CN106139850B - Energy-efficient gas-liquid coupling oxidation SOx/NOx control device - Google Patents
Energy-efficient gas-liquid coupling oxidation SOx/NOx control device Download PDFInfo
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- CN106139850B CN106139850B CN201610731455.XA CN201610731455A CN106139850B CN 106139850 B CN106139850 B CN 106139850B CN 201610731455 A CN201610731455 A CN 201610731455A CN 106139850 B CN106139850 B CN 106139850B
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- 230000003647 oxidation Effects 0.000 title claims abstract description 87
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 87
- 239000007788 liquid Substances 0.000 title claims abstract description 63
- 230000008878 coupling Effects 0.000 title claims abstract description 18
- 238000010168 coupling process Methods 0.000 title claims abstract description 18
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 18
- 238000010521 absorption reaction Methods 0.000 claims abstract description 140
- 239000003546 flue gas Substances 0.000 claims abstract description 62
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 59
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 29
- 230000023556 desulfurization Effects 0.000 claims abstract description 29
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 17
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000005406 washing Methods 0.000 claims abstract description 9
- 239000007921 spray Substances 0.000 claims description 21
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 13
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 13
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 13
- 239000006096 absorbing agent Substances 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 8
- 238000002425 crystallisation Methods 0.000 claims description 6
- 230000008025 crystallization Effects 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 239000007789 gas Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000005507 spraying Methods 0.000 abstract description 8
- 238000001179 sorption measurement Methods 0.000 abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 27
- 229910021529 ammonia Inorganic materials 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 230000001590 oxidative effect Effects 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 239000007787 solid Substances 0.000 description 8
- 239000000443 aerosol Substances 0.000 description 5
- 239000007800 oxidant agent Substances 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 150000002826 nitrites Chemical class 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical class [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- 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
- B01D53/75—Multi-step processes
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- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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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
- 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
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- Environmental & Geological Engineering (AREA)
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- Biomedical Technology (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a high-efficiency energy-saving gas-liquid coupling oxidation desulfurization and denitrification device, which comprises an absorption tower, wherein the lower part of the absorption tower is provided with a flue gas inlet, the absorption tower is internally provided with a demisting section, an absorption section, an oxidation section and a concentration section which are arranged from top to bottom, the demisting section comprises a first-stage demister arranged at the upper part of the absorption tower, a washing layer is arranged below the first-stage demister, the absorption section comprises an absorption layer positioned below the washing layer, the concentration section comprises a concentration spraying layer arranged above the flue gas inlet and a concentration tank positioned at the bottom of the absorption tower, the oxidation section comprises an oxidation tank which is internally communicated with ozone, the oxidation tank is arranged between the absorption layer and the concentration spraying layer and is connected with the concentration spraying layer, a hydrogen peroxide solution inlet pipe is arranged above the oxidation tank on the oxidation section of the desulfurization tower, the demisting section comprises an absorption tank communicated with the top of the absorption tower, the absorption, a second-stage demister is arranged in the flue gas outlet. The invention has the advantages of improving the adsorption efficiency and saving energy.
Description
Technical Field
The invention relates to an ammonia desulfurization and denitrification device for coal-fired flue gas, in particular to a high-efficiency and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device, and belongs to the technical field of environmental protection for controlling the emission of coal-fired pollutants.
Background
SO generated in coal-fired flue gas2、NOxThe pollutants such as SO have great harm to the atmospheric environment, ecology and human health, and the requirement of environmental protection is stricter and stricter2And NOxAnd the control of emission reduction is also gradually strengthened.
There are many processes for flue gas desulfurization, wet processesThe desulfurization process is the most applied desulfurization method at present, while ammonia desulfurization is one of wet desulfurization processes, and the device uses ammonia or ammonium sulfite and the like as an absorbent to absorb SO in flue gas2And the method is widely applied to wet desulphurization processes at home and abroad. It features high desulfurizing rate, stable operation, high use value of desulfurizing by-product ammonium sulfate, and no waste water or dregs.
