicoke port of export, the top of selective gas-solid separator 2 is provided with ash-laden gas port of export 2-1, the semicoke port of export of selective gas-solid separator 2 is communicated with the semicoke entrance point of half coke bin 3, the semicoke port of export of half coke bin 3 is communicated with the semicoke entrance point of humidification activation device 4, humidification activation device 4 is provided with water vapour entrance point, warm-air pipe is communicated with heat smoke entrance point with the hot-air of humidification activation device 4 by blower fan 6 with thermal chimney 7, the port of export of humidification activation device 4 is communicated with two swirl injection device 1-1.
Detailed description of the invention two: composition graphs 1 illustrates present embodiment, the device of present embodiment also comprises control valve 8, the semicoke port of export of half coke bin 3 is communicated with position with the semicoke entrance point of humidification activation device 4 and is provided with described control valve 8, and this structure is for controlling the quality entering into humidification activation device 4 semicoke.Other embodiment is identical with detailed description of the invention one.
Detailed description of the invention three: composition graphs 1 and Fig. 2 illustrate present embodiment, the described technique of present embodiment comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler 1 enters into selective gas-solid separator 2 and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin 3;
Step 2, half coke bin 3 transport semicoke in humidification activation device 4, now water vapour, hot-air and heat smoke are passed in humidification activation device 4, semicoke and water vapour carry out humidification activation reaction in humidification activation device 4, reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the hot-air in humidification activation device 4 is 110-160 DEG C, and the temperature being passed into the heat smoke in humidification activation device 4 is 80-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device 1-1 and by swirl injection device 1-1 clockwise or be rotated counterclockwise jet and enter into burner hearth by hot-air and heat smoke, time wherein in swirl injection device 1-1 is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
When oxygen at furnace exit is lower than 5.5%, fuel fugitive constituent higher than 35% time, adopt hot-air loopback semicoke; When oxygen at furnace exit is higher than 10%, fuel fugitive constituent higher than 25% time, adopt heat smoke loopback semicoke; When oxygen at furnace exit is between 5.5%-10%, fuel fugitive constituent, higher than when 25%-35%, adopts heat smoke, hot-air mixing loopback semicoke.
Detailed description of the invention four: composition graphs 1 and Fig. 2 illustrate present embodiment, the described technique of present embodiment comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler 1 enters into selective gas-solid separator 2 and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin 3;
Step 2, half coke bin 3 transport semicoke in humidification activation device 4, now water vapour and hot-air are passed in humidification activation device 4, semicoke and water vapour carry out humidification activation reaction in humidification activation device 4, reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the hot-air in humidification activation device 4 is 110-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device 1-1 and by swirl injection device 1-1 clockwise or be rotated counterclockwise jet and enter into burner hearth by hot-air, time wherein in swirl injection device 1-1 is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
When oxygen at furnace exit is lower than 5.5%, fuel fugitive constituent higher than 35% time, adopt hot-air loopback semicoke.
Detailed description of the invention five: composition graphs 1 and Fig. 2 illustrate present embodiment, the described technique of present embodiment comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler 1 enters into selective gas-solid separator 2 and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin 3;
Step 2, half coke bin 3 transport semicoke in humidification activation device 4, now water vapour and heat smoke are passed in humidification activation device 4, semicoke and water vapour carry out humidification activation reaction in humidification activation device 4, reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the heat smoke in humidification activation device 4 is 80-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device 1-1 and by swirl injection device 1-1 clockwise or be rotated counterclockwise jet and enter into burner hearth by heat smoke, time wherein in swirl injection device 1-1 is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
When oxygen at furnace exit is higher than 10%, fuel fugitive constituent higher than 25% time, adopt heat smoke loopback semicoke.
Detailed description of the invention six: composition graphs 1 and Fig. 2 illustrate present embodiment, in the step 2 of present embodiment, heat smoke is extracted by the smoke outlet of grate firing boiler and uses, and flue gas recirculation can utilize by this step, reduces exhaust emission.Other embodiment is identical with detailed description of the invention three.
