CN213528065U - Sintering flue gas desulfurization and denitrification device - Google Patents
Sintering flue gas desulfurization and denitrification device Download PDFInfo
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- CN213528065U CN213528065U CN202022207416.4U CN202022207416U CN213528065U CN 213528065 U CN213528065 U CN 213528065U CN 202022207416 U CN202022207416 U CN 202022207416U CN 213528065 U CN213528065 U CN 213528065U
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- flue gas
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The utility model discloses a sintering flue gas desulfurization and denitration device belongs to iron and steel trade environmental protection field, including desulfurization assembly, dust removal condensation assembly, flue gas heat transfer assembly, thermal cycle assembly and denitration assembly. Compared with the prior art, the utility model discloses can all stabilize work under any circumstance, avoid wet flue gas desulfurization export flue gas to take away more moisture content, cause discharge port flue gas tailing overlength, realize that chimney above the zero degree does not have visual smoke feather.
Description
Technical Field
The utility model relates to an environmental protection field, especially a wet flue gas desulfurization denitrification facility suitable for ferrous metallurgy trade flue gas is handled.
Background
The ferrous metallurgy industry is an important flow direction of coal consumption and is also an important object for preventing and controlling air pollution in recent years. In recent years, through popularization of a wet flue gas desulfurization technology, emission concentrations of main pollution source particles, sulfur dioxide and nitrogen oxides are greatly reduced, however, pollutants such as a large amount of water vapor, a small amount of ultrafine particles and soluble solids are carried in flue gas generated by combustion between raw materials and fuel, certain pollution is caused to the environment, and when saturated flue gas is emitted to the atmosphere, a white smoke plume phenomenon is generated under sunlight refraction, and visual pollution is caused. Therefore, regulations for eliminating white smoke plume of chimney have been provided in foreign and domestic parts.
The current common ultra-clean discharge process comprises the following steps: wet desulfurization + selective catalytic reduction denitration (SCR). The rated temperature range of the medium-high temperature catalyst adopted in the SCR is 200-320 ℃, but when the SCR is just started or the flue gas volume is less than 1/3 of the rated flue gas volume, the temperature of the SCR catalyst cannot meet the ammonia injection condition, and the catalytic reaction is sufficiently supported, so that a high-temperature mode is adopted under the condition of just starting or insufficient flue gas, namely the inlet air temperature at the cold end of a flue gas heat exchanger is higher than 80 ℃, the heat supplement is more than 260 ℃, and the SCR operation temperature is 280 ℃, so that the NOx emission cannot exceed the standard. Also, this high heat situation is accompanied by high moisture content, so that the white plume is difficult to control at start-up or in case of insufficient smoke. And the moisture content is high, the particles are easy to be entrained, the SCR and the GGH are easy to cause the excessive emission of the particles in the blowing process, and the particles in the desulfurized flue gas cannot be removed again.
SUMMERY OF THE UTILITY MODEL
The technical task of the utility model is not enough to above prior art, provides a sintering flue gas desulfurization denitrification facility, makes it all can stable work under any circumstance.
