CN113019092A - Flue gas desulfurization and denitrification method and system based on dense-phase semi-dry method - Google Patents
Flue gas desulfurization and denitrification method and system based on dense-phase semi-dry method Download PDFInfo
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- CN113019092A CN113019092A CN202110174026.8A CN202110174026A CN113019092A CN 113019092 A CN113019092 A CN 113019092A CN 202110174026 A CN202110174026 A CN 202110174026A CN 113019092 A CN113019092 A CN 113019092A
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- 239000003546 flue gas Substances 0.000 title claims abstract description 93
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 36
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 36
- 238000010521 absorption reaction Methods 0.000 claims abstract description 66
- 230000001590 oxidative Effects 0.000 claims abstract description 35
- 239000007800 oxidant agent Substances 0.000 claims abstract description 32
- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000000428 dust Substances 0.000 claims abstract description 27
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 24
- 230000003647 oxidation Effects 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 7
- 238000007599 discharging Methods 0.000 claims abstract description 3
- 238000005245 sintering Methods 0.000 claims description 42
- 238000000889 atomisation Methods 0.000 claims description 20
- 238000001816 cooling Methods 0.000 claims description 20
- 239000007921 spray Substances 0.000 claims description 18
- 238000002347 injection Methods 0.000 claims description 12
- 239000007924 injection Substances 0.000 claims description 12
- 239000006227 byproduct Substances 0.000 claims description 10
- 238000009827 uniform distribution Methods 0.000 claims description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 4
- 239000002250 absorbent Substances 0.000 abstract description 12
- 230000002745 absorbent Effects 0.000 abstract description 12
- 238000006243 chemical reaction Methods 0.000 abstract description 5
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 4
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- 239000003054 catalyst Substances 0.000 abstract description 2
- 238000005260 corrosion Methods 0.000 abstract description 2
- 230000004048 modification Effects 0.000 abstract description 2
- 238000006011 modification reaction Methods 0.000 abstract description 2
- 229910052813 nitrogen oxide Inorganic materials 0.000 abstract description 2
- 230000000607 poisoning Effects 0.000 abstract description 2
- 231100000572 poisoning Toxicity 0.000 abstract description 2
- 238000003860 storage Methods 0.000 description 11
- 238000005507 spraying Methods 0.000 description 9
- 239000000498 cooling water Substances 0.000 description 8
- 238000002360 preparation method Methods 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000000243 solution Substances 0.000 description 6
- 238000010790 dilution Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000003814 drug Substances 0.000 description 4
- 239000004744 fabric Substances 0.000 description 4
- 239000011550 stock solution Substances 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- RJIWZDNTCBHXAL-UHFFFAOYSA-N Nitroxoline Chemical compound C1=CN=C2C(O)=CC=C([N+]([O-])=O)C2=C1 RJIWZDNTCBHXAL-UHFFFAOYSA-N 0.000 description 2
- 238000011068 load Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011112 process operation Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- UKLNMMHNWFDKNT-UHFFFAOYSA-M Sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229940079593 drugs Drugs 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229960002218 sodium chlorite Drugs 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention discloses a flue gas desulfurization and denitrification method and system based on a dense-phase semi-dry method, wherein the method comprises the following steps: after the flue gas is cooled, primarily oxidizing NO in the flue gas by using an oxidant, and secondarily oxidizing by using ozone; the flue gas after secondary oxidation is subjected to high-valence NO in the flue gas by slaked limeXAnd SO2Carrying out dense-phase and semi-dry absorption, and then carrying out dust removal; the flue gas after dust removal is high-price NOXAnd performing secondary absorption, and discharging. The method generates more high-valence nitrogen oxides through secondary oxidation of the oxidizing agent and the ozone, and is convenient for efficient absorption of the dense-phase semi-dry absorbent; a secondary absorption system after dense-phase semi-dry desulfurization and denitrification to ensure SO2And NOXUltra-low emission of (2); the reaction condition does not need high temperature, the desulfurization and denitrification agents are alkaline, and the equipment is protectedThe corrosion is small; compared with the raw materials of the denitration agent component, the adopted desulfurizer has low price, does not have the problems of catalyst poisoning, blockage, failure and the like, and has lower equipment modification engineering and raw material cost investment.
Description
Technical Field
The invention relates to a flue gas purification method and a flue gas purification system, in particular to a flue gas desulfurization and denitrification method and a flue gas desulfurization and denitrification system based on a dense-phase semi-dry method.
