CN215842443U - Flue gas treatment system for semi-dry desulfurization and denitrification - Google Patents
Flue gas treatment system for semi-dry desulfurization and denitrification Download PDFInfo
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Abstract
The utility model relates to a flue gas treatment system for semi-dry desulfurization and denitrification. The system comprises a plasma oxidation device, a denitration reaction tower, a concentration tower, a desulfurization absorption tower, a sodium carbonate liquid preparation device, a plurality of flue gas pipelines and a plurality of solution pipelines; the denitration reaction tower is communicated with the plasma oxidation device and the concentration tower, and the concentration tower is communicated with the desulfurization absorption tower; the sodium carbonate solution preparation device is communicated with the concentration tower and the desulfurization absorption tower. The flue gas treatment system can realize denitration and desulfurization treatment of flue gas, does not need to adopt separate equipment for respective treatment, and has the advantages of simple structure, high efficiency and good treatment effect.
Description
Technical Field
The utility model relates to the technical field of flue gas purification, in particular to a flue gas treatment system for semi-dry desulfurization and denitrification.
Background
With the rapid development of industrialization, the problem of atmospheric pollution is gradually highlighted. For example, flue gas generated in furnaces such as steel, cement, building materials, glass, metallurgy and the like contains a large amount of pollutants such as sulfur dioxide, nitrogen oxides, smoke dust and the like, which cause great harm to human health and ecological environment.
In the prior art, a system for simultaneously carrying out denitration and desulfurization treatment usually uses a catalyst and ammonia water, and the treatment method generates waste water and is not beneficial to environmental protection and safety; meanwhile, the method also has the problems of low efficiency, easy failure and the like.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem of providing a flue gas treatment system for semi-dry desulfurization and denitrification.
The technical scheme for solving the technical problems is as follows:
the utility model provides a flue gas treatment system for semi-dry desulfurization and denitrification, which comprises a plasma oxidation device, a denitrification reaction tower, a concentration tower, a desulfurization absorption tower and a sodium carbonate solution preparation device, wherein the plasma oxidation device is connected with the denitrification reaction tower through a pipeline; the denitration reaction tower is respectively communicated with the plasma oxidation device and the concentration tower through two flue gas pipelines, a solution atomizer is fixedly installed in the denitration reaction tower, and the solution atomizer is communicated with the concentration tower through a solution pipeline; a concentration tower nozzle is fixedly arranged in the concentration tower and is communicated with the desulfurization absorption tower through a solution pipeline; the concentration tower is also communicated with the desulfurization absorption tower through a flue gas pipeline; the sodium carbonate solution preparation device is respectively communicated with the concentration tower and the desulfurization absorption tower through two solution pipelines; and a gas recovery port is also arranged on the desulfurization absorption tower.
The sodium carbonate solution preparation device has the beneficial effects that the sodium carbonate solution can be introduced into the desulfurization absorption tower and is used for desulfurizing flue gas, after the flue gas is desulfurized, the sodium carbonate solution reacts to generate sodium sulfite solution, the sodium sulfite solution is introduced into the concentration tower, the flue gas directly exchanges heat with the sodium sulfite solution in the concentration tower, the temperature of the solution in the concentration tower is increased, the temperature of the flue gas is reduced, sodium sulfate and sodium sulfite in the flue gas are condensed and cooled and dissolved in the solution, and the concentration of the sodium sulfite solution is increased to saturation or supersaturation; when the solution is saturated or supersaturated, the solution is introduced into a denitration reaction tower, and the sodium sulfite can continuously carry out denitration treatment on the flue gas; by arranging the solution atomizer, the introduced solution can be atomized, so that the contact area of the solution and the flue gas is increased, and the reaction is more complete; through setting up the concentrated tower nozzle that contracts, can make the interior gas-liquid two-phase countercurrent contact that produces of concentration tower, make heat transfer speed faster.
The technical scheme of the utility model can be further implemented by the following further scheme:
further, a first circulating nozzle is fixedly installed in the concentration tower and is positioned below the concentration tower nozzle; the first circulation nozzle is communicated with the bottom of the concentration tower through a solution pipeline positioned outside the concentration tower.
The beneficial effect of adopting the further technical scheme is that: through setting up circulation nozzle, can make the solution circulation in the concentrated tower spray, make solution can be with the abundant reaction of flue gas.
Further, the denitration reaction tower comprises a cyclone separator and a booster fan, wherein the cyclone separator and the booster fan are arranged on a flue gas pipeline communicated with the denitration reaction tower and the concentration tower, and the booster fan is positioned between the cyclone separator and the concentration tower.