However, ammonia desulfurization also has some problems at present: the circulating liquid contains the para-SO2The ammonium sulfite has absorption effect and also contains a large amount of ammonium sulfate components, so that a large amount of energy consumption and waste of power of the circulating liquid pump are caused; the consumption of the ammonia absorbent is large and the problem of ammonia escape exists; the smoke at the outlet is easy to carry small liquid drops and aerosol, and is difficult to completely remove; the quality of the byproduct ammonium sulfate is not high, and the investment and the operation cost of the total equipment are high. Therefore, the structure of the ammonia desulfurization and denitrification device still has a larger improvement space, and the efficient, stable and low-cost wet desulfurization and denitrification device is researched and developed, so that the ammonia desulfurization and denitrification device has strong practical significance and popularization value.
Disclosure of Invention
The invention aims to provide an efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device which improves adsorption efficiency and reduces energy loss, thereby achieving the purpose of high efficiency and energy saving.
The invention adopts the following technical scheme: an efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device comprises an absorption tower, wherein a flue gas inlet is formed in the lower part of the absorption tower, a demisting section and an absorption section below the demisting section are arranged in the absorption tower, the demisting section comprises a first-stage demister arranged on the upper part of the absorption tower, a washing layer is arranged below the first-stage demister, the absorption section comprises an absorption layer below the washing layer, the bottommost part of the absorption tower is a concentration section, an oxidation section is arranged between the concentration section and the absorption section, the concentration section comprises a concentration spraying layer arranged above the flue gas inlet and a concentration tank arranged at the bottom of the absorption tower, the oxidation section comprises an oxidation tank internally communicated with ozone, the oxidation tank is arranged between the absorption layer and the concentration spraying layer and is connected with the concentration spraying layer, a hydrogen peroxide solution inlet pipe is arranged above the oxidation tank on the oxidation section of the desulfurization tower, the demisting section comprises an, the absorption tank is arranged on one side of the absorption tower, a flue gas outlet is arranged on the absorption tank, and a secondary demister is arranged in the flue gas outlet.
The absorption tank is of a V-shaped structure, one end of the absorption tank of the V-shaped structure is communicated with the top of the absorption tower, the flue gas outlet is formed in the other end of the absorption tank of the V-shaped structure, and the V-shaped angle of the absorption tank of the V-shaped structure is 40 degrees ~ 90 degrees.
The oxidation pond is connected with an ozone generator positioned outside the absorption tower.
An oxidation distribution pipe is arranged in the oxidation pond.
An oxidation liquid collecting disc is arranged above the oxidation pond.
An absorption liquid collecting disc is arranged between the first-stage absorber and the second-stage absorber, and a gas channel is formed in the absorption liquid collecting disc.
The absorption tower is equipped with the ammonium sulfate crystallization system outward, the ammonium sulfate crystallization system include with the circulation tank that the absorption section is connected and with the cyclone that the concentration section is connected has connected gradually centrifuge and desicator on the cyclone, be connected with the centrifugate recovery pipeline who lets in the circulation tank on the centrifuge, the heat transfer structure has on the desicator.
An ammonia water replenishing pipe is arranged on the circulating tank
And a cooling sprayer is arranged at the flue gas inlet and connected with the concentration tank.
When the invention is in operation, the temperature of the flue gas with the temperature of about 200 ℃ is controlled at 70 ℃ ~ 80 ℃ after the temperature of the flue gas is reduced by the temperature reducing sprayer from the flue gas inlet, the flue gas rises to enter the oxidation section and the absorption section, the flue gas is reacted with absorption liquid in the absorption layer and then returns to the circulating tank through the absorption liquid collecting disc to form circulation, and SO in the flue gas is absorbed by the absorption liquid collecting disc and is then circulated2And NOxReacting with ammonia water through a secondary absorption layer, a liquid collecting disc and a primary absorption layer respectively, absorbing, and then demisting in a demisting section, wherein the flow rate of flue gas in the absorption section is controlled to be 2.5 ~ 4m/s, the optimal flow rate is 3 ~ 3.5.5 m/s, the temperature of the flue gas after reaction with absorption liquid is controlled to be 50 ~ 60 ℃, the flue gas after reaction passes through the primary demister in sequence, and the flue gas is absorbed through a V-shaped structureThe V-shaped process water tank is arranged at the joint of the first-stage demister and the second-stage demister, the V-shaped angle of 40 degrees ~ 90 degrees is set according to the smoke volume, the contact area of the smoke and the water surface can be increased, the ammonia escape can be reduced through the absorption effect, and liquid drops and aerosol in the smoke can be removed more effectively through the inertia effect.
