CN217068332U - Desulfurization and denitrification system - Google Patents
Desulfurization and denitrification system Download PDFInfo
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- CN217068332U CN217068332U CN202121287271.1U CN202121287271U CN217068332U CN 217068332 U CN217068332 U CN 217068332U CN 202121287271 U CN202121287271 U CN 202121287271U CN 217068332 U CN217068332 U CN 217068332U
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Abstract
The utility model belongs to the technical field of flue gas purification is relevant, it discloses a SOx/NOx control system, and this system includes H 2 O 2 Supply device, H 2 O 2 Transport pipe, H 2 O 2 A gasification mixing device, a microwave generation device and a catalytic oxidation device, wherein：H 2 O 2 The conveying pipeline is positioned in the flue gas pipeline, and one end of the conveying pipeline is connected with the H 2 O 2 The other end of the supply device is connected with H 2 O 2 A gasification mixing device; h 2 O 2 The outlet end of the gasification mixing device is provided with a spraying grid which is positioned in the flue gas pipeline, and the carrier gas and the H gas are mixed 2 O 2 The 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 H 2 O 2 Catalytic oxidation to OH radicals. The application combines heating atomization and microwave catalysis to enable H 2 O 2 A 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 utility model belongs to the technical field of flue gas purification is relevant, more specifically relates to a SOx/NOx control system.
Background
A large amount of pollutants such as sulfur dioxide, nitrogen oxide and the like are generated in the coal-fired power generation process. 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.
SUMMERY OF THE UTILITY MODEL
To the defects of the prior art, the utility model aims at providing a desulfurization and denitrification device, which jointly makes H by heating atomization and microwave catalysis 2 O 2 A 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.
In order to achieve the above object, the utility model provides a SOx/NOx control system, the system includes H 2 O 2 Supply device, H 2 O 2 Transport pipe, H 2 O 2 Gasification mixing arrangement, microwave generating device and catalytic oxidation device, wherein: said H 2 O 2 The transport pipeline is positioned in the flue gas pipeline, and one end of the transport pipeline is connected with the H 2 O 2 The other end of the supply device is connected with the H 2 O 2 A gasification mixing device, through which the flue gas in the flue gas pipeline passes 2 O 2 H in the conveying pipeline pair 2 O 2 Heating, the heated H 2 O 2 Enters the H under the action of carrier gas 2 O 2 A gasification mixing device; said H 2 O 2 The 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 mixed 2 O 2 The 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 gas 2 O 2 Heating and catalyzing for atomizing H 2 O 2 Catalytic oxidation to OH radicals.
Preferably, said H 2 O 2 The outlet of the conveying pipeline is a swirl nozzle, and H is 2 O 2 The 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 H 2 O 2 The 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) x Ti 1-x )O 3 、Ce(Fe x Ti 1-x )O 3 And Sr (Fe) x Ti 1-x )O 3 One 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, 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 through a circulating pump for recycling.
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/m 3 -3000W/m 3 。
Preferably, the carrier gas is air, and the temperature of the carrier gas is 140-180 ℃.
Through the utility model discloses above technical scheme who thinks, compare with prior art, the utility model provides a pair of desulfurization takes off system has following beneficial effect:
1. h of the present application 2 O 2 The transport duct is located in the flue gas duct so that H 2 O 2 Heated during transportation and then atomized by a spray grid so that H 2 O 2 The 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.H 2 O 2 the outlet of the conveying pipeline is a swirl nozzle, and H is 2 O 2 The inlet of the gasification mixing device is a convergent-divergent nozzle which can lead the heated H 2 O 2 Is atomized quickly, and the atomization efficiency is improved obviously;
3. for H in microwave and catalyst coupling heating process 2 O 2 Compared 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 H 2 O 2 Active 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 application provides a catalyst low cost, and have higher air space velocity ratio, satisfy the flue gas processing requirement of big flue gas flow, high velocity of flow among the practical application, the catalyst that uses among the reaction process is small, and efficient can be designed into small-size fixed bed with it, reduces construction cost, practices thrift the occupation of land space.