The technical proposal of the utility model for solving the technical problem is that: the utility model provides a sintering flue gas desulfurization denitrification facility which characterized in that: the system comprises a desulfurization assembly, a dust removal condensation assembly, a flue gas heat exchange assembly, a thermal cycle assembly and a denitration assembly;
the desulfurization assembly comprises a tube bundle demister, a spraying layer and a pneumatic desulfurization unit which are sequentially arranged in a shell; the side wall of the lower part of the shell is provided with an air inlet, and the top of the shell is provided with an air outlet; the spraying layer is connected with the liquid inlet, and a liquid outlet is formed in the bottom of the shell; the liquid outlet and the liquid inlet are connected through a slurry condenser; the pneumatic desulfurization units are arranged in a dot matrix manner; the bottom of the pneumatic desulfurization unit is provided with a cyclone; the tube bundle demister comprises a cyclone cylinder and a cyclone plate;
the dust removal condensation assembly comprises a wet dust remover and a flue gas condenser which are sequentially connected; the inlet of the wet dust collector is connected with the gas outlet of the desulfurization assembly, and the water path of the flue gas condenser is connected with the cooling tower;
the flue gas heat exchange assembly comprises a medium type flue gas heat exchanger and a rotary type flue gas heat exchanger; the medium type flue gas heat exchanger comprises a cooling side and a heating side which are connected by a water path, the front end of an air passage of the cooling side is connected with a smoke outlet of the sintering machine, and the rear end of the air passage of the cooling side is connected with an air inlet of the desulfurization assembly; the front end of the temperature-rising side air passage is connected with the outlet of the flue gas condenser, and the rear end of the temperature-rising side air passage is connected with the air inlet of the rotary flue gas heat exchanger; the outlet of the rotary flue gas heat exchanger loop is connected with a denitration assembly through a flue; the side wall of the flue is sequentially provided with a coal gas heat supplementing device and an ammonia water charging port; the outlet of the rotary flue gas heat exchanger is connected with a chimney through a denitration induced draft fan;
the heat circulation assembly comprises a heat circulation fan, wherein an inlet of the heat circulation fan is connected with an outlet of a return circuit of the rotary flue gas heat exchanger through a pipeline, and the heat circulation fan is specifically positioned between the outlet of the return circuit of the rotary flue gas heat exchanger and the coal gas heat supplementing device; the outlet of the medium type smoke heat exchanger is connected with a pipeline between the temperature rising side of the medium type smoke heat exchanger and the inlet of the rotary type smoke heat exchanger through a pipeline;
the denitration assembly is a denitration reactor SCR; and the SCR outlet is connected with the inlet of the rotary flue gas heat exchanger loop.
The spraying layer is three layers, wherein one layer is arranged above the pneumatic desulfurization unit, and the two layers are arranged below the pneumatic desulfurization unit.
And a main exhaust fan is arranged between the cooling side of the medium type flue gas heat exchanger and the smoke outlet of the sintering machine.
And a flue demister is arranged between the flue gas condenser and the temperature rising side of the medium type flue gas heat exchanger.
The coal gas heat supplementing device is a hot blast stove.
Compared with the prior art, the utility model discloses following outstanding beneficial effect has:
1. the device avoids the wet desulphurization outlet flue gas from taking away more water, so that the tail of the flue gas at the discharge outlet is too long, and the chimney above zero has no visible smoke plume;
2. after the temperature is reduced by adopting flue gas condensation at 7 ℃, 210 ten thousand meters3The water of the smoke per hour can be saved by about 40-50t/h for recycling;
3. after heat exchange of a medium type flue gas heat exchanger (MGGH), the desulfurized saturated wet flue gas is changed into unsaturated flue gas to enter GGH after being heated to 25 ℃ through heat exchange, so that the heat exchange effect is improved, and the blockage probability of the GGH is reduced; meanwhile, the exhaust temperature is relatively increased by 25 ℃, and the emission of white smoke plume can be reduced;
4. the hot air circulation can heat the SCR catalyst in advance, the ammonia spraying condition is achieved in advance, the NOx standard exceeding emission is avoided, the standard reaching emission is realized, and the system operation is more stable.
Drawings
Fig. 1 is a schematic view of the connection relationship of the present invention.
Detailed Description
The invention is further described with reference to the drawings and the detailed description. For convenience of description, the flue gas inlet direction in fig. 1 is set as front, and the flue gas outlet direction is set as rear.
As shown in fig. 1, the utility model discloses a desulfurization assembly, dust removal condensation assembly, flue gas heat transfer assembly, thermal cycle assembly and denitration assembly.
The desulfurization assembly comprises a tube bundle demister 11, a spraying layer 12 and a pneumatic desulfurization unit 13 which are sequentially arranged in a shell.