In the oxidation section, ozone is generated through an ozone generator, the oxidation distribution pipe sends the ozone to an oxidation pond, residual NO in flue gas is oxidized into high-valence nitrogen oxide with higher solubility by using the strong oxidizing property of the ozone, and meanwhile, the ozone and hydrogen peroxide solution are combined and cooperated to be used as a strong oxidizing agent, so that more hydroxyl free radicals with strong oxidizing property can be generated, sulfite and nitrite are oxidized quickly and efficiently, and the problem that the energy consumption of a traditional pump is large is solved. The novel in-tower oxidation mode is adopted, and the oxidation section is arranged at the upper part of the concentration section, so that the configuration has the advantages that compared with the traditional in-tower oxidation mode, circulating liquid does not need to be extracted from the bottom of the desulfurization tower, the circulating absorption liquid amount can be effectively reduced, and the absorption utilization rate of the oxidant is enhanced; compared with the traditional external oxidation of the tower, the method saves space, does not need to establish an additional oxidation device, simplifies the system and reduces the equipment investment.
The oxidation overflow liquid is concentrated after passing through a concentration spraying layer, the bottom concentrated liquid enters a cooling sprayer through a concentration circulating pump, the temperature is raised by utilizing the heat of flue gas, evaporation is accelerated, crystallization is carried out, concentrated liquid with the solid content of 10 ~ 15% is obtained, then concentrated liquid with the solid content of 40% ~ 50% is obtained through a vortex concentrator, the solid content of 95 ~ 97% is obtained after passing through a centrifugal drier, and finally the byproduct ammonium sulfate with the solid content of more than 99% is obtained through a drier.
The invention has the advantages that 1) the integrated operation of the whole process is matched, demisting cleaning, absorption reaction, absorption liquid oxidation and absorption liquid concentration are carried out in the absorption tower, 2) two stages of absorption layers are arranged, so that the absorption liquid is only partially oxidized, and the absorption efficiency is improved, 3) a novel in-tower oxidation mode is adopted, and the oxidation section is arranged at the upper part of the concentration section, so that compared with the traditional in-tower oxidation, the invention has the advantages that the circulating liquid is not required to be extracted from the bottom of the desulfurization tower, the circulating absorption liquid amount can be effectively reduced, and the absorption utilization rate of the oxidant is enhanced, meanwhile, compared with the traditional outside-tower oxidation, a space is saved, an additional oxidation device is not required, the system is simplified, and the equipment investment is reduced, 4) a V-shaped structure absorption groove is arranged at the connection part of a first-stage demister and a second-stage demister, a V-shaped angle of 40 degrees ~ 90 degrees is arranged according to the flue gas amount, the contact area of the flue gas and the water surface is increased, the ammonia escape can be reduced through the absorption effect, the liquid drops and aerosol in the flue gas and liquid in the oxidation area are effectively removed through the inertia effect, the gas-liquid coupling oxidation of the traditional ozone and hydrogen peroxide solution is utilized, the nitrite is really.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of the efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification apparatus according to the invention.