Background
In recent years, with the stricter national environmental protection policy, the emission standard of the flue gas is upgraded for many times, and SO in the sintering flue gas is removed2And NOXAs key treatment objects, steel enterprises increase investment and improve or newly build sintering flue gas desulfurization and denitrification systems so as to achieve the aim that the particulate matters are less than 10mg/Nm3、SO2Less than 35mg/Nm3、NOXLess than 50mg/Nm3Ultra-low emission standards. At present, the mature desulfurization and denitrification technology comprises the following steps: the method comprises an active coke desulfurization and denitrification integrated technology, a semi-dry desulfurization and SCR denitrification technology, a semi-dry and oxidation integrated desulfurization and denitrification technology and the like. Wherein, the integrated desulfurization and denitrification technology of the semi-dry method and the oxidation mainly adopts an absorption tower with higher absorption efficiency, such as a circulating fluidized bed method (CFB), a rotary spray drying method (SDA) and the like; the method has the advantages of low investment, economical operation, simple process operation, good expansibility, difficult hardening of the absorption tower, no limitation of bed pressure loss, strong flue gas impact load resistance and the likeThe dense-phase semi-dry absorption tower with multiple advantages is relatively low in absorption efficiency, and is difficult to achieve ultralow emission by being matched with oxidation integrated denitration, so that the dense-phase semi-dry absorption tower is abandoned by many steel enterprises.
Disclosure of Invention
The invention aims to solve the technical problem of providing a flue gas desulfurization and denitrification method based on a dense-phase semi-dry method, which has high absorption efficiency; the invention also provides a flue gas desulfurization and denitrification system based on the dense-phase semi-dry method.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: the method comprises the following steps: after the flue gas is cooled, primarily oxidizing NO in the flue gas by using an oxidant, and secondarily oxidizing by using ozone; the flue gas after secondary oxidation is subjected to high-valence NO in the flue gas by slaked limeXAnd SO2Carrying out dense-phase and semi-dry absorption, and then carrying out dust removal; the flue gas after dust removal is high-price NOXAnd performing secondary absorption, and discharging.
The flue gas is cooled to 140-150 ℃.
The system is characterized in that a sintering flue gas pipeline is sequentially communicated with a cooling spray device, an oxidant atomization spray device, an ozone uniform distribution spray device, a dense-phase semi-dry absorption device, a transition bin, a bag-type dust collector and an atomization spray absorption device.
The front end of the cooling spray device of the system is also communicated with an electrostatic dust collector.
The dense-phase semi-dry absorption device of the system comprises a dense-phase semi-dry absorption tower, a humidifying device, a raw material bin, a byproduct bin, a bucket lifting device and a scraper machine; the humidifying device is arranged at the top of the dense-phase semi-dry absorption tower; the bucket lifting device, the humidifying device, the dense-phase semi-dry absorption tower, the scraper conveyor, the raw material bin and the byproduct bin form a slaked lime circulation loop. And the desulfurization and denitrification ash collected by the transition bin and the bag-type dust collector is sent into a scraper conveyor.
Adopt the produced beneficial effect of above-mentioned technical scheme to lie in: the invention generates more high-valence nitrogen oxides than single oxidation by secondary oxidation of the oxidizing agent and ozone, and is convenient for efficient absorption of the dense-phase semi-dry absorbent at the rear end; secret keyA secondary absorption system after desulfurization and denitrification by a phase semidry method to ensure SO2And NOXUltra-low emission of (2); the reaction condition does not need high temperature, and the desulfurization and denitrification agents are alkaline and have small corrosion to equipment; compared with the raw materials of the denitration agent component, the adopted desulfurizer has low price, does not have the problems of catalyst poisoning, blockage, failure and the like, and has lower equipment modification engineering and raw material cost investment. The method is based on a dense-phase semi-dry sintering flue gas efficient desulfurization and denitrification system, so that the oxidation and absorption effects are obviously enhanced, higher desulfurization and denitrification efficiency is achieved, and finally ultralow emission of sintering flue gas pollutants is realized.
The system ensures that the flue gas is at the optimal reaction temperature through the cooling and spraying device, effectively reduces the failure of ozone and oxidant, and greatly improves the oxidation efficiency. The system of the invention synchronously completes high-efficiency desulfurization and denitration at low temperature based on a dense-phase semi-dry absorption tower; the method has the advantages of low investment, economical operation, simple process operation, good expansibility, difficult hardening of the absorption tower, small fluctuation along with the flue gas load and the like, and fully exerts the advantages of the dense-phase semi-dry absorption method.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
FIG. 1 is a schematic diagram of the system of the present invention.