Claims (5)
1. grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove, described method is that the device based on the activation of grate firing flying dust semicoke and for catalyzing and reducing nitrogen oxides in stove realizes, described device comprises grate firing boiler (1), selective gas-solid separator (2), half coke bin (3), humidification activation device (4), first pipeline (5), blower fan (6), warm-air pipe and thermal chimney (7), the left furnace wall of grate firing boiler (1) and right furnace wall have been arranged symmetrically with swirl injection device (1-1), the ash-laden gas of grate firing boiler (1) is communicated with semicoke entrance point by the ash-laden gas of the first pipeline (5) with selective gas-solid separator (2) with the semicoke port of export, the top of selective gas-solid separator (2) is provided with the ash-laden gas port of export (2-1), the semicoke port of export of selective gas-solid separator (2) is communicated with the semicoke entrance point of half coke bin (3), the semicoke port of export of half coke bin (3) is communicated with the semicoke entrance point of humidification activation device (4), humidification activation device (4) is provided with water vapour entrance point, warm-air pipe is communicated with heat smoke entrance point by the hot-air of blower fan (6) with humidification activation device (4) with thermal chimney (7), the port of export of humidification activation device (4) is communicated with two swirl injection devices (1-1),
It is characterized in that described method comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler (1) enters into selective gas-solid separator (2) and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin (3);
Step 2, half coke bin (3) transport semicoke in humidification activation device (4), now water vapour, hot-air and heat smoke are passed in humidification activation device (4), semicoke and water vapour carry out humidification activation reaction in humidification activation device (4), reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, the temperature being wherein passed into the hot-air in humidification activation device (4) is 110-160 DEG C, and the temperature being passed into the heat smoke in humidification activation device (4) is 80-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device (1-1) and by swirl injection device (1-1) clockwise or be rotated counterclockwise jet and enter into burner hearth by hot-air and heat smoke, time wherein in swirl injection device (1-1) is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
2. grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove, described method is that the device based on the activation of grate firing flying dust semicoke and for catalyzing and reducing nitrogen oxides in stove realizes, described device comprises grate firing boiler (1), selective gas-solid separator (2), half coke bin (3), humidification activation device (4), first pipeline (5), blower fan (6), warm-air pipe (7), the left furnace wall of grate firing boiler (1) and right furnace wall have been arranged symmetrically with swirl injection device (1-1), the ash-laden gas of grate firing boiler (1) is communicated with semicoke entrance point by the ash-laden gas of the first pipeline (5) with selective gas-solid separator (2) with the semicoke port of export, the top of selective gas-solid separator (2) is provided with the ash-laden gas port of export (2-1), the semicoke port of export of selective gas-solid separator (2) is communicated with the semicoke entrance point of half coke bin (3), the semicoke port of export of half coke bin (3) is communicated with the semicoke entrance point of humidification activation device (4), humidification activation device (4) is provided with water vapour entrance point, warm-air pipe (7) is communicated with by the hot-air inlets end of blower fan (6) with humidification activation device (4), the port of export of humidification activation device (4) is communicated with two swirl injection devices (1-1),
It is characterized in that described method comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler (1) enters into selective gas-solid separator (2) and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin (3);
Step 2, half coke bin (3) transport semicoke in humidification activation device (4), now water vapour and hot-air are passed in humidification activation device (4), semicoke and water vapour carry out humidification activation reaction in humidification activation device (4), reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the hot-air in humidification activation device (4) is 110-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device (1-1) and by swirl injection device (1-1) clockwise or be rotated counterclockwise jet and enter into burner hearth by hot-air, time wherein in swirl injection device (1-1) is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
3. grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove, described method is that the device based on the activation of grate firing flying dust semicoke and for catalyzing and reducing nitrogen oxides in stove realizes, described device comprises grate firing boiler (1), selective gas-solid separator (2), half coke bin (3), humidification activation device (4), first pipeline (5), blower fan (6), thermal chimney (7), the left furnace wall of grate firing boiler (1) and right furnace wall have been arranged symmetrically with swirl injection device (1-1), the ash-laden gas of grate firing boiler (1) is communicated with semicoke entrance point by the ash-laden gas of the first pipeline (5) with selective gas-solid separator (2) with the semicoke port of export, the top of selective gas-solid separator (2) is provided with the ash-laden gas port of export (2-1), the semicoke port of export of selective gas-solid separator (2) is communicated with the semicoke entrance point of half coke bin (3), the semicoke port of export of half coke bin (3) is communicated with the semicoke entrance point of humidification activation device (4), humidification activation device (4) is provided with water vapour entrance point, thermal chimney (7) is communicated with by the heat smoke entrance point of blower fan (6) with humidification activation device (4), the port of export of humidification activation device (4) is communicated with two swirl injection devices (1-1),
It is characterized in that described method comprises the steps:
The coal-fired flue-gas of step one, grate firing boiler (1) enters into selective gas-solid separator (2) and carries out gas solid separation, and after gas solid separation, flue gas is discharged, and the semicoke that particle diameter is greater than 0.1mm is collected in half coke bin (3);
Step 2, half coke bin (3) transport semicoke in humidification activation device (4), now water vapour and heat smoke are passed in humidification activation device (4), semicoke and water vapour carry out humidification activation reaction in humidification activation device (4), reaction time is 5-7 second, the pressure of water vapour is 0.4-0.6MPa, water vapour and semicoke mass ratio are 0.2-0.35, and the temperature being wherein passed into the heat smoke in humidification activation device (4) is 80-160 DEG C;
The gaseous product of the reaction of humidification activation described in step 3, step 2 is carbon monoxide and hydrogen, carbon monoxide, hydrogen and semicoke to be brought in swirl injection device (1-1) and by swirl injection device (1-1) clockwise or be rotated counterclockwise jet and enter into burner hearth by heat smoke, time wherein in swirl injection device (1-1) is 0.1-0.2 second, in burner hearth, carbon monoxide and hydrogen and nitrogen oxide react, in burner hearth, the reaction time of carbon monoxide and hydrogen and nitrogen oxide is 2-5.5 second, realizes the reduction of nitrogen oxide.
4. grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove according to claim 1,2 or 3, it is characterized in that the activation of described grate firing flying dust semicoke and device for catalyzing and reducing nitrogen oxides in stove also comprises control valve (8), the semicoke port of export of half coke bin (3) is communicated with position with the semicoke entrance point of humidification activation device (4) and is provided with described control valve (8).
5. grate firing flying dust semicoke activation for the method for catalyzing and reducing nitrogen oxides in stove according to claim 1 or 3, to is characterized in that in described step 2 that heat smoke is extracted by the smoke outlet of grate firing boiler and uses.
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| CN109945160A (en) * | 2019-03-11 | 2019-06-28 | 哈尔滨工业大学 | A kind of flue gas recirculation combustion system |
| CN113332840A (en) * | 2021-05-28 | 2021-09-03 | 上海交通大学 | Modified pulverized coal partial gasification reburning NOx emission reduction device and method |
| CN113280353A (en) * | 2021-05-28 | 2021-08-20 | 上海交通大学 | Sludge treatment and coal-fired NOx emission reduction integrated device and method |
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| CN202660533U (en) * | 2012-06-26 | 2013-01-09 | 哈尔滨工业大学 | Device for activation of grate-fired fly ash semi-coke and furnace catalytic reduction of nitric oxide (NOx) |
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| JP2005274015A (en) * | 2004-03-24 | 2005-10-06 | Mitsui Eng & Shipbuild Co Ltd | Circulation fluidized bed boiler device and its operation control method |
| JP2006189199A (en) * | 2005-01-06 | 2006-07-20 | Mitsui Eng & Shipbuild Co Ltd | Premixed combustion method of fuel of high sulfur content and fuel of high chlorine content |
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| CN2076197U (en) * | 1990-11-01 | 1991-05-01 | 清华大学 | Layered combustion boiler with elevated temp fly ash return device |
| CN1385500A (en) * | 2002-05-12 | 2002-12-18 | 郑州永泰能源新设备有限公司 | Fluidized bed water gas production method equipped with auxiliary bed reactor and installation thereof |
| CN202660533U (en) * | 2012-06-26 | 2013-01-09 | 哈尔滨工业大学 | Device for activation of grate-fired fly ash semi-coke and furnace catalytic reduction of nitric oxide (NOx) |
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