In the figure, 1, a chimney; 2, a flue gas outlet; 3, a second-stage demister; 4 an absorption tank; 5 an absorption tower; 6, a first-stage demister; 7, washing a layer with water; 8 first-order absorption layers; 9 an absorption drip pan; 10 a secondary absorption layer; 11 oxidizing the liquid collecting disc; 12 oxidizing the distribution pipe; 13 an ozone generator; 14 a flue gas inlet; 15 cooling sprayer; 16 a concentration circulating pump; 17, an oxidation pond; 18 concentrating the spray layer; 19 a concentration tank; 20 an absorption circulation pump; 21 a circulation tank; 22 ammonium sulfate pump; 23 a vortex concentrator; 24, a centrifuge; 25, a dryer; 26 introducing a hydrogen peroxide solution into the tube; 27 ammonia make-up pipe.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
The structure of an embodiment of the efficient energy-saving gas-liquid coupling oxidation desulfurization and denitration device is shown in fig. 1, the gas-liquid coupling oxidation desulfurization and denitration device comprises an absorption tower 5, a flue gas inlet 14 is arranged at the lower part of the absorption tower 5, a cooling spray device 15 is arranged at the flue gas inlet 14, a demisting section and an absorption section positioned below the demisting section are arranged in the absorption tower 5, the demisting section comprises a primary demister 6 arranged at the upper part of the absorption tower, a water washing layer 7 is arranged below the primary demister 6, the absorption section comprises an absorption layer positioned below the water washing layer, the absorption layer comprises a primary absorber 8 and a secondary absorber 10 positioned below the primary absorber 8, an absorption liquid collecting disc 9 is arranged between the primary absorber 8 and the secondary absorber 10, a gas passage is arranged on the absorption liquid collecting disc 9, the bottommost part of the absorption tower is a concentration section, an oxidation section is arranged between the concentration section and the absorption section, the concentration section comprises a concentration spray layer 18 arranged above the flue gas inlet and a concentration pool 19 arranged at the bottom of the absorption tower, the concentration spray layer 18 arranged at the bottom of the absorption tower, the concentration pool 19 is arranged above the absorption tower, a concentration pool 19 is arranged above the oxidation spray pool 18, a concentration spray pool 17 arranged on a pipeline between the oxidation spray tank 15 and the concentration pool 17, a flue gas outlet 354-type ozone spray tank, a flue gas absorption tower is arranged on the absorption tower, a flue gas absorption tower, a 2-type oxidation spray tank, a flue gas oxidation spray tank 2-type absorption tower, a flue gas spray tank is arranged on a flue gas oxidation spray tank 2-type oxidation spray tank 2 absorption tower, a flue gas oxidation spray tank 2 absorption tower top of a flue gas-type oxidation spray tank 2 absorption tower, a flue gas spray tank 2 adsorption structure is arranged between the concentration spray tank 2-type oxidation spray.
The absorption tower 5 is equipped with the ammonium sulfate crystal system outward, the ammonium sulfate crystal system include with the circulation tank 21 that the absorption section is connected and with the cyclone 23 that the concentrated section is connected, be equipped with aqueous ammonia replenishment pipe 27 on the circulation tank, be equipped with absorption circulating pump 20 on the pipeline between oxidation circulation tank 21 and the absorption section, be equipped with ammonium sulfate pump 22 on the pipeline between concentrated pond 19 and the cyclone 23, centrifuge 24 and desicator 25 have connected gradually on the cyclone 23, be connected with the centrifugate recovery pipeline that lets in the circulation tank 21 on the centrifuge 24, heat transfer structure has on the desicator 25.
The temperature of the invention is aboutThe temperature of the flue gas with the temperature of 200 ℃ is controlled at 70 ℃ of ~ 80 ℃ after the temperature of the flue gas is reduced by a cooling sprayer from a flue gas inlet, the flue gas rises to enter an oxidation section and an absorption section, the flue gas is reacted with absorption liquid in an absorption layer and then returns to a circulating tank through an absorption liquid collecting disc to form circulation, and SO in the flue gas is absorbed by the flue gas2And NOxThe flue gas temperature after reaction with the absorption liquid is controlled at 50 ~ ℃, the flue gas after reaction sequentially passes through the first-stage demister, passes through the absorption tank with a V-shaped structure, and then passes through the second-stage demister, enters a chimney through a flue and is discharged, a V-shaped process water tank is arranged at the joint of the first-stage demister and the second-stage demister, a V-shaped angle of 40 degrees ~ degrees is arranged according to the flue gas amount, the contact area of the flue gas and the water surface can be increased, ammonia escape can be reduced through absorption, and liquid drops and aerosol in the flue gas can be more effectively removed through inertia effect.
In the oxidation section, ozone is generated by an ozone generator, the ozone is sent to an oxidation tank by an oxidation distribution pipe, the residual NO in the flue gas is oxidized into high-valence nitrogen oxides with higher solubility by the strong oxidizing property of the ozone, and meanwhile, the high-valence nitrogen oxides are combined with a hydrogen peroxide solution to be used as a strong oxidizing agent in a synergistic manner, so that more hydroxyl radicals with strong oxidizing property can be generated, sulfites and nitrites can be quickly and efficiently oxidized, and the problem of high energy consumption of a traditional utilization pump is solved.
The oxidation overflow liquid is concentrated after passing through a concentration spraying layer, the bottom concentrated liquid enters a cooling sprayer through a concentration circulating pump, the temperature is raised by utilizing the heat of flue gas, evaporation is accelerated, crystallization is carried out, concentrated liquid with the solid content of 10 ~ 15% is obtained, then concentrated liquid with the solid content of 40% ~ 50% is obtained through a vortex concentrator, the solid content of 95 ~ 97% is obtained after passing through a centrifugal drier, and finally the byproduct ammonium sulfate with the solid content of more than 99% is obtained through a drier.
In conclusion, the device has the advantages that 1) the device is matched with the integrated operation of the whole process, demisting cleaning, absorption reaction, absorption liquid oxidation and absorption liquid concentration are carried out in the absorption tower, 2) two stages of absorption layers are arranged, so that the absorption liquid is only partially oxidized, the absorption efficiency is improved, 3) a novel in-tower oxidation mode is adopted, and the oxidation section is arranged at the upper part of the concentration section, so that the device has the advantages that compared with the traditional in-tower oxidation, circulating liquid does not need to be extracted from the bottom of the desulfurization tower, the circulating absorption liquid amount can be effectively reduced, the absorption utilization rate of an oxidant is enhanced, compared with the traditional outside-tower oxidation, a space is saved, an oxidation device is not needed to be additionally established, the system is simplified, the equipment investment is reduced, 4) a V-shaped structure absorption groove is arranged at the connection part of the first-stage demister and the second-stage demister, a V-shaped angle of 40 degrees ~ 90 degrees is arranged according to the flue gas amount, the contact area of the flue gas and water is increased, ammonia escape can be reduced through the absorption effect, liquid drops in the flue gas and aerosol in the flue gas in the oxidation area are effectively removed through the inertia effect, the combination of ozone and hydrogen peroxide solution, the defects of the traditional air oxidation method, the high efficiency of denitrification and the high.
Claims (8)
1. The utility model provides an energy-efficient gas-liquid coupling oxidation SOx/NOx control device, includes absorption tower (5), and absorption tower (5) lower part is equipped with flue gas inlet (14), has the defogging section in absorption tower (5) and is located the absorption section of defogging section below, and the defogging section is including setting up one-level defroster (6) on absorption tower upper portion, and one-level defroster (6) below is equipped with washing layer (7), and the absorption section is including the absorbed layer that is located washing layer (7) below, its characterized in that absorption tower (5) bottommost be concentrated section, is equipped with the oxidation section between concentrated section and the absorption section, and concentrated section is including setting up concentrated spray layer (18) and concentrated pond (19) that are located the absorption tower bottom in flue gas inlet top, the oxidation section is equipped with hydrogen peroxide solution and lets in pipe (26) including inside oxidation distribution pipe (17), be equipped with oxidation distribution pipe (12) in oxidation tank (17), oxidation tank (17) set up between absorbed layer and concentrated spray layer (18) and be connected with concentrated spray layer (18), be equipped with hydrogen peroxide solution lets in oxidation tank (17) top and be equipped with the one end V outlet of absorption tower (4) of absorption tower (5) and the absorption tower (2V-shaped absorption tower outlet (2), absorption tower outlet (5) that the absorption tower (5) top communicates the absorption tower (5V-shaped absorption tower (4), the absorption tower (2V-shaped absorption tower outlet structure (2) that the absorption tower (5) communicates the absorption tower (5) is equipped with the absorption tower top angle is equipped with the absorption tower (2V-shaped absorption tower (4.
2. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 1, characterized in that: the oxidation pond (17) is connected with an ozone generator (13) positioned outside the absorption tower.
3. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 1, characterized in that: an oxidation liquid collecting disc (11) is arranged above the oxidation pond (17).
4. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 1, characterized in that: the absorption layer comprises a primary absorber (8) and a secondary absorber (10) positioned below the primary absorber (8).
5. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 4, characterized in that: an absorption liquid collecting disc (9) is arranged between the primary absorber (8) and the secondary absorber (10), and a gas channel is formed in the absorption liquid collecting disc (9).
6. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 1, characterized in that: the absorption tower is equipped with the ammonium sulfate crystallization system outward, the ammonium sulfate crystallization system include with circulation groove (21) that the absorption section is connected and with cyclone (23) that the concentrated section is connected have connected gradually centrifuge (24) and desicator (25) on cyclone (23), be connected with the centrifugate recovery pipeline that lets in circulation groove (21) on centrifuge (24), heat transfer structure has on desicator (25).
7. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 6, characterized in that: an ammonia water replenishing pipe (27) is arranged on the circulating tank (21).
8. The efficient and energy-saving gas-liquid coupling oxidation desulfurization and denitrification device according to claim 1, characterized in that: the flue gas inlet (14) is provided with a cooling sprayer (15), and the cooling sprayer (15) is connected with the concentration tank (19).
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| CN201610731455.XA CN106139850B (en) | 2016-08-26 | 2016-08-26 | Energy-efficient gas-liquid coupling oxidation SOx/NOx control device |
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| CN201610731455.XA CN106139850B (en) | 2016-08-26 | 2016-08-26 | Energy-efficient gas-liquid coupling oxidation SOx/NOx control device |
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| CN106540532A (en) * | 2017-01-25 | 2017-03-29 | 大连铭晟环保设备有限公司 | Column for smoke purification and flue gas purifying equipment |
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| CN111443170A (en) * | 2020-05-21 | 2020-07-24 | 无锡诺信安全科技有限公司 | System and method for detecting sulfur oxides in air |
| CN112604458B (en) * | 2020-12-30 | 2022-12-06 | 双盾环境科技有限公司 | Process for treating nitrogen oxide-containing tail gas by hydrogen peroxide-ozone coupling |
| CN114288824A (en) * | 2022-01-21 | 2022-04-08 | 中国环境科学研究院 | Absorption tower for removing nitric oxide in daily glass production tail gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995035153A3 (en) * | 1994-06-22 | 1996-03-14 | Fls Miljoe A S | Mass transfer method and apparatus |
| CN102500188A (en) * | 2011-11-23 | 2012-06-20 | 浙江菲达脱硫工程有限公司 | Wet type electric dust-removing device |
| CN103272468A (en) * | 2013-06-13 | 2013-09-04 | 北京中环新锐环保技术有限公司 | Absorption tower for simultaneously removing sulfur dioxide and nitrogen oxide in smoke |
| CN105854547A (en) * | 2016-04-01 | 2016-08-17 | 河北科技大学 | Ammonia oxidizing denitration process and reaction apparatus |
| CN206008418U (en) * | 2016-08-26 | 2017-03-15 | 江苏中圣高科技产业有限公司 | Energy-efficient gas-liquid coupling oxidation sweetening denitrification apparatus |
-
2016
- 2016-08-26 CN CN201610731455.XA patent/CN106139850B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1995035153A3 (en) * | 1994-06-22 | 1996-03-14 | Fls Miljoe A S | Mass transfer method and apparatus |
| CN102500188A (en) * | 2011-11-23 | 2012-06-20 | 浙江菲达脱硫工程有限公司 | Wet type electric dust-removing device |
| CN103272468A (en) * | 2013-06-13 | 2013-09-04 | 北京中环新锐环保技术有限公司 | Absorption tower for simultaneously removing sulfur dioxide and nitrogen oxide in smoke |
| CN105854547A (en) * | 2016-04-01 | 2016-08-17 | 河北科技大学 | Ammonia oxidizing denitration process and reaction apparatus |
| CN206008418U (en) * | 2016-08-26 | 2017-03-15 | 江苏中圣高科技产业有限公司 | Energy-efficient gas-liquid coupling oxidation sweetening denitrification apparatus |
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|---|---|
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