CN113262617A - Desulfurization and denitrification system - Google Patents
Desulfurization and denitrification system Download PDFInfo
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- CN113262617A CN113262617A CN202110642317.5A CN202110642317A CN113262617A CN 113262617 A CN113262617 A CN 113262617A CN 202110642317 A CN202110642317 A CN 202110642317A CN 113262617 A CN113262617 A CN 113262617A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 11
- 230000023556 desulfurization Effects 0.000 title claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 54
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 51
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 28
- 230000003647 oxidation Effects 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 25
- 238000002309 gasification Methods 0.000 claims abstract description 24
- 230000003197 catalytic effect Effects 0.000 claims abstract description 23
- 239000007921 spray Substances 0.000 claims abstract description 17
- 239000012159 carrier gas Substances 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims abstract description 12
- 238000010438 heat treatment Methods 0.000 claims abstract description 11
- 238000005507 spraying Methods 0.000 claims abstract description 7
- 238000010521 absorption reaction Methods 0.000 claims description 26
- 239000003054 catalyst Substances 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 17
- 239000002131 composite material Substances 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 4
- 230000005855 radiation Effects 0.000 claims description 4
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000004020 conductor Substances 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 239000010453 quartz Substances 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 238000006555 catalytic reaction Methods 0.000 abstract description 7
- 238000000889 atomisation Methods 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 2
- 239000001257 hydrogen Substances 0.000 abstract 1
- 229910052739 hydrogen Inorganic materials 0.000 abstract 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 239000007800 oxidant agent Substances 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 5
- 230000001590 oxidative effect Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 3
- 239000013543 active substance Substances 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 238000004435 EPR spectroscopy Methods 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003421 catalytic decomposition reaction Methods 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001808 coupling effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000010248 power generation Methods 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
- B01D53/46—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
- 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
- B01D53/007—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 by irradiation
-
- 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
-
- 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
- B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
-
- 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
- B01D53/88—Handling or mounting catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/106—Peroxides
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/80—Employing electric, magnetic, electromagnetic or wave energy, or particle radiation
- B01D2259/806—Microwaves
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Toxicology (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention belongs to the technical field related to flue gas purification, and discloses a desulfurization and denitrification system which comprises a hydrogen (H)2O2Supply device, H2O2Transport pipe, H2O2Gasification mixing arrangement, microwave generating device and catalytic oxidation device, wherein: h2O2The conveying pipeline is positioned in the flue gas pipeline, and one end of the conveying pipeline is connected with the H2O2The other end of the supply device is connected with H2O2A gasification mixing device; h2O2The outlet end of the gasification mixing device is provided with a spraying grid which is positioned in the flue gas pipelineInternal, carrier gas and H2O2The mixed gas is atomized by the spraying grating and then mixed with the flue gas; the microwave generating device and the catalytic oxidation device are connected with the flue gas pipeline and positioned at the downstream of the spray grating for atomizing the atomized H2O2Catalytic oxidation to OH radicals. The application combines heating atomization and microwave catalysis to enable H2O2A large amount of OH free radicals are quickly excited to meet the requirements of flue gas desulfurization and denitration, and the device is high in efficiency and small in size.
Description
Technical Field
The invention belongs to the technical field related to flue gas purification, and particularly relates to a desulfurization and denitrification system.
Background
At present, coal consumption still occupies a leading position in energy consumption in China. A large amount of pollutants such as sulfur dioxide, nitrogen oxides and the like are generated in the coal-fired power generation process, serious problems such as haze, acid rain, photochemical pollution and the like can be caused, and the environmental influence is very severe. The NOx emission standard is increasingly strict with the continuous improvement of NOx treatment technology and environmental protection requirements, and the emission concentration of nitrogen oxides respectively does not exceed 50mg/m3 according to the current standard. The simple series arrangement of the existing selective catalytic reduction method and the wet desulphurization system (SCR-WFGD) in the thermal power plant has the defects of large floor area, complex system, high investment and operation cost and the like.