The side wall of the lower part of the shell is provided with an air inlet, and the top of the shell is provided with an air outlet.
The spraying layer 12 is connected with a liquid inlet, and a liquid outlet is arranged at the bottom of the shell. The liquid outlet and the liquid inlet are connected through a slurry condenser 14. The specific spray layer 12 is three layers, wherein one layer is arranged above the pneumatic desulfurization unit 13, and the other two layers are arranged below the pneumatic desulfurization unit 13.
The pneumatic desulfurization unit 13 be a plurality of, the dot matrix is arranged, specifically adopt the 316L material, 198 pneumatic desulfurization units 13 are totally counted to single tower, single pneumatic desulfurization unit 13 diameter 600mm, height 1 m. The bottom of the pneumatic desulfurization unit 13 is provided with a cyclone. Flue gas enters from the lower part of the pneumatic desulfurization unit 13, upward rotating airflow with a certain speed (less than 9.8m/s) is formed under the action of a cyclone, calcium sulfate and calcium sulfite slurry injected from the upper end of the pneumatic desulfurization unit 13 is supported, rotary cutting is repeatedly carried out, a section of dynamically stable liquid particle suspension layer is formed, the gathering and scattering combination of liquid phase occurs at any time, gas phase is subjected to mass transfer to liquid phase, and the purposes of harmful gas absorption and dust collection are achieved. The pneumatic desulfurization unit 13 is a common wet desulfurization device, and the internal structure thereof will not be described again.
The tube bundle demister 11 is positioned above the spraying layer 12 and comprises a cyclone cylinder and a cyclone plate. The pneumatic desulfurization unit 13 provides rotary airflow power, so that desulfurized smoke enters and rotates in the cyclone cylinder to form violent rotation and disturbance of gas-liquid phases, so that fine liquid drops, fine dust particles, aerosol and other fine particles in the smoke collide with each other and are agglomerated into large liquid drops, centrifugal motion is generated under the action of the cyclone plate, and the large liquid drops are captured and absorbed by a liquid film on the wall of the cyclone cylinder, so that efficient demisting and dedusting are realized, and the ultralow emission requirement that the smoke at the outlet is less than 10mg/Nm3 can be met.
The dedusting condensation assembly comprises a wet type dust collector 21 and a flue gas condenser 22 which are connected in sequence.
The inlet of the wet dust collector 21 is connected with the gas outlet of the desulfurization assembly, so that 2-3mg/Nm of particulate matters in the desulfurized flue gas can be reduced3。
The water path of the flue gas condenser 22 is connected with a cooling tower 23. The flue gas condenser 22 can cool the desulfurized flue gas by 7 ℃, thereby reducing the moisture in the flue gas.
After the treatment of the dust removal condensation assembly, the concentration of particulate matters in the flue gas before entering the SCR is reduced again, and the risk of GGH and SCR blockage is reduced; the water condensed from the flue gas is recycled, so that the cost is saved; can realize no visible smoke plume above the environment temperature of 0 ℃.
The flue gas heat exchange assembly comprises a medium type flue gas heat exchanger MGGH and a rotary type flue gas heat exchanger GGH.
The MGGH comprises a cooling side 31 and a heating side 32 which are connected by a water way, the front end of an air passage of the cooling side 31 is connected with a smoke outlet of the sintering machine, and the rear end of the air passage of the cooling side is connected with an air inlet of the desulfurization assembly; the front end of the air passage of the heating side 32 is connected with the outlet of the flue gas condenser 22, and the rear end of the air passage of the heating side is connected with the air inlet of the GGH cold end 33. MGGH exchanges heat of the flue gas before desulfurization to the GGH inlet, the desulfurized wet saturated flue gas is heated to 20-25 ℃ to become unsaturated wet flue gas, the risk of GGH blockage is reduced, the temperature of the flue gas at the inlet of the desulfurization assembly is reduced by 20-25 ℃, the evaporation capacity in the desulfurization assembly is reduced, water is saved, and excessive wet flue gas is prevented from entering the SCR denitration system. In the optimization scheme, a main exhaust fan is arranged between the MGGH cooling side 31 and the smoke outlet of the sintering machine. In the optimized scheme, a flue demister 24 is arranged between the flue gas condenser 22 and the MGGH temperature rising side 32.