Drawings
FIG. 1 is a schematic view of a SOx/NOx control system according to the present embodiment;
FIG. 2 shows this embodiment H 2 O 2 Schematic 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-H 2 O 2 liquid storage tank, 2-electric pump, 3-H 2 O 2 The 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 clearly understood, the present invention is further described in 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.
Referring to fig. 1, the present invention provides a desulfurization and denitrification system, which comprises a H-shaped catalyst 2 O 2 Supply device, H 2 O 2 Transport pipe, H 2 O 2 A gasification mixing device, a microwave generating device and a catalytic oxidation device.
H 2 O 2 The supply device comprises 2 O 2 Liquid storage tank 1 and electric pump 2, H 2 O 2 H in the liquid storage tank 1 2 O 2 Feeding H through said electric pump 2 2 O 2 A delivery conduit.
Said H 2 O 2 The transport pipeline is positioned in the flue gas pipeline, and one end of the transport pipeline is connected with the H 2 O 2 Another supply deviceEnd-connected to the H 2 O 2 A gasification mixing device 3 through which the flue gas in the flue gas pipeline passes 2 O 2 H in the conveying pipeline pair 2 O 2 Heating, the heated H 2 O 2 Enters the H under the action of carrier gas 2 O 2 A gasification mixing device.
Specifically, the above-mentioned H 2 O 2 The part of the conveying pipeline, which is positioned in the smoke pipeline, is made of heat conducting materials and is in a spiral shape. So that H 2 O 2 Is sufficiently heated by the flue gas in the conveying pipeline.
As shown in FIG. 2, said H 2 O 2 The outlet of the conveying pipeline is a swirl nozzle, and H is 2 O 2 The 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 H 2 O 2 And 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 ℃. H 2 O 2 The gas at the outlet of the conveying pipeline is uniformly mixed with the preheated air.
Said H 2 O 2 The 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 mixed 2 O 2 The 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 mixed 2 O 2 Heating and catalyzing for atomizing H 2 O 2 Catalytic 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/m 3 -3000W/m 3 . The catalyst 8 in the catalytic oxidation apparatus is preferably a perovskite-type composite catalyst, and may be, for example, La (Fe) x Ti 1-x )O 3 、 Ce(Fe x Ti 1-x )O 3 And Sr (Fe) x Ti 1-x )O 3 One or a plurality of combinations in the catalyst, the main active component of the catalyst is redox coordination Fe on the surface 2 + /Fe 3+ And Ti 3+ /Ti 4+ Can accelerate the surface H 2 O 2 Electron transfer in the molecule, catalyzing H 2 O 2 Active substances such as OH are generated by decomposition. The catalyst is preferably in the form of a honeycomb catalyst for catalyzing H 2 O 2 OH free radicals generated by steam react with NO and SO in the flue gas 2 、 Hg 0 And (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 added 2 S removal of Hg from solution 2+ 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 absorbed 2 、HNO 2 、HNO 3 And Hg 2+ And SO 2 And H 2 SO 4 And the like.