Chinese patent CN105032142A provides an inverted U-shaped pre-oxidizer, the flue gas is with higher speed at the venturi tube of inverted U-shaped pre-oxidizer, the gas phase composite oxidant spouts people in venturi tube constriction department, former flue gas after accelerating strikes and carries the type gas phase composite oxidant and gets into oxidizer main part, the torrent effect of porous baffle in order to strengthen the flue gas has been arranged to the venturi tube exit, flue gas need pass through venturi tube and porous baffle in the device, pressure fluctuation and pressure drop are great, be unfavorable for the great operating mode of handling flue gas volume. Therefore, it is necessary to develop an efficient and economical integrated flue gas removal technology.
Disclosure of Invention
In view of the above defects or improvement needs of the prior art, the present invention provides a desulfurization and denitrification apparatus, which combines heating atomization and microwave catalysis to make H2O2A large amount of OH free radicals are quickly excited to meet the requirements of flue gas desulfurization and denitration, and the device is high in efficiency and small in size.
To achieve the above objects, according to one aspect of the present invention, there is provided a desulfurization and denitrification system including H2O2Supply device, H2O2Transport pipe, H2O2Gasification mixing arrangement, microwave generating device and catalytic oxidation device, wherein: said H2O2The transport pipeline is positioned in the flue gas pipeline, and one end of the transport pipeline is connected with the H2O2The other end of the supply device is connected with the H2O2A gasification mixing device, through which the flue gas in the flue gas pipeline passes2O2H in the conveying pipeline pair2O2Heating, the heated H2O2Enters the H under the action of carrier gas2O2A gasification mixing device; said H2O2The outlet end of the gasification mixing device is provided with a spray grid which is positioned in the flue gas pipeline, and the carrier gas and the H gas are mixed2O2The mixed gas is atomized by the spraying grating and then mixed with the flue gas; the microwave generating device and the catalytic oxidation device are connected with the flue gas pipeline, positioned at the downstream of the spraying grid and used for mixing the H with the flue gas2O2Heating and catalyzing for atomizing H2O2Catalytic oxidation to OH radicals.
Preferably, said H2O2The outlet of the conveying pipeline is a swirl nozzle, and H is2O2The inlet of the gasification mixing device is a reducing and gradually expanding spray pipe, and the swirl nozzle is arranged at the middle section of the spray pipe.
Preferably, said H2O2The part of the conveying pipeline, which is positioned on the flue gas pipeline, is made of heat conducting materials and is in a spiral shape.
Preferably, the catalyst in the catalytic oxidation apparatus is a perovskite-type composite catalyst.
Preferably, the catalyst is La (Fe)xTi1-x)O3、Ce(FexTi1-x)O3And Sr (Fe)xTi1-x)O3One or a combination of several of them.
Preferably, the system further comprises an absorption tower connected to the outlet of the catalytic oxidation device and used for absorbing the flue gas after catalytic oxidation.
Preferably, the absorption tower comprises a nozzle positioned at the upper part and absorption liquid positioned at the lower part of the nozzle, the bottom end of the absorption tower is connected with a separator, impurities in the absorption liquid are removed by the separator, and the treated absorption liquid is sent to the nozzle for recycling through a circulating pump.
Preferably, the microwave generating device is connected with the flue gas pipeline through a microwave guide pipe, and a quartz or ceramic baffle plate is arranged at the connection position.
Preferably, the microwave radiation power density of the microwave generating device is 500W/m3-3000W/m3。
Preferably, the carrier gas is air, and the temperature of the carrier gas is 140-180 ℃.
Generally, compared with the prior art, the desulfurization and desorption system provided by the invention has the following beneficial effects:
1. h of the present application2O2The transport duct is located in the flue gas duct so that H2O2Heated during transportation and then atomized by a spray grid so that H2O2The mixed gas is more uniform and can be further efficiently excited to generate active substances such as OH and the like under the action of microwaves and catalysts, so that the catalytic oxidation efficiency of the smoke pollutants is remarkably improved, and the requirement of large-scale smoke treatment can be met;
2.H2O2the outlet of the conveying pipeline is a swirl nozzle, and H is2O2The inlet of the gasification mixing device is a convergent-divergent nozzle which can lead the heated H2O2Is atomized quickly, and the atomization efficiency is obviously improved;
3. for H in microwave and catalyst coupling heating process2O2Compared with single microwave catalysis or catalyst catalysis, the catalyst has higher EPR (electron paramagnetic resonance) signal intensity, and shows that the coupling mode can more efficiently excite H2O2Active substances such as OH and the like are generated, the catalyst can work at the optimal working temperature under the microwave heating, the highest catalytic efficiency is achieved, and the pollutant removal efficiency can be kept at a high level.
4. The catalyst provided by the invention has low cost and higher air-space-time speed ratio, meets the flue gas treatment requirements of large flue gas flow and high flow rate in practical application, has small volume and high efficiency in the reaction process, can be designed into a small fixed bed, reduces the construction cost and saves the occupied space.
Drawings
FIG. 1 is a schematic view of a SOx/NOx control system according to the present embodiment;
FIG. 2 shows this embodiment H2O2Schematic structure of the inlet of the gasification mixing device.
The same reference numbers will be used throughout the drawings to refer to the same or like elements or structures, wherein:
1-H2O2liquid storage tank, 2-electric pump and 3-H2O2The device comprises a gasification mixing device, 4-spray grids, 5-microwave generating devices, 6-baffles, 7-catalytic oxidation devices, 8-catalysts, 10-nozzles, 9-absorption towers, 11-separators and 12-circulating pumps.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. In addition, the technical features involved in the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
Referring to FIG. 1, the present invention provides a desulfurization and denitrification system, which comprises a H2O2Supply device, H2O2Transport pipe, H2O2A gasification mixing device, a microwave generating device and a catalytic oxidation device.
H2O2The supply device comprises2O2 Liquid storage tank 1 and electric pump 2, H2O2H in the liquid storage tank 12O2Feeding H through said electric pump 22O2A delivery conduit.
Said H2O2The transport pipeline is positioned in the flue gas pipeline, and one end of the transport pipeline is connected with the H2O2The other end of the supply device is connected with the H2O2A gasification mixing device 3 through which the flue gas in the flue gas pipeline passes2O2H in the conveying pipeline pair2O2Heating, the heated H2O2Enters the H under the action of carrier gas2O2A gasification mixing device.
Specifically, the above-mentioned H2O2The part of the conveying pipeline, which is positioned on the flue gas pipeline, is made of heat conducting materials and is in a spiral shape. So that H2O2Is sufficiently heated by the flue gas in the conveying pipeline.
As shown in FIG. 2, said H2O2The outlet of the conveying pipeline is a swirl nozzle, and H is2O2The inlet of the gasification mixing device is a reducing and diverging spray pipe, the swirl nozzle is arranged at the middle section of the spray pipe, the diameter of solution liquid drops ejected by the swirl nozzle is not more than 0.5mm, and part of fresh preheated air extracted from the air preheater enters H2O2And the gasification mixing device carries and impacts oxidant liquid drops to uniformly atomize the oxidant liquid drops.
In the embodiment, the carrier gas is preferably preheated air extracted from an air preheater, and the temperature of the carrier gas is 140-180 ℃. H2O2The gas at the outlet of the conveying pipeline is uniformly mixed with the preheated air.
Said H2O2The outlet end of the gasification mixing device is provided with a spray grid 4, the spray grid 4 is positioned in the flue gas pipeline, and the carrier gas and the H gas are mixed2O2The mixed gas is atomized by the spray grid 4 and then mixed with the flue gas.
A microwave generating device 5 and a catalytic oxidation device are connected with the flue gas pipeline and positioned at the downstream of the spraying grid for leading the H to be mixed2O2Heating and catalyzing for atomizing H2O2Catalytic oxidation to OH radicals. The microwave generating device is connected with the flue gas pipeline through a microwave guide pipe, and a quartz or ceramic baffle 6 is arranged at the joint for preventing flue gas from flowing into the microwave generating device. The microwave radiation power density of the microwave generating device is 500W/m3-3000W/m3. Catalytic converterThe catalyst 8 in the oxidation apparatus is preferably a perovskite-type composite catalyst, and may be, for example, La (Fe)xTi1-x)O3、Ce(FexTi1-x)O3And Sr (Fe)xTi1-x)O3One or a plurality of combinations in the catalyst, the main active component of the catalyst is redox coordination Fe on the surface2+/Fe3+And Ti3+/Ti4+Can accelerate the surface H2O2Electron transfer in the molecule, catalyzing H2O2Active substances such as OH are generated by decomposition. The catalyst is preferably in the form of a honeycomb catalyst for catalyzing H2O2OH free radicals generated by steam react with NO and SO in the flue gas2、Hg0And (4) oxidizing.