In the figure: a sintering machine 1; an electrostatic precipitator 2; a main exhaust fan 3; a cooling spray device 4; an oxidant atomizing and spraying device 5; the ozone is uniformly distributed in the injection device 6; a dense-phase semi-dry absorption device 7; a transition bin 8; a bag-type dust collector 9; a booster fan 10; an atomizing spray absorption device 11; an exhaust stack 12; an oxidizing agent preparation device 13; an oxidant storage device 14; an ozone generation system 15; a dilution air system 16; a humidifying device 17; a raw material bin 18; a byproduct bin 19; a bucket elevator 20; a scraper machine 21; an ash hopper 22; a feeder 23; an absorbent preparation system 24; an absorbent storage device 25; a PLC temperature regulation control system 26; a drug solution pump 27; a regulating cooling water pump 28; and a water pump 29.
Detailed Description
The flue gas desulfurization and denitrification method and system based on the dense-phase semi-dry method are specifically as follows: (1) the sintering flue gas discharge port of the sintering machine 1 is sequentially communicated with an electrostatic dust collector 2, a main exhaust fan 3, a cooling spray device 4, an oxidant atomization injection device 5, an ozone uniform distribution injection device 6, a dense-phase semi-dry absorption tower 7, a transition bin 8, a bag-type dust collector 9, a booster fan 10, a rear end atomization spray absorption device 11 and a discharge chimney 12 through a sintering flue gas pipeline. And the sintering flue gas is discharged after sequentially passing through the equipment under the action of the main exhaust fan 3 and the booster fan 10.
(2) Dust removal: the sintering flue gas is dedusted by the electrostatic precipitator 2, so that the influence of dust in the sintering flue gas on subsequent treatment is avoided.
(3) Cooling: the cooling spray device 4 is arranged at the rear end of the main exhaust fan 3, and the cooling spray device 4 is arranged at a straight pipe section of the sintering flue gas pipeline which is 40-60 m away from the inlet of the dense-phase semi-dry absorption tower 7 to cool the sintering flue gas. The cooling spray device 4 comprises a cooling sprayer, a PLC temperature regulation control system 26 and a regulation cooling water pump 28; the cooling sprayer is arranged on the section of the sintering flue gas pipeline, and the cooling water adopts production fresh water; the adjusting cooling water pump 28 is communicated with a cooling water source and a cooling sprayer to provide cooling water for the cooling sprayer; the PLC temperature regulation control system 26 regulates the frequency of the cooling water pump 28 according to the temperature in the pipeline so as to control the water quantity, so that the temperature of the flue gas is kept at 140-150 ℃ after cooling.
(4) Primary oxidation: the oxidant atomization and injection device 5 comprises an oxidant atomization injector, and the source end of the oxidant atomization injector is communicated with an oxidant preparation device 13 and an oxidant storage device 14; the oxidant ejector is arranged on the section of the sintering flue gas pipeline, and the oxidant adopts sodium chlorite solution; the oxidant storage device 14 stores stock solution, the stock solution in the storage device enters the oxidation preparation device 13 for proportioning, and the mass concentration of the oxidant solution is 8-10%. The prepared oxidant solution is sprayed into a sintering flue gas pipeline through an oxidant atomization spraying device 5 by a liquid medicine pump 27 to carry out primary oxidation on NO in the flue gas; the oxidant atomization injection device 5 is arranged at a straight pipe section which is 30-50 m away from the inlet of the dense-phase semi-dry absorption tower 7 and 5-20 m away from the cooling spray device; the NO oxidation rate in the flue gas after primary oxidation reaches 55-70%.
(5) Secondary oxidation: the ozone uniform distribution injection device 6 comprises an ozone distributor, and the source end of the ozone distributor is communicated with an ozone generation system 15 and a dilution air system 16; the spraying structure of the ozone distributor is arranged on the section of the sintering flue gas pipeline; ozone generated by the ozone generating system 15 is mixed with air sent by the dilution air system 16, and then the mixed air is sprayed into a sintering flue gas pipeline through an ozone distributor, so that the ozone and the sintering flue gas are fully mixed, and the sintering flue gas can be secondarily oxidized by the ozone. After secondary oxidation, the NO oxidation rate in the flue gas reaches more than 90 percent. The ozone uniform distribution injection device is arranged 6 at a pipe section of 10 m-20 m of the inlet of the dense-phase semi-dry absorption tower 7. Wherein, the oxidation reaction in the sintering flue gas pipeline is as follows:
(6) dense-phase semi-dry absorption: the dense-phase semi-dry absorption device comprises a dense-phase semi-dry absorption tower 7, a humidifying device 17, a raw material bin 18, a byproduct bin 19, a bucket lifting device 20 and a scraper 21. The top of the dense-phase semi-dry absorption tower 7 is provided with a humidifying device 17, a raw material bin 18 and a byproduct bin 19 are arranged at the side end, and a bucket lifting device 20 and a scraper 21 are used for recycling the absorbent; the oxidized flue gas enters a dense-phase semi-dry absorption tower 7, and slaked lime in the tower is used for treating high-valence NO in the flue gasXAnd SO2Absorption is carried out, slaked lime in the tower continuously circulates in the absorption tower 7 through a bucket lifting device 20, a scraper 21, a humidifying device 17, a raw material bin 18 and a byproduct bin 19, and high absorption capacity is continuously maintained; after the dense-phase semi-dry tower 7 absorbs the flue gas, the flue gas can reach SO2≤20mg/Nm3，NOX≤80 mg/Nm3. The desulfurization and denitrification reactions in the absorption tower 7 are as follows:
。
(7) recovering desulfurization and denitrification ash: the clothAn ash hopper 22 is arranged at an ash outlet at the lower part of the bag dust collector 9; the lower ash outlet of the transition bin 8 is communicated with the ash bucket 22 through a feeder 23, and the feeder 23 is communicated with the scraper 21. The sintering flue gas can carry desulfurization and denitrification ash after dense-phase and semi-dry absorption; the sintering flue gas is settled by the transition bin 8 and intercepted by the cloth bag of the cloth bag dust remover 9, so that the desulfurization and denitrification ash in the sintering flue gas is removed and collected; the settled and cloth bag intercepted desulfurization and denitrification ash is collected into an ash bucket 22, the ash in the ash bucket 22 is conveyed into a scraper conveyor 21 through a feeder 23, and enters a bucket elevator device 20 through a connecting chute to participate in absorption circulation as a whole; meanwhile, the bag-type dust collector 9 collects the particulate matter and dust, so that the particulate matter in the flue gas is less than or equal to 10mg/m after dust removal3Ultra-low emission requirements.
(8) Secondary absorption: an atomization spraying absorption device 11 is arranged behind the booster fan 10 for high-price NOXAnd carrying out secondary absorption. The atomization spray absorption device 11 comprises an atomization sprayer, and the source end of the atomization sprayer is communicated with an absorbent preparation system 24, an absorbent storage device 25 and a water pump 29; the atomization sprayer is arranged on the section of the sintering flue gas pipeline, and the absorbent adopts sodium hydroxide solution; the absorbent prepared by the absorbent preparation system 24 enters an absorbent storage device 25 for storage, and is sprayed into the sintering flue gas pipeline through a water pump 29, so that secondary absorption can be performed, and the secondary absorption mainly absorbs NO which is not absorbed by the absorption tower 72. The flue gas after the secondary absorption can be discharged into the atmosphere through a discharge chimney 12, and finally SO can be achieved2≤20mg/Nm3，NOX≤50 mg/Nm3。
Example (b): the flue gas desulfurization and denitrification method based on the dense-phase semi-dry method is as follows.
265m of a certain steel mill2The flue gas amount of the flue gas of the sintering machine is 100-110 ten thousand Nm3The smoke temperature is 140-180 ℃ and SO2At 700-1500 mg/Nm3、NOXIn the range of 250 to 400mg/Nm3. The sintering flue gas is introduced into a sintering flue gas pipeline under the action of a main exhaust fan, dust is removed by an electrostatic dust collector, the concentration of particulate matters after dust removal is greatly reduced to 50mg/Nm3The following. After passing through the main exhaust fan, at a certain distanceA cooling spray device is arranged at a straight pipe section of a sintering flue gas pipeline which is 50m away from the dense-phase semi-dry absorption tower, the sintering flue gas is cooled, a PLC temperature adjusting and controlling system is utilized, the frequency of a cooling water pump is adjusted to control the water quantity according to the temperature in the sintering flue gas pipeline, and the flue gas temperature is kept at 140-150 ℃ all the time after cooling. And arranging an oxidant atomization injection device at a straight pipe section of the sintering flue gas pipeline 45m away from the inlet of the dense-phase semi-dry absorption tower to oxidize NO in the sintering flue gas. Then an ozone distributor is arranged at a pipe section 10m of the inlet of the dense-phase semi-dry absorption tower, and the spraying structure of the ozone distributor is arranged on the section of the sintering flue gas pipeline, so that the ozone and the sintering flue gas are fully mixed for secondary oxidation, and part of NO is oxidized2Oxidation to higher valence NOX. At this time, SO2And NO after oxidationXThe wet mixed ash has excellent reaction activity and reacts with sintering flue gas entering from the top of the tower, the reacted materials are sent into a scraper machine through a dense phase absorption tower and an ash bucket at the bottom of the cloth bag dust remover, and then are sent into the humidifier through a bucket lifting system to complete the circulation of an ash system, and a small part of inactive absorbent is discharged into a byproduct bin as a byproduct. And (3) under the action of a booster fan, the sintering flue gas treated by the absorption tower is secondarily absorbed by a rear-end atomization spraying absorption system and finally discharged out of a discharge chimney.