And the outlet of the GGH loop is connected with a denitration assembly 5 through a flue. And a coal gas heat supplementing device 35 and an ammonia water charging port 36 are sequentially arranged on the side wall of the flue. The coal gas concurrent heating device can be a hot blast stove.
And the outlet of the hot end 34 of the GGH is connected with a chimney 38 through a denitration induced draft fan 37.
The thermal circulation assembly comprises a thermal circulation fan 41, wherein the inlet of the thermal circulation fan is connected with the outlet of the GGH loop through a pipeline, and the thermal circulation fan is specifically positioned between the outlet of the GGH loop and the gas concurrent heating device. The outlet of the MGGH is connected with a pipeline between the MGGH warming side 32 and the inlet of the GGH cold end 33 through a pipeline. Realizing the unidirectional flow of hot air from the outlet of the GGH loop → the inlet of the GGH. When the sintering is just started or the flue gas volume is less than 1/3 of the rated flue gas volume and the flue gas temperature after desulfurization is less than 55 ℃, hot air circulation is started, the temperature of the SCR catalyst can be raised in advance, the ammonia spraying condition is achieved in advance, and the excessive emission of NOx is avoided.
The denitration assembly 5 is a denitration reactor SCR. And the SCR outlet is connected with the inlet of the GGH loop. The SCR is a prior art, and its internal structure is not described in detail because it is not improved. The SCR denitration adopts the concept of 'medium temperature design and wide temperature operation', namely a denitration body and equipment are designed according to 280 ℃, and the denitration operation is designed according to the design idea of operation in a temperature range of 200-280 ℃. In the optimization scheme, the operation is carried out at 200 ℃. The detection result shows that the inlet flue gas amount is 718569.80Nm when the denitration is carried out at the temperature of 280 DEG C3H, blast furnace gas calorific value 3858.01KJ/Nm314334.59Nm blast furnace gas consumption3H, converted to 1Nm3The energy consumption of blast furnace gas of the original flue gas (per standard cubic meter) is 76.96KJ/Nm3And the inlet flue gas amount is 718477.63Nm when the denitration operation is carried out at 200 DEG C3H, blast furnace gas calorific value 3904.56KJ/Nm3The blast furnace gas consumption is 8734.58Nm3H, converted to 1Nm3Energy consumption of blast furnace gas of original flue gas (per standard cubic meter) is 47.47KJ/Nm3The denitration system runs at 200 ℃, and the energy consumption of the fuel gas is saved by 38.32% compared with the denitration system running at 280 ℃.
The using method of the device comprises the following steps:
1. flue gas from a sintering machine with the initial temperature of 130 +/-5 ℃ exchanges heat through a cooling side 31 of a medium type flue gas heat exchanger (MGGH), and enters a desulfurization assembly after being cooled to 20-25 ℃;
2. and a wet desulphurization device is adopted in the desulphurization assembly for desulphurization. The method specifically comprises the following steps: flue gas enters from the lower part of the pneumatic desulfurization unit 13, upward rotating airflow with a certain speed (less than 9.8m/s) is formed under the action of a cyclone, calcium sulfate and calcium sulfite slurry injected from the upper end of the pneumatic desulfurization unit 13 is supported, rotary cutting is repeatedly carried out, a section of dynamically stable liquid particle suspension layer is formed, the gathering and scattering combination of liquid phase occurs at any time, gas phase is subjected to mass transfer to liquid phase, and the purposes of harmful gas absorption and dust collection are achieved. In an optimized scheme, the slurry in the slurry condenser is subjected to condensation circulation through a slurry condenser 14.
3. Desulfurized gasThe body enters a demister for gas-water separation. The defroster is tube bank defroster 11, and gas-water separation specifically does: the pneumatic desulfurization unit 13 provides rotary airflow power to enable desulfurized smoke to enter and rotate in the cyclone cylinder to form violent rotation and disturbance of gas-liquid phases, so that fine liquid drops, fine dust particles, aerosol and other fine particles in the smoke collide with each other and are agglomerated into large liquid drops, centrifugal motion is generated under the action of the cyclone plate, and the large liquid drops are captured and absorbed by a liquid film on the wall of the cyclone cylinder, so that efficient demisting and dedusting are realized, and the condition that the smoke at the outlet is less than 10mg/Nm can be met3Ultra-low emission requirements. The temperature of the demisted flue gas is 50 +/-1 ℃, and the moisture content is 12-12.5%.
4. The demisted flue gas enters a wet dust collector 21, and the operation can reduce the particle content in the desulfurized flue gas by 2-3mg/Nm3. The temperature of the flue gas after dust removal is 50 +/-1 ℃, and the moisture content is 12-12.5%. The wet scrubber 21 is independent of the desulfurization assembly and can achieve dust removal without changing temperature and without increasing flue gas moisture content.
5. The temperature of the dedusted flue gas is reduced by 7-8 ℃ through the flue gas condenser 22, the temperature of the condensed flue gas is 43 +/-1 ℃, and the moisture content is 8.4-8.8%. The method avoids the phenomenon that the flue gas at the outlet of the wet desulphurization takes away more water, causes the over-long trailing of the flue gas at the discharge outlet, and realizes that the chimney above zero has no visible smoke plume;
6. the condensed flue gas enters an MGGH temperature rise side 32 for heat exchange, the temperature rises by 20-25 ℃, the condensed flue gas enters a GGH cold end 33 and exchanges heat with denitration flue gas at a hot end 34 after rotation, and the temperature rises to 190 +/-10 ℃; the moisture content is 12-12.5%, and under the condition that the moisture content is not changed, saturated smoke is converted into unsaturated smoke.
7. The smoke at the cold end 33 of the GGH enters a flue through a loop outlet, is heated to 220 +/-10 ℃ through a heat supplementing device, and is mixed with added ammonia gas to form ammonia-containing smoke;
8. the ammonia-containing flue gas enters a denitration assembly 5, and denitration is completed under the active catalytic action of a wide-temperature catalyst in the denitration assembly 5, so that denitration flue gas is obtained;
9. returning the denitrated flue gas to the GGH hot end 34, exchanging heat with the flue gas at the cold end 33, and cooling to 100 +/-10 ℃; the moisture content is 12-12.5%.
10. And the cooled denitration flue gas is discharged from a chimney through a denitration induced draft fan.
11. When the smoke at the cold end 33 of the GGH is discharged from the outlet of the GGH loop and is not heated, the smoke is introduced into a pipeline between the MGGH heating side 32 and the inlet of the GGH through a thermal circulation assembly. When the sintering is just started or the flue gas volume is less than 1/3 of the rated flue gas volume and the flue gas temperature after desulfurization is less than 55 ℃, the thermal cycle is started, the temperature of the SCR catalyst can be raised in advance, the ammonia spraying condition is achieved in advance, the NOx standard exceeding emission is avoided, the standard reaching emission is realized, and the system operation is more stable.
The device can be used for better removing sulfur and dust; the cooled unsaturated flue gas enters GGH, so that blockage is not easy to occur; and the risk of excessive NOx emission is avoided when the sintering is just started or the load is small.
It should be noted that while the invention has been described in detail with respect to specific embodiments thereof, it will be apparent to those skilled in the art that various obvious changes can be made therein without departing from the spirit and scope of the invention.
