CN111905542A - Pre-oxidation and wet catalysis combined desulfurization and denitrification system and method - Google Patents
Pre-oxidation and wet catalysis combined desulfurization and denitrification system and method Download PDFInfo
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 25
- 230000023556 desulfurization Effects 0.000 title claims abstract description 25
- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 16
- 238000010521 absorption reaction Methods 0.000 claims abstract description 72
- 239000003054 catalyst Substances 0.000 claims abstract description 57
- 230000003647 oxidation Effects 0.000 claims abstract description 47
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000003546 flue gas Substances 0.000 claims abstract description 28
- 239000007788 liquid Substances 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims abstract description 12
- 238000005507 spraying Methods 0.000 claims abstract description 10
- 239000002002 slurry Substances 0.000 claims abstract description 7
- SHFJWMWCIHQNCP-UHFFFAOYSA-M hydron;tetrabutylazanium;sulfate Chemical compound OS([O-])(=O)=O.CCCC[N+](CCCC)(CCCC)CCCC SHFJWMWCIHQNCP-UHFFFAOYSA-M 0.000 claims description 24
- STCOOQWBFONSKY-UHFFFAOYSA-N tributyl phosphate Chemical compound CCCCOP(=O)(OCCCC)OCCCC STCOOQWBFONSKY-UHFFFAOYSA-N 0.000 claims description 22
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 20
- 238000002347 injection Methods 0.000 claims description 8
- 239000007924 injection Substances 0.000 claims description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 7
- 230000002195 synergetic effect Effects 0.000 claims description 7
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 238000000889 atomisation Methods 0.000 description 17
- 239000007800 oxidant agent Substances 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 238000007906 compression Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- -1 nitrogen-containing organic compound Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000004056 waste incineration Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- 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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D53/34—Chemical or biological purification of waste gases
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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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8609—Sulfur oxides
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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Abstract
The invention provides a preposed oxidation and wet catalysis combined desulfurization and denitrification system and a method, comprising a preposed oxidation system arranged on a flue, an absorption system arranged at the outlet of the flue, and a catalyst feeding system and a chimney which are respectively connected with the absorption system; the pre-oxidation system comprises H connected in sequence2O2The device comprises a storage tank, an ultrasonic atomizer and a compressed gas tank connected with an inlet of the ultrasonic atomizer; the outlet of the ultrasonic atomizer is connected with the flue;the absorption system comprises an absorption tower; the absorption tower adopts a wet spraying tower, and the bottom of the absorption tower is provided with a slurry tank for containing alkaline absorption liquid; a flue gas inlet of the absorption tower is connected with a flue outlet, and a flue gas outlet is connected with a chimney; the catalyst feeding system comprises a catalyst storage tank and a catalyst delivery pump; the catalyst storage tank is connected with the slurry pool through a catalyst delivery pump, and the catalyst storage tank is filled with a catalyst for realizing SO in alkaline absorption liquid2And NO2A synergistically removed catalyst.
Description
Technical Field
The invention relates to the field of flue gas purification for comprehensive treatment of waste gas in industries such as coal-fired power plants, steel plant sintering machines, industrial boilers, biomass power plants, waste incineration plants and the like, in particular to a system and a method for pre-oxidation combined with wet catalysis combined desulfurization and denitrification.
Background
The ultra-low emission of over 95 percent large coal-fired units in China is realized, but the treatment process route is single, the operation cost is high, the urgent transformation requirements are met, and the integrated removal and resource utilization are the future development direction. Compared with pollutant treatment in the power industry, the pollutant emission distribution in the non-power industry is wide, the smoke amount is small, the smoke working condition is complex, the treatment difficulty is large, and the integrated removal and low-temperature denitration technology has urgent market requirements.