The beneficial effect of adopting the further technical scheme is that: the cyclone separator can separate solid particles in the flue gas and prevent the solid particles from entering the concentration tower to influence the treatment effect; the booster fan can provide power for the introduction of the flue gas.
Further, the desulfurization absorption tower comprises a tower body, and a demister nozzle, a demister, a packing layer and a second circulating nozzle are fixedly installed in the tower body at intervals from top to bottom in sequence; the second circulating nozzle is communicated with the bottom of the tower body through a solution pipeline positioned outside the tower body.
The beneficial effect of adopting the further technical scheme is that: the structure can ensure that the flue gas in the desulfurization absorption tower fully reacts with the solution.
And the process water device is communicated with the second circulating nozzle through a solution pipeline.
Further, the sodium carbonate solution preparation device comprises a sodium carbonate solution tank, and a stirrer is fixedly arranged in the sodium carbonate solution tank; the sodium carbonate solution tank is respectively communicated with the concentration tower and the desulfurization absorption tower through two solution pipelines, and is also communicated with a discharging star-shaped valve weighing machine which is communicated with a sodium carbonate bin.
The beneficial effect of adopting the further technical scheme is that: the above structure enables the supply amount of the sodium carbonate solution to be specifically controlled.
Further, the concentration of the sodium carbonate solution in the sodium carbonate solution tank is 10-20 g/ml.
Further, a pH detection device is fixedly installed on the concentration tower and the desulfurization absorption tower respectively.
The beneficial effect of adopting the further technical scheme is that: so that the pH in the solution can be accurately monitored.
Drawings
FIG. 1 is a schematic structural diagram of a flue gas treatment system for semi-dry desulfurization and denitrification.
In the drawings, the components represented by the respective reference numerals are listed below:
1. a plasma oxidation device;
2. a denitration reaction tower; 21. a swirl plate; 22. a solution atomizer;
3. a cyclone separator; 31. a recovery bin;
4. a booster fan;
5. a concentration tower; 511. a concentrating tower nozzle; 512. a first circulation nozzle;
6. a desulfurization absorption tower; 61. a liquid outlet pump; 62. a second circulation nozzle; 63. a filler layer; 64. a demister; 65. a demister nozzle;
7. a sodium carbonate solution preparation device; 71. a sodium carbonate solution tank; 72. a sodium carbonate bin; 73. a discharging star-shaped valve weighing machine;
8. a process water device.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the utility model.
As shown in fig. 1, the flue gas treatment system for semi-dry desulfurization and denitrification of the present invention comprises a plasma oxidation device 1, a denitrification reaction tower 2, a concentration tower 5, a desulfurization absorption tower 6, a sodium carbonate solution preparation device 7, a plurality of flue gas pipelines and a plurality of solution pipelines; the denitration reaction tower 2 is communicated with the plasma oxidation device 1 through a flue gas pipeline, a solution atomizer 22 is fixedly installed in the denitration reaction tower 2, and the solution atomizer 22 is communicated with the concentration tower 5 through a solution pipeline; a concentration tower nozzle 511 is fixedly arranged in the concentration tower 5, and the concentration tower nozzle 511 is communicated with the desulfurization absorption tower 6 through a solution pipeline; the concentration tower 5 is also communicated with a desulfurization absorption tower 6 through a flue gas pipeline; the sodium carbonate solution preparation device 7 is respectively communicated with the concentration tower 5 and the desulfurization absorption tower 6 through two solution pipelines; the desulfurization absorption tower 6 is also provided with a gas recovery port; the gas recovery port is communicated with a flue gas pipeline, and purified flue gas can be introduced into the collecting device; the sodium carbonate solution preparation device 7 can introduce a sodium carbonate solution into the desulfurization absorption tower 6 for desulfurizing flue gas, after the flue gas is desulfurized, the sodium carbonate solution reacts to generate a sodium sulfite solution, the sodium sulfite solution is introduced into the concentration tower 5, the flue gas directly exchanges heat with the sodium sulfite solution in the concentration tower 5, the temperature of the solution in the concentration tower 5 is increased, the temperature of the flue gas is reduced, sodium sulfate and sodium sulfite in the flue gas are condensed, cooled and dissolved in the solution, and the concentration of the sodium sulfite solution is increased to saturation or supersaturation; when the solution is saturated or supersaturated, the solution is introduced into the denitration reaction tower 2, and the sodium sulfite can continuously carry out denitration treatment on the flue gas; by arranging the solution atomizer 22, the introduced solution can be atomized, so that the contact area of the solution and the flue gas is increased, and the reaction is more complete; by arranging the concentrating tower nozzle 511, gas-liquid two-phase countercurrent contact can be generated in the concentrating tower 5, so that the heat exchange speed is higher.