Claims (5)
1. The utility model provides a sintering flue gas desulfurization denitrification facility which characterized in that: the system comprises a desulfurization assembly, a dust removal condensation assembly, a flue gas heat exchange assembly, a thermal cycle assembly and a denitration assembly; the desulfurization assembly comprises a tube bundle demister, a spraying layer and a pneumatic desulfurization unit which are sequentially arranged in a shell; the side wall of the lower part of the shell is provided with an air inlet, and the top of the shell is provided with an air outlet; the spraying layer is connected with the liquid inlet, and a liquid outlet is formed in the bottom of the shell; the liquid outlet and the liquid inlet are connected through a slurry condenser; the pneumatic desulfurization units are arranged in a dot matrix manner; the bottom of the pneumatic desulfurization unit is provided with a cyclone; the tube bundle demister comprises a cyclone cylinder and a cyclone plate; the dust removal condensation assembly comprises a wet dust remover and a flue gas condenser which are sequentially connected; the inlet of the wet dust collector is connected with the gas outlet of the desulfurization assembly, and the water path of the flue gas condenser is connected with the cooling tower; the flue gas heat exchange assembly comprises a medium type flue gas heat exchanger and a rotary type flue gas heat exchanger; the medium type flue gas heat exchanger comprises a cooling side and a heating side which are connected by a water path, the front end of an air passage of the cooling side is connected with a smoke outlet of the sintering machine, and the rear end of the air passage of the cooling side is connected with an air inlet of the desulfurization assembly; the front end of the temperature-rising side air passage is connected with the outlet of the flue gas condenser, and the rear end of the temperature-rising side air passage is connected with the air inlet of the rotary flue gas heat exchanger; the outlet of the rotary flue gas heat exchanger loop is connected with a denitration assembly through a flue; the side wall of the flue is sequentially provided with a coal gas heat supplementing device and an ammonia water charging port; the outlet of the rotary flue gas heat exchanger is connected with a chimney through a denitration induced draft fan; the heat circulation assembly comprises a heat circulation fan, wherein an inlet of the heat circulation fan is connected with an outlet of a return circuit of the rotary flue gas heat exchanger through a pipeline, and the heat circulation fan is specifically positioned between the outlet of the return circuit of the rotary flue gas heat exchanger and the coal gas heat supplementing device; the outlet of the medium type smoke heat exchanger is connected with a pipeline between the temperature rising side of the medium type smoke heat exchanger and the inlet of the rotary type smoke heat exchanger through a pipeline; the denitration assembly is a denitration reactor SCR; and the SCR outlet is connected with the inlet of the rotary flue gas heat exchanger loop.
2. The desulfurization and denitrification device for sintering flue gas as claimed in claim 1, wherein: the spraying layer is three layers, wherein one layer is arranged above the pneumatic desulfurization unit, and the other two layers are arranged below the pneumatic desulfurization unit.
3. The desulfurization and denitrification device for sintering flue gas as claimed in claim 1, wherein: and a main exhaust fan is arranged between the cooling side of the medium type flue gas heat exchanger and the smoke outlet of the sintering machine.
4. The desulfurization and denitrification device for sintering flue gas as claimed in claim 1, wherein: and a flue demister is arranged between the flue gas condenser and the temperature rising side of the medium type flue gas heat exchanger.
5. The desulfurization and denitrification device for sintering flue gas as claimed in claim 1, wherein: the coal gas heat supplementing device is a hot blast stove.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022207416.4U CN213528065U (en) | 2020-09-30 | 2020-09-30 | Sintering flue gas desulfurization and denitrification device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022207416.4U CN213528065U (en) | 2020-09-30 | 2020-09-30 | Sintering flue gas desulfurization and denitrification device |
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| CN213528065U true CN213528065U (en) | 2021-06-25 |
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| CN202022207416.4U Expired - Fee Related CN213528065U (en) | 2020-09-30 | 2020-09-30 | Sintering flue gas desulfurization and denitrification device |
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Granted publication date: 20210625 |