The outlet of the catalytic oxidation device is connected with an absorption tower 9 for absorbing the flue gas after catalytic oxidation. The absorption tower 9 comprises a nozzle 10 positioned at the upper part and absorption liquid positioned at the lower part of the nozzle 10, a separator 11 is connected to the bottom end of the absorption tower, impurities in the absorption liquid are removed by the separator 11, and the treated absorption liquid is sent to the nozzle for recycling through a circulating pump 12. In the embodiment of the present disclosure, the absorption liquid is ammonia water for absorbing the flue gas after catalytic oxidation, the bottom of the absorption tower 9 is provided with a solution inlet and a solution outlet, the solution outlet is connected to the separator 11, and Na is added2S removal of Hg from solution2+Then the ammonium salt separated by drying crystallization can be used as fertilizer, the residual mother liquor is circulated by a circulating pump 12 through a spray pipe and a nozzle 10, and NO in the smoke can be absorbed2、HNO2、HNO3And Hg2+And SO2And H2SO4And the like.
In this example, the H2O2The solution concentration is 10-25 wt%, and the liquid-gas ratio is 10-20L/m3. Said H2O2The temperature of the air inlet of the gasification mixing device is 140-. Catalyst air space velocity ratio 400000h-1-700000h-1(ii) a The concentration of the ammonia water absorption solution is 5 wt%. The temperature of the microwave generator is 120-180 ℃, and the power density of microwave radiation is 500W/m3-3000W/m3。
In the course of operation, H2O2The solution enters H through the electric pump 2 by preheating through a flue gas pipeline2O2The gasification mixing device 3 is uniformly mixed with part of fresh preheated air extracted by the air preheater, then the mixture is sprayed into a flue gas pipeline through the spray grid 4, and then the mixture flows through the baffle 6 and is subjected to the heating and catalytic action of microwaves generated by the microwave generating device 5;
the mixed gas of the flue gas enters a catalytic oxidation device 7, H2O2Catalytic decomposition of catalyst to generate active molecules OH, etc. to remove NO and SO from fume2、Hg0Oxidation to a soluble valence state;
the flue gas after catalytic oxidation by the catalyst enters an absorption tower 9, and NO and SO in the flue gas2、Hg2+The components with higher solubility are absorbed by the absorption liquid sprayed from the spray pipe and the nozzle 10, and Na is added into the separator 112S removal of Hg from solution2+Then, the ammonium salt separated by drying crystallization can be used as fertilizer, and the residual mother liquor repeatedly enters an absorption tower for use through a circulating pump 12.
Catalyst surface H2O2The steam decomposition includes the following reactions:
Fe2++H2O2→Fe3++OH-+·OH
Fe3++H2O2→Fe2++H++·OOH
Ti3++H2O2→Ti4++OH-+·OH
Ti4++H2O2→Ti3++H++·OOH
H2O2OH and SO formed by decomposition2NO and Hg0The reactions that occur are respectively:
NO+H2O2→NO2+H2O
2NO+3H2O2→2HNO3+2H2O
2NO2+H2O2→2HNO3
NO+·OH→NO2+·H
NO+·OH→HNO2
HNO2+·OH→HNO3+·H
2·OH+Hg+2H+→Hg2++2H2O
NO oxidation product and SO2The absorption process of (a) takes place in the following reaction:
NO2+NO+H2O→2NO2-+2H+
3NO2+H2O→2NO3-+NO+2H+
example 1
Example 2
Example 3
Example 4
Example 5
Example 6
Example 7
Example 8
Example 9
As can be seen from the above examples, the present application adoptsMicrowave and catalyst coupling catalysis, compare single microwave catalysis and catalyst catalysis, can realize better SOx/NOx control effect. SO under optimum conditions2The removal efficiency can reach 100 percent, the removal efficiency of NO can reach 98.6 percent, and Hg0The removal efficiency can reach 98.4%.