The source end of the oxidant atomization injection device is provided with an oxidant preparation system and an oxidant storage device, the oxidant storage device stores stock solution, and the mass of the stored liquid medicine is 30 t. The stock solution in the storage device enters an oxidation preparation system for proportioning, and the mass concentration of the oxidant liquid medicine is 8-10%. The prepared oxidant solution is sprayed into a sintering flue gas pipeline through an oxidant atomization spraying device, and the spraying amount is along with NO at an inletXThe concentration and the temperature change of the flue gas are adjusted to be 0.8-2 m3/h，
The ozone uniform distribution injection device source end is provided with an ozone generation system and a dilution air system, the ozone generation system is provided with three generators, the output of each generator is 90kg/h, and daily operation is controlled to be 150-200 kg/h according to inlet flue gas actual working conditions. The concentration of ozone generated by the dilution fan is controlled to be adjustable between 6% and 13%, and the ozone can be optimally adjusted according to the production operation condition.
The tower temperature of the dense-phase semi-dry absorption tower is controlled to be 90-110 ℃, and the water quantity of a humidifier is 4.5-5.5 m3The pressure difference of the bag-type dust collector is 1000-1300 Pa, the current of the bucket lifting system is 50-70A, and the flow velocity of flue gas of the whole system is 9-12 m/s.
The oxygen content of the emission chimney is 14.5-16%, and SO2In the range of 3 to 20mg/Nm3， NOXIn the range of 25 to 50mg/Nm3The desulfurization rate can reach more than 99 percent, the denitration rate can reach 95 percent, and the ultralow emission of sintering flue gas is realized.
Claims (6)
1. A flue gas desulfurization and denitrification method based on a dense-phase semi-dry method is characterized by comprising the following steps: after the flue gas is cooled, primarily oxidizing NO in the flue gas by using an oxidant, and secondarily oxidizing by using ozone; the flue gas after secondary oxidation is subjected to high-valence NO in the flue gas by slaked limeXAnd SO2Carrying out dense-phase and semi-dry absorption, and then carrying out dust removal; the flue gas after dust removal is high-price NOXAnd performing secondary absorption, and discharging.
2. The flue gas desulfurization and denitrification method based on the dense-phase semi-dry method as claimed in claim 5, wherein: and cooling the flue gas to 140-150 ℃.
3. The utility model provides a flue gas desulfurization deNOx systems based on dense phase semidry method which characterized in that: a sintering flue gas pipeline is sequentially communicated with a cooling spray device (4), an oxidant atomization injection device (5), an ozone uniform distribution injection device (6), a dense-phase semi-dry absorption device (7), a transition bin (8), a bag-type dust collector (9) and an atomization spray absorption device (11).
4. The flue gas desulfurization and denitrification system based on the dense-phase semi-dry method as claimed in claim 3, wherein: the front end of the cooling spray device (4) is also communicated with an electrostatic dust collector (2).
5. The flue gas desulfurization and denitrification system based on the dense-phase semi-dry method as claimed in claim 3 or 4, wherein: the dense-phase semi-dry absorption device comprises a dense-phase semi-dry absorption tower, a humidifying device (17), a raw material bin (18), a byproduct bin (19), a bucket lifting device (20) and a scraper (21); the humidifying device (17) is arranged at the top of the dense-phase semi-dry absorption tower; the bucket lifting device (20), the humidifying device (17), the dense-phase semi-dry absorption tower, the scraper conveyor (21), the raw material bin (18) and the byproduct bin (19) form a slaked lime circulation loop.
6. The flue gas desulfurization and denitrification system based on the dense-phase semi-dry method as claimed in claim 5, wherein: and the desulfurization and denitrification ash collected by the transition bin (8) and the bag-type dust collector (9) is sent into a scraper conveyor (21).
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| CN103816795A (en) * | 2014-03-17 | 2014-05-28 | 北京承天明德环保科技有限公司 | Semi-dry process desulfurization dust-removing technique and device |
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