In this example, the H 2 O 2 The solution concentration is 10-25 wt%, and the liquid-gas ratio is 10-20L/m 3 . Said H 2 O 2 The temperature of the air inlet of the gasification mixing device is 140-. Catalyst gas space velocity ratio of 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/m 3 -3000W/m 3 。
In the course of operation, H 2 O 2 The solution enters H through the electric pump 2 by preheating through a flue gas pipeline 2 O 2 The 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, H 2 O 2 Catalytic decomposition of catalyst to generate active molecules OH, etc. to remove NO and SO from fume 2 、Hg 0 Oxidation 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 gas 2 、Hg 2+ 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 11 2 S removal of Hg from solution 2 + 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 H 2 O 2 The steam decomposition includes the following reactions:
Fe 2+ +H 2 O 2 →Fe 3+ +OH - +·OH
Fe 3+ +H 2 O 2 →Fe 2+ +H + +·OOH
Ti 3+ +H 2 O 2 →Ti 4+ +OH - +·OH
Ti 4+ +H 2 O 2 →Ti 3+ +H + +·OOH
H 2 O 2 OH and SO formed by decomposition 2 NO and Hg 0 The reactions that occur are respectively:
NO+H 2 O 2 →NO 2 +H 2 O
2NO+3H 2 O 2 →2HNO 3 +2H 2 O
2NO 2 +H 2 O 2 →2HNO 3
NO+·OH→NO 2 +·H
NO+·OH→HNO 2
HNO 2 +·OH→HNO 3 +·H
2·OH+Hg+2H + →Hg 2+ +2H 2 O
NO oxidation product and SO 2 The absorption process of (a) takes place in the following reaction:
NO 2 +NO+H 2 O→2NO 2- +2H +
3NO 2 +H 2 O→2NO 3- +NO+2H +
example 1
Example 2
Example 3
Example 4
Example 5
Example 6
Example 7
Example 8
Example 9
It can be seen from the above embodiments that the present application adopts microwave and catalyst coupled catalysis, and can realize better desulfurization and denitrification effects compared with single microwave catalysis and catalyst catalysis. SO under optimum conditions 2 The removal efficiency can reach 100 percent, the removal efficiency of NO can reach 98.6 percent, and Hg 0 The removal efficiency can reach 98.4%.
To sum up, the utility model discloses a fully preheat the atomizing to combine heterogeneous catalyst and microwave coupling effect's method to come catalytic oxidation flue gas pollutant, can make H 2 O 2 The 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, SO 2 The removal efficiency can reach 100 percent, the removal efficiency of NO can reach 98.6 percent, and Hg 0 The removal efficiency can reach 98.4%.
It will be understood by those skilled in the art that the foregoing is merely a preferred embodiment of the present invention, and is not intended to limit the invention to the particular forms disclosed, but on the contrary, the intention is to cover all modifications, equivalents, and alternatives falling within the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. The desulfurization and denitrification system is characterized by comprising H 2 O 2 Supply device, H 2 O 2 Transport pipe, H 2 O 2 Gasification mixing arrangement, microwave generating device and catalytic oxidation device, wherein:
said H 2 O 2 The transport pipeline is positioned in the flue gas pipeline, and one end of the transport pipeline is connected with the H 2 O 2 The other end of the supply device is connected with the H 2 O 2 A gasification mixing device, through which the flue gas in the flue gas pipeline passes 2 O 2 H in the conveying pipeline pair 2 O 2 Heating, the heated H 2 O 2 Enters the H under the action of carrier gas 2 O 2 A gasification mixing device;
said H 2 O 2 The outlet end of the gasification mixing device is provided with a spray grid which is positioned in the flue gas pipeline, the carrier gas and the H 2 O 2 The 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 are positioned on the spraying gridsDownstream of the grid for atomizing H 2 O 2 The heating catalyzes the oxidation to OH free radicals.
2. The system of claim 1, wherein the H is 2 O 2 The outlet of the conveying pipeline is a swirl nozzle, and H is 2 O 2 The 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 is 2 O 2 The 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 1, further comprising an absorption tower connected to the outlet of the catalytic oxidation unit for absorbing the flue gas after catalytic oxidation.
6. The system of claim 5, wherein the absorption tower comprises a nozzle positioned at the upper part and absorption liquid positioned 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.
7. 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.
8. The system of claim 7, wherein the microwave generating device has a microwave radiation power density of 500W/m 3 -3000W/m 3 。
9. 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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| CN113262617A (en) * | 2021-06-09 | 2021-08-17 | 华中科技大学 | Desulfurization and denitrification system |
| CN113262617B (en) * | 2021-06-09 | 2024-05-14 | 华中科技大学 | Desulfurization and denitrification system |
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