In the existing wet combined desulfurization and denitrification process, O is mostly adopted3As oxidizing agent, in O3In the case of a molar ratio/NO of more than 2.0, the NO is oxidized to N2O5The existing wet desulphurization system is utilized to realize SO2And removing NOx synergistically. In the process, O3High cost of generation (1 kgO per generation)3And the power consumption is 7-8 kWh, O2The consumption is about 10kg, calculated according to the commercial power consumption of 0.7 yuan/kWh and the unit O3The cost is about 10500 yuan/ton), the consumption is large (the mol ratio is generally more than 2.0), and O exists in the process3Escape, nitrate as a product and discharge after treatment, resulting in complex process and high operation cost。
And O3In contrast, H2O2Is a cheap and clean oxidant, and the unit mass cost is only O 31/10 and H2O2Small molecular weight, equal molar ratio, mass of only O 32/3 of (1); oxidation of NO, H at equivalent molar ratios2O2The cost is only O 31/15 and H2O2The oxidation process produces only O2No secondary pollution is generated. Thus, if H can be used in the wet integrated removal process2O2Substituted O3Has important significance for reducing the process cost.
But in H2O2In the oxidation of NO, H2O2Oxidation of NO product to NO2The NO is oxidized in the flue by adopting a compression atomization mode, and the oxidation efficiency of the process is low and is generally less than 60 percent; combined absorption of SO in existing wet desulfurization tower2And NO2In process, NO2The absorption efficiency is only 10-20%, the efficiency is low, and the NOx emission requirement cannot be met.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a preposed oxidation and wet catalysis combined desulfurization and denitrification system and method, which can effectively meet the integrated pollutant removal requirement and realize SO2And NOxThe integrated removal of the catalyst is realized, the desulfurization and denitrification efficiency is high, the process is simple, and the investment and operation cost is low.
The invention is realized by the following technical scheme:
the system comprises a preposed oxidation system arranged on a flue, an absorption system arranged at the outlet of the flue, a catalyst feeding system and a chimney, wherein the catalyst feeding system and the chimney are respectively connected with the absorption system;
the pre-oxidation system comprises H connected in sequence2O2The device comprises a storage tank, an ultrasonic atomizer and a compressed gas tank connected with an inlet of the ultrasonic atomizer; the outlet of the ultrasonic atomizer is connected with the flue;
the absorption system comprises an absorption tower; the absorption tower adopts a wet spraying tower, and the bottom of the absorption tower is provided with a slurry tank for containing alkaline absorption liquid; a flue gas inlet of the absorption tower is connected with a flue outlet, and a flue gas outlet is connected with a chimney;
the catalyst feeding system comprises a catalyst storage tank and a catalyst delivery pump; the catalyst storage tank is connected with the slurry pool through a catalyst delivery pump, and the catalyst storage tank is filled with a catalyst for realizing SO in alkaline absorption liquid2And NO2A synergistically removed catalyst.
Preferably, the pre-oxidation system further comprises a section mixer and a jet grid which are sequentially arranged in the flue; the spraying grid is connected with the outlet of the ultrasonic atomizer; the cross-section mixer is disposed on the upstream side of the injection grid.
Preferably, H2O2A delivery pump is arranged between the storage tank and the ultrasonic atomizer.
Preferably, the flue gas inlet of the absorption tower is connected with the flue outlet through an induced draft fan.
Preferably, the catalyst storage tank is filled with one or a mixture of tributyl phosphate TBP and tetrabutylammonium hydrogen sulfate THS.
The combined desulfurization and denitrification method based on the combination of pre-oxidation and wet catalysis comprises the following steps,
after hydrogen peroxide is subjected to ultrasonic atomization, compressed gas is uniformly sprayed into a flue of an absorption tower, SO that SO is contained2And NO in NO flue gas is oxidized into NO2；
Containing SO2And NO2The flue gas enters an absorption tower and carries out SO treatment under the synergistic action of alkaline absorption liquid and a catalyst of the absorption tower2And NO2And the flue gas is absorbed and removed cooperatively, so that the flue gas is discharged after desulfurization and denitrification.
Preferably, the hydrogen peroxide after ultrasonic atomization is uniformly sprayed into a flue at the flue gas temperature of 250-500 ℃.
Preferably, the mass concentration of the hydrogen peroxide is 20-50%, and the molar ratio of the sprayed hydrogen peroxide to NO is 1-5.
Preferably, the alkaline absorption liquid adopts Ca (OH)2、CaCO3NaOH and NH3·H2At least one of O; the catalyst adopts one or two of tributyl phosphate TBP and tetrabutylammonium hydrogen sulfate THS.
Furthermore, the concentration of the catalyst tributyl phosphate TBP is 10-30%, and the concentration of the catalyst tetrabutylammonium hydrogen sulfate THS is 1-2%.