In conclusion, the method for fully preheating and atomizing, combining the heterogeneous catalyst and the microwave coupling effect to catalyze and oxidize the smoke pollutants can ensure that H is oxidized2O2The decomposition generates a large amount of OH, which can efficiently and rapidly attack various pollutant molecules flowing on the surface of the catalyst, and the pollutant molecules lose electrons to form high-valence oxides. Under ideal operating conditions, SO2The removal efficiency can reach 100 percent, the removal efficiency of NO can reach 98.6 percent, and Hg0The removal efficiency can reach 98.4%.
It will be understood by those skilled in the art that the foregoing is only a preferred embodiment of the present invention, and is not intended to limit the invention, and that any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (10)
1. The desulfurization and denitrification system is characterized by comprising H2O2Supply device, H2O2Transport pipe, H2O2Gasification mixing arrangement, microwave generating device and catalytic oxidation device, wherein:
said H2O2The transport pipeline is positioned in the flue gas pipeline, and one end of the transport pipeline is connected with the H2O2The other end of the supply device is connected with the H2O2A gasification mixing device, through which the flue gas in the flue gas pipeline passes2O2H in the conveying pipeline pair2O2Heating, the heated H2O2Enters the H under the action of carrier gas2O2A gasification mixing device;
said H2O2The outlet end of the gasification mixing device is provided with a spraying gridA grid located in the flue gas duct, the carrier gas, and H2O2The mixed gas is atomized by the spraying grating and then mixed with the flue gas;
the microwave generating device and the catalytic oxidation device are connected with the flue gas pipeline and positioned at the downstream of the spray grating and used for atomizing the atomized H2O2The heating catalyzes the oxidation to OH free radicals.
2. The system of claim 1, wherein the H is2O2The outlet of the conveying pipeline is a swirl nozzle, and H is2O2The inlet of the gasification mixing device is a reducing and gradually expanding spray pipe, and the swirl nozzle is arranged at the middle section of the spray pipe.
3. The system of claim 1, wherein the H is2O2The part of the conveying pipeline, which is positioned on the flue gas pipeline, is made of heat conducting materials and is in a spiral shape.
4. The system of claim 1, wherein the catalyst in the catalytic oxidation unit is a perovskite-type composite catalyst.
5. The system of claim 4, wherein the catalyst is La (Fe)xTi1-x)O3、Ce(FexTi1-x)O3And Sr (Fe)xTi1-x)O3One or a combination of several of them.
6. The system of claim 1, further comprising an absorption tower connected to the outlet of the catalytic oxidation device for absorbing the flue gas after catalytic oxidation.
7. The system of claim 6, wherein the absorption tower comprises a nozzle at the upper part and absorption liquid at the lower part of the nozzle, a separator is connected to the bottom end of the absorption tower, impurities in the absorption liquid are removed by the separator, and the treated absorption liquid is sent to the nozzle for recycling through a circulating pump.
8. The system of claim 1, wherein the microwave generating device is connected to the flue gas duct by a microwave conduit and is provided with a quartz or ceramic baffle at the connection.
9. The system of claim 8, wherein the microwave generating device has a microwave radiation power density of 500W/m3-3000W/m3。
10. The system of claim 1, wherein the carrier gas is air extracted after an air preheater, and the temperature of the carrier gas is 140-180 ℃.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110642317.5A CN113262617B (en) | 2021-06-09 | 2021-06-09 | Desulfurization and denitrification system |
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|---|---|---|---|
| CN202110642317.5A CN113262617B (en) | 2021-06-09 | 2021-06-09 | Desulfurization and denitrification system |
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| CN113262617A true CN113262617A (en) | 2021-08-17 |
| CN113262617B CN113262617B (en) | 2024-05-14 |
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| CN116099541A (en) * | 2022-12-01 | 2023-05-12 | 华北电力大学（保定） | Preparation of iron-based perovskite catalyst rich in oxygen vacancies and efficient NO removal method thereof |
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