CN112337275A - Sintering flue gas desulfurization and denitrification method and device - Google Patents

Sintering flue gas desulfurization and denitrification method and device Download PDF

Info

Publication number
CN112337275A
CN112337275A CN202011063105.3A CN202011063105A CN112337275A CN 112337275 A CN112337275 A CN 112337275A CN 202011063105 A CN202011063105 A CN 202011063105A CN 112337275 A CN112337275 A CN 112337275A
Authority
CN
China
Prior art keywords
flue gas
desulfurization
temperature
denitration
sintering
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.)
Pending
Application number
CN202011063105.3A
Other languages
Chinese (zh)
Inventor
徐开斌
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Rizhao Steel Holding Group Co Ltd
Original Assignee
Rizhao Steel Holding Group Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rizhao Steel Holding Group Co Ltd filed Critical Rizhao Steel Holding Group Co Ltd
Priority to CN202011063105.3A priority Critical patent/CN112337275A/en
Publication of CN112337275A publication Critical patent/CN112337275A/en
Pending legal-status Critical Current

Links

Images

Classifications

    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/48Sulfur compounds
    • B01D53/50Sulfur oxides
    • B01D53/501Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D47/00Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/02Separating dispersed particles from gases, air or vapours by liquid as separating agent by passing the gas or air or vapour over or through a liquid bath
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/002Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8621Removing nitrogen compounds
    • B01D53/8625Nitrogen oxides
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27FURNACES; KILNS; OVENS; RETORTS
    • F27DDETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28HEAT EXCHANGE IN GENERAL
    • F28DHEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2258/00Sources of waste gases
    • B01D2258/02Other waste gases
    • B01D2258/0283Flue gases
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/25Process efficiency
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10Greenhouse 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 invention discloses a sintering flue gas desulfurization and denitrification device, belongs to the field of steel environmental protection, and relates to a sintering flue gas desulfurization and denitrification method which comprises the following steps: (1) flue gas from the sintering machine enters a desulfurization assembly through heat exchange; (2) wet desulphurization; (3) carrying out gas-water separation on a demister; (4) a wet dust collector; (5) cooling the flue gas condenser; (6) entering a medium type flue gas heat exchanger for heat exchange and temperature rise at a temperature rise side, and entering a cold end of the flue gas heat exchanger for heat exchange and temperature rise; (7) adding ammonia gas for heat supplement; (8) denitration of ammonia-containing flue gas; (9) heat exchange and temperature reduction; (10) and (4) discharging from a chimney. Compared with the prior art, the process can work stably under any condition, and avoids the phenomenon that more moisture is taken away by the flue gas at the outlet of the wet desulphurization, so that the tail of the flue gas at the discharge outlet is too long, and the chimney above zero degree has no visible smoke plume.

Description

Sintering flue gas desulfurization and denitrification method and device
Technical Field
The invention relates to the field of environmental protection, in particular to a wet desulfurization and denitrification method suitable for flue gas treatment in the ferrous metallurgy industry.
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 sintering is just started or the smoke volume is less than 1/3 of the rated smoke 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 conditions of just starting or insufficient smoke, namely the inlet air temperature at the cold end of a smoke 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.
Disclosure of Invention
The technical task of the invention is to provide a sintering flue gas desulfurization and denitrification method and a device thereof aiming at the defects of the prior art, so that the sintering flue gas desulfurization and denitrification method can stably work under any condition.
The technical scheme for solving the technical problem is as follows: the sintering flue gas desulfurization and denitrification method is characterized by comprising the following steps of:
(1) flue gas from the sintering machine is subjected to heat exchange through a cooling side of a medium type flue gas heat exchanger, and is cooled to 20-25 ℃ to enter a desulfurization assembly;
(2) desulfurizing in the desulfurization assembly by a wet desulfurization method;
(3) the desulfurized gas enters a demister for gas-water separation; 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, the temperature of the dedusted flue gas is 50 +/-1 ℃, and the moisture content is 12-12.5%;
(5) the temperature of the dedusted flue gas is reduced by 7-8 ℃ through a flue gas condenser, the temperature of the condensed flue gas is 43 +/-1 ℃, and the moisture content is 8.4-8.8%;
(6) the condensed flue gas enters a medium type flue gas heat exchanger for heat exchange at the temperature rising side, the temperature rises by 20-25 ℃, enters the cold end of the flue gas heat exchanger, exchanges heat with the denitration flue gas at the hot end after rotation, and the temperature rises to 190 +/-10 ℃; the moisture content is 12-12.5%;
(7) the flue gas at the cold end of the flue gas heat exchanger enters a flue through a loop outlet, is heated to 220 +/-10 ℃ through a heat supplementing device, and is mixed with the added ammonia gas to form ammonia-containing flue gas;
(8) the ammonia-containing flue gas enters a denitration assembly, and denitration is completed under the active catalytic action of a wide-temperature catalyst in the denitration assembly to obtain denitration flue gas;
(9) returning the denitrated flue gas to the hot end of the flue gas heat exchanger, exchanging heat with the flue gas at the cold end, 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.
The initial temperature of the flue gas from the sintering machine in the step (1) is 130 +/-5 ℃.
And (3) the flue gas desulfurization in the step (2) is pneumatic desulfurization.
The demister in the step (3) is a tube bundle demister.
In the optimization scheme, the smoke at the cold end of the GGH is discharged from the outlet of the GGH loop and is introduced into the inlet of the GGH through a thermal cycle assembly.
Compared with the prior art, the invention has the following outstanding beneficial effects:
1. the method 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 diagram 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.
The invention provides a sintering flue gas desulfurization and denitrification method, which comprises the following specific steps:
1. flue gas from a sintering machine with the initial temperature of 130 +/-5 ℃ is subjected to heat exchange at the cooling side of a medium type flue gas heat exchanger (MGGH), and is cooled to 20-25 ℃ to enter a desulfurization assembly;
2. and desulfurizing in the desulfurizing assembly by a wet desulfurizing method. The method specifically comprises the following steps: flue gas enters from the lower part of the pneumatic desulfurization unit, 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 is supported and repeatedly rotary-cut to form a section of dynamically stable liquid particle suspension layer, the gathering and scattering combination of liquid phase occurs at any time, and gas phase transfers mass to liquid phase, so that the purposes of harmful gas absorption and dust capture are achieved. In an optimized scheme, the slurry in the slurry condenser is subjected to condensation circulation.
3. And the desulfurized gas enters a demister for gas-water separation. The demister isThe tube bank defroster, the gas-water separation specifically does: the pneumatic desulfurization unit 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 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, 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 dust collector is independent of the desulfurization assembly, can achieve dust removal without changing temperature and increasing the moisture content of the flue gas.
5. The temperature of the dedusted flue gas is reduced by 7-8 ℃ through a flue gas condenser, 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 for heat exchange, the temperature rises by 20-25 ℃, the condensed flue gas enters a GGH cold end and exchanges heat with denitration flue gas at a hot end 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 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, and denitration is completed under the active catalytic action of a wide-temperature catalyst in the denitration assembly to obtain denitration flue gas;
9. returning the denitrated flue gas to the hot end of the GGH, exchanging heat with the flue gas at the cold end, 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. And when the smoke at the cold end of the GGH is discharged from the outlet of the GGH loop and is not subjected to heat compensation, introducing the smoke into a pipeline between the MGGH temperature rise side and the GGH inlet 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, and the excessive emission of NOx is avoided.
The method can better remove 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.
As shown in figure 1, the invention 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 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 7184 is used in denitration operation at 200 DEG C77.63Nm3H, 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 ℃.
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 sintering flue gas desulfurization and denitrification method is characterized by comprising the following steps of:
(1) flue gas from the sintering machine is subjected to heat exchange through a cooling side of a medium type flue gas heat exchanger, and is cooled to 20-25 ℃ to enter a desulfurization assembly;
(2) desulfurizing in the desulfurization assembly by a wet desulfurization method;
(3) the desulfurized gas enters a demister for gas-water separation; 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, the temperature of the dedusted flue gas is 50 +/-1 ℃, and the moisture content is 12-12.5%;
(5) the temperature of the dedusted flue gas is reduced by 7-8 ℃ through a flue gas condenser, the temperature of the condensed flue gas is 43 +/-1 ℃, and the moisture content is 8.4-8.8%;
(6) the condensed flue gas enters a medium type flue gas heat exchanger for heat exchange at the temperature rising side, the temperature rises by 20-25 ℃, enters the cold end of the flue gas heat exchanger, exchanges heat with the denitration flue gas at the hot end after rotation, and the temperature rises to 190 +/-10 ℃; the moisture content is 12-12.5%;
(7) the flue gas at the cold end of the flue gas heat exchanger enters a flue through a loop outlet, is heated to 220 +/-10 ℃ through a heat supplementing device, and is mixed with the added ammonia gas to form ammonia-containing flue gas;
(8) the ammonia-containing flue gas enters a denitration assembly, and denitration is completed under the active catalytic action of a wide-temperature catalyst in the denitration assembly to obtain denitration flue gas;
(9) returning the denitrated flue gas to the hot end of the flue gas heat exchanger, exchanging heat with the flue gas at the cold end, 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.
2. The desulfurization and denitrification method for sintering flue gas as recited in claim 1, wherein: the initial temperature of the flue gas from the sintering machine in the step (1) is 130 +/-5 ℃.
3. The desulfurization and denitrification method for sintering flue gas as recited in claim 1, wherein: and (3) the flue gas desulfurization in the step (2) is pneumatic desulfurization.
4. The desulfurization and denitrification method for sintering flue gas as recited in claim 1, wherein: the demister in the step (3) is a tube bundle demister.
5. The desulfurization and denitrification method for sintering flue gas as recited in claim 1, wherein: the smoke at the cold end of the GGH is discharged from the outlet of the GGH loop and is introduced into the inlet of the GGH through a thermal cycle assembly.
CN202011063105.3A 2020-09-30 2020-09-30 Sintering flue gas desulfurization and denitrification method and device Pending CN112337275A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202011063105.3A CN112337275A (en) 2020-09-30 2020-09-30 Sintering flue gas desulfurization and denitrification method and device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202011063105.3A CN112337275A (en) 2020-09-30 2020-09-30 Sintering flue gas desulfurization and denitrification method and device

Publications (1)

Publication Number Publication Date
CN112337275A true CN112337275A (en) 2021-02-09

Family

ID=74361475

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202011063105.3A Pending CN112337275A (en) 2020-09-30 2020-09-30 Sintering flue gas desulfurization and denitrification method and device

Country Status (1)

Country Link
CN (1) CN112337275A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113144893A (en) * 2021-05-31 2021-07-23 攀钢集团研究院有限公司 Process for reducing fault of ultralow emission treatment system for carrying out wet desulphurization and SCR denitration on low-temperature flue gas

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113144893A (en) * 2021-05-31 2021-07-23 攀钢集团研究院有限公司 Process for reducing fault of ultralow emission treatment system for carrying out wet desulphurization and SCR denitration on low-temperature flue gas

Similar Documents

Publication Publication Date Title
CN105444582B (en) A kind of combined and staged kiln exit gas processing unit and the process of burning of cement kiln bypass
CN108380041A (en) A kind of coke oven flue gas system for desulfuration and denitration and method based on activated carbon/coke
CN202478804U (en) Sintering machine flue gas desulphurization denitration device
CN106996702A (en) A kind of agglomeration for iron mine flue gas segmentation enrichment and UTILIZATION OF VESIDUAL HEAT IN emission reduction SOxAnd NOxMethod
CN106524771A (en) Technical method for denitration of sintering flue gas
CN105080332A (en) Resource utilization system for pellet sintering waste gas and method
CN105698550A (en) Sintering flue gas purification system and method achieving energy conservation and emission reduction
CN107131770A (en) A kind of agglomeration for iron mine waste heat recovery collaboration emission reduction SOXAnd NOXMethod
CN108704463A (en) A kind of sintering flue gas desulfurization denitration, flue gas disappear white total system and technique
WO2023050897A1 (en) Flue gas low-temperature desulfurization and denitrification system for rotary kiln combustion furnace of garbage power plant
WO2023050702A1 (en) Low-temperature desulfurization and denitrification method and system for flue gas from rotary kiln combustion furnace of refuse incineration power plant
CN205448732U (en) Energy saving and emission reduction's sintering gas cleaning system
CN208177248U (en) It is a kind of based on active carbon/coke coke oven flue gas system for desulfuration and denitration
CN204952658U (en) Sintering pelletizing flue gas resource system
CN112337275A (en) Sintering flue gas desulfurization and denitrification method and device
CN114151817A (en) Flue gas treatment system and treatment method
CN109731472A (en) Power economized boiler flue gas purification system and method
CN109647544A (en) A kind of technique of the composite regenerated waste and old copper bismuth catalyst of recycling of wet-dry change
CN107349783B (en) Sintering flue gas denitration process based on sintering flue gas circulation and flue gas catalysis
CN108704464A (en) A kind of sintering flue gas desulfurization denitration, flue gas disappear white total system and technique
CN213528065U (en) Sintering flue gas desulfurization and denitrification device
CN107899413A (en) A kind of exhaust gas of hot-blast stove desulphurization denitration cooperates with administering method
CN209490656U (en) It is a kind of to disappear white device for fire coal tail gas desulphurization denitration dedusting
CN107270713A (en) A kind of ultra-clean discharge sintering system of iron ore thermal coupling and method
CN208583169U (en) A kind of sintering flue gas desulfurization denitration, flue gas disappear white total system

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