Compared with the prior art, the invention has the following beneficial technical effects:
the system is provided with a front-end oxidation system and adopts H2O2By substitution of oxidizing agents for O3The compressed air is conveyed to the flue in an atomization mode carried by ultrasonic atomization and compressed air, and compared with direct atomization of the compressed air, H2O2The particle size of the molecular atomization is smaller, and H is avoided2O2Ineffective decomposition during evaporation, thereby reducing H2O2Oxygen amount, simultaneously with H2O2The NO oxidation efficiency is improved to more than 98%, and under the same condition, H2O2The cost of oxidation is only O 31/15 of oxidation cost, simple whole equipment and low investment and operation cost; meanwhile, the absorption system adopts a wet spraying absorption tower which is connected with a catalyst feeding system, and the catalyst is added into the absorption slurry to promote SO2、NO2And the denitration efficiency is improved through synergistic absorption.
Furthermore, the system of the invention also adopts a mode of arranging a section mixer on the upstream side of the jet grid to ensure that H is mixed with the mixed gas2O2Can be fully mixed with the flue gas, thereby improving the treatment effect.
Furthermore, the system adopts a mode of arranging the delivery pump to deliver the hydrogen peroxide into the ultrasonic atomizer, thereby improving the treatment efficiency.
Furthermore, the system of the invention can ensure the absorption efficiency in the absorption tower by arranging the induced draft fan to send the flue gas in the flue into the absorption tower.
The method adopts an ultrasonic atomization and compressed air carrying atomization mode and adopts H2O2For oxidizing agents, by ultrasonic atomization, of H2O2The particle size of the molecular atomization is smaller, and H is avoided2O2Ineffective decomposition during evaporation to promote oxidation of NO to NO2Efficiency of (2) of (H)2O2The NO oxidation efficiency is improved to more than 98 percent; on the basis, adding the para-SO into the absorption tower2And NO2Catalyst for synergistic absorption and removal to greatly improve NO2Absorption efficiency, achievement of SO2、NOxThe integrated removal is realized, the oxidation cost is low, and the removal efficiency is high; because of the adoption of H2O2Is green oxidant, and its decomposition product is H2O, avoid excessive O3The secondary pollution caused by spraying; and H2O2NO oxidation has strong selectivity and NO SO generation2Problem of oxidation, SO can be realized2、NOxAnd various pollutants such as Hg, VOC and the like are removed integrally, low-temperature denitration can be realized, and the market potential is huge.
Furthermore, the method of the invention can effectively ensure atomized H by uniformly spraying the hydrogen peroxide after ultrasonic atomization into the flue at the flue temperature of 250-500 DEG C2O2The efficiency of oxidation.
Furthermore, the method adopts organic extracting agents of tributyl phosphate TBP and tetrabutylammonium hydrogen sulfate THS as catalysts to stabilize SO in a desulfurization system3 2-Thereby increasing NO2The absorption efficiency is high, and the catalyst only plays a catalytic role in an absorption system and is not consumed, so the operation cost is low.
Drawings
FIG. 1 is a schematic view of the structure of the process system of the present invention.
FIG. 2 is H2O2Compression atomization NO characterization.
FIG. 3 is H2O2The characteristic diagram of the ultrasonic atomization oxidation NO.
FIG. 4 shows TBP catalyzed SO2/NO2And (3) a schematic diagram of the synergistic absorption denitration characteristics.
FIG. 5 shows THS catalyzed SO2/NO2And (3) a schematic diagram of the synergistic absorption denitration characteristics.
In the figure: 1 is H2O2A storage tank, 2 a delivery pump, 3 a compressed gas tank, 4 an ultrasonic atomizer and 5The device comprises a jet grid, 6 a section mixer, 7 an induced draft fan, 8 an absorption tower, 9 a catalyst storage tank, 10 a catalyst delivery pump and 11 a chimney.
Detailed Description
The present invention will now be described in further detail with reference to specific examples, which are intended to be illustrative, but not limiting, of the invention.
The invention discloses a preposed oxidation and wet catalysis combined desulfurization and denitrification system, which comprises a preposed oxidation system, an absorption system, a catalyst feeding system and a chimney as shown in figure 1. The pre-oxidation system comprises H connected in sequence2O2Storage tank 1, delivery pump 2, ultrasonic atomizer 4, atomized H2O2The ultrasonic atomizer 4 is carried by compressed gas, the inlet is connected with the compressed gas tank 3, the outlet is connected with the injection grid 5, and the section mixer 6 is arranged in front of the injection grid 5 and used for H2O2Mixing with flue gas. H2O2Sprayed into the flue to oxidize NO into NO2Containing SO2And NO2The flue gas of gas gets into absorption tower 8 through draught fan 7, and absorption tower 8 adopts the wet process spray column, and the thick liquid pond is connected with catalyst storage tank 9 through catalyst delivery pump 10 for maintain the catalyst concentration in the thick liquid pond. The catalyst adopts tributyl phosphate TBP or tetrabutylammonium hydrogen sulfate THS, and the absorption liquid is Ca (OH)2、CaCO3、NaOH、NH3·H2O, etc., SO2、NO2Realize high-efficient removal in coordination under the effect of absorption liquid and catalyst, the outlet of absorption tower 8 is connected with chimney 11, and the flue gas after the SOx/NOx control discharges through the chimney.
In a preferred embodiment of the invention, a section mixer 6 is arranged in front of the injection grid 5 and used for H2O2Fully mixing with the flue gas;
as a preferred embodiment of the present invention, said H2O2A delivery pump 2 is arranged between the storage tank 1 and the ultrasonic atomizer 4;
as a preferred embodiment of the present invention, the flue gas inlet of the absorption tower 8 is connected to the flue outlet through an induced draft fan 7;
in a preferred embodiment of the present invention, the catalyst storage tank 9 contains one or a mixture of tributyl phosphate TBP and tetrabutylammonium hydrogen sulfate THS.
The invention discloses a preposed oxidation and wet catalysis combined desulfurization and denitrification method, which controls the power of an ultrasonic atomizer 4 and the flow of compressed gas to control an oxidant H2O2Amount of injection, H2O2The storage tank 1 and the delivery pump 2 are used for supplementing H in the ultrasonic atomizer 42O2Amount of atomized H at 250-500 deg.C2O2The NO is evenly sprayed into the flue through the spraying grid 5 to be oxidized into NO2The oxidation efficiency is ensured to be more than 98 percent; then containing SO2、NO2The gas enters an absorption tower 8, and SO is strengthened under the action of alkaline absorption liquid and a catalyst2、NO2To realize SO by synergistic absorption2The removal efficiency is more than 98 percent, NO2The removal efficiency is more than 80 percent.
As a preferred embodiment of the invention, the position of the injection grid 5 corresponds to the flue gas temperature of 250-500 ℃;
as a preferred embodiment of the present invention, said H2O2H in the storage tank 12O2Mass concentration of 20-50%, H2O2The molar ratio of the nitrogen-containing organic compound to NO is 1-5;
as a preferable embodiment of the invention, the corresponding concentration of the catalyst tributyl phosphate TBP is 10-30%, the corresponding concentration of the catalyst tetrabutylammonium hydrogen sulfate THS is 1-2%, and the catalyst is one or a mixture of the two.
At present H2O2In the NO oxidation process, H is atomized in a compression mode2O2As shown in fig. 2, the research result of spraying flue NO for oxidation to perform desulfurization and denitrification treatment is that the process oxidation efficiency is low, generally less than 60%; the research results of desulfurization and denitrification treatment by the system and method of the invention are shown in FIG. 3, so that H is2O2The NO oxidation efficiency is improved to more than 98 percent;
meanwhile, the invention provides an ultrasonic atomization and compressed air carrying atomization mode，H2O2Oxidation of NO product to NO2，NO2Is difficult to dissolve in water, the absorption efficiency in a wet desulphurization system is only about 20 percent, and a large number of researches show that SO3 2-Can promote NO2Absorption, and the specific reaction process is shown in formulas (1) and (2). But in O2In the presence of the sulfur, the desulfurizing tower absorbs SO2SO produced3 2-Will be rapidly oxidized to result in NO2The absorption efficiency is low. Therefore, the invention proposes that the NO is improved by adding the liquid catalyst into the wet desulphurization tower2The absorption efficiency is verified through experiments, and TBP and THS can stabilize SO in a desulfurization system3 2-Promoting NO2The absorption efficiency was investigated as shown in fig. 4 and 5.
Based on the research results, the invention provides a preposed oxidation and wet catalysis combined desulfurization and denitrification system and method, namely H is adopted2O2For oxidation, the oxidation of NO to NO is promoted by ultrasonic atomization2On the basis, TBP and THS are added into the desulfurizing tower as catalysts to greatly improve NO2Absorption efficiency, achievement of SO2、NOxIntegrated removal, low oxidation cost and high removal efficiency.
Claims (10)
1. The combined desulfurization and denitrification system combining pre-oxidation and wet catalysis is characterized by comprising a pre-oxidation system arranged on a flue, an absorption system arranged at the outlet of the flue, and a catalyst feeding system and a chimney (11) which are respectively connected with the absorption system;
the pre-oxidation system comprises H connected in sequence2O2Storage tank (1) and ultrasonic atomizer (4), and ultrasonic atomizer(4) A compressed gas tank (3) with an inlet connected; the outlet of the ultrasonic atomizer (4) is connected into the flue;
the absorption system comprises an absorption tower (8); the absorption tower (8) adopts a wet spraying tower, and the bottom of the absorption tower is provided with a slurry tank for containing alkaline absorption liquid; a flue gas inlet of the absorption tower (8) is connected with a flue gas outlet, and a flue gas outlet is connected with a chimney (11);
the catalyst feeding system comprises a catalyst storage tank (9) and a catalyst delivery pump (10); the catalyst storage tank (9) is connected with the slurry pool through a catalyst delivery pump (10), and the catalyst storage tank (9) is filled with a catalyst for realizing SO in alkaline absorption liquid2And NO2A synergistically removed catalyst.
2. The pre-oxidation and wet catalysis combined desulfurization and denitrification system as claimed in claim 1, wherein the pre-oxidation system further comprises a section mixer (6) and an injection grid (5) which are sequentially arranged in the flue; the spraying grid (5) is connected with the outlet of the ultrasonic atomizer (4); the cross-section mixer (6) is disposed on the upstream side of the injection grid (5).
3. The system of claim 1, wherein the H is selected from the group consisting of H, and a combination thereof2O2A delivery pump (2) is arranged between the storage tank (1) and the ultrasonic atomizer (4).
4. The combined desulfurization and denitrification system with combination of pre-oxidation and wet catalysis according to claim 1, wherein the flue gas inlet of the absorption tower (8) is connected with the flue gas outlet through an induced draft fan (7).
5. The system of claim 1, wherein the catalyst storage tank (9) contains one or a mixture of tributyl phosphate (TBP) and Tetrabutylammonium Hydrogen Sulfate (THS).
6. The preposed oxidation and wet catalysis combined desulfurization and denitrification method is characterized by comprising the following steps of,
hydrogen peroxide is atomized by ultrasonic, and then is uniformly sprayed into a flue of an absorption tower (8) by using compressed gas to lead SO2And NO in NO flue gas is oxidized into NO2；
Containing SO2And NO2The flue gas enters an absorption tower (8) and is used for treating SO under the synergistic action of alkaline absorption liquid and a catalyst of the absorption tower (8)2And NO2And the flue gas is absorbed and removed cooperatively, so that the flue gas is discharged after desulfurization and denitrification.
7. The combined desulfurization and denitrification method through combination of pre-oxidation and wet catalysis according to claim 6, wherein the ultrasonically atomized hydrogen peroxide is uniformly sprayed into the flue at a flue temperature of 250-500 ℃.
8. The method for desulfurization and denitrification in combination with pre-oxidation and wet catalysis according to claim 6, wherein the mass concentration of the hydrogen peroxide is 20-50%, and the molar ratio of the injected hydrogen peroxide to NO is 1-5.
9. The method as claimed in claim 6, wherein Ca (OH) is used as alkaline absorption liquid2、CaCO3NaOH and NH3·H2At least one of O; the catalyst adopts one or two of tributyl phosphate TBP and tetrabutylammonium hydrogen sulfate THS.
10. The method for desulfurization and denitrification by combination of pre-oxidation and wet catalysis according to claim 9, wherein the concentration of TBP is 10-30%, and the concentration of THS is 1-2%.
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