According to the flue gas treatment system, the plasma oxidation device 1 and the semi-dry denitration and desulfurization treatment process are combined together, so that nitric oxide and sulfur dioxide in the flue gas can be removed simultaneously, the flue gas treatment process is shortened, and the investment cost is reduced; in addition, the sodium sulfite is used as the denitration concentrated solution, so that the use of a catalyst and ammonia water is avoided, secondary pollution caused by wastewater is prevented, and the sodium sulfate product can also be used as a raw material of other industries, so that the reutilization is effectively realized.
For the plasma oxidation device 1 of the present invention, one end is introduced with flue gas to be treated; in the process of discharging of the device in the plasma oxidation device 1, high-energy electrons will excite partial gas in the flue gas to ionize and generate active free radicals, the active particles have strong oxidizing property, partial nitric oxide and sulfur dioxide in the flue gas can be oxidized, and the reaction formula of the specifically occurring chemical reaction is as follows:
H2O+e＝H++OH－+e；
O2+e＝O2++O2++e；
O2++O2+M＝O3+M；
O2++NO＝NO2；
O2++SO2＝SO3。
preferably, the plasma oxidation apparatus 1 includes a housing having an air inlet and an air outlet, a positive electrode disposed in the housing and extending in the direction in which the flue gas flows, and a negative electrode disposed in the housing and extending in the direction in which the flue gas flows and spaced apart from the positive electrode, and a plasma module. The plasma oxidation device 1 is provided with a high-voltage power supply, and a sulfur dioxide and nitrogen oxide analysis instrument, a temperature meter, a pressure meter and a flow meter are respectively arranged at the gas inlet and the gas outlet, so that the temperature, the pressure and the flow of the flue gas can be controlled and detected. The plasma discharge module is formed by connecting a plurality of discharge tubes in parallel, and the number of the discharge tubes can be set according to the oxidation rate of nitric oxide in smoke.
Further preferably, the discharge tube of the plasma module adopts a bobbin type dielectric barrier discharge structure, and a single discharge tube consists of a quartz glass tube and a stainless steel discharge electrode. The spiral stainless steel band is wrapped outside the quartz glass tube to be used as a grounding electrode. The structure is beneficial to enhancing charge diffusion, improving reaction rate and controlling reaction conditions. The high-voltage electrode adopts a suspension type structure and is fixed by an electrode fixing plate, the quartz glass tube is fixed by an organic glass porous plate, and the power supply is a power frequency alternating current high-voltage power supply.
For the denitration reaction tower 2, a rotational flow plate 21 is fixedly arranged in the denitration reaction tower 2, the rotational flow plate 21 is positioned at the bottom of the denitration reaction tower 2, and a solution atomizer 22 is positioned above the rotational flow plate 21; the top of the denitration reaction tower 2 is an air outlet; an air inlet of the denitration reaction tower 2, which is communicated with the plasma oxidation device 1, is positioned on the lower side of the cyclone plate 21; by arranging the rotational flow plate 21 and the solution atomizer 22 in a spraying mode from top to bottom, the contact area between the flue gas and the solution sprayed by the solution atomizer 22 can be increased, the reaction speed is increased, and the denitration reaction is more complete; after denitration, the flue gas rises and is discharged through an air outlet at the top of the denitration reaction tower 2.
Preferably, a solution pipeline of the concentration tower 5 communicated with the solution atomizer 22 is provided with a concentration tower liquid outlet pump for controlling the introduction and flow of the solution.
Preferably, the spraying direction of the solution atomizer 22 is upward, the liquid supersaturated sodium sulfite is dispersed into fine droplets by the solution atomizer 22, and the fine droplets are rapidly evaporated in hot flue gas to form small crystals, and are dried by the high-temperature flue gas to form sodium sulfite solid particles. During the evaporation process, the sodium sulfite particles react with the nitrogen dioxide and residual nitric oxide in the flue gas simultaneously to produce sodium sulfate particles and nitrogen gas. In addition, the flue gas is also mixed with oxygen atoms in the plasma oxidation device 1, and the oxygen atoms can also react with sodium sulfite.
The chemical reaction formulas generated in the denitration reaction tower 2 are respectively as follows:
4Na2SO3+2NO2＝4Na2SO4+N2；
2Na2SO3+2NO＝2Na2SO4+N2；
Na2SO3+O2+＝Na2SO4。
the flue gas treatment system also comprises a cyclone separator 3 and a booster fan 4; the cyclone separator 3 comprises a bin body and a recovery bin 31 communicated with the bin body; the denitration reaction tower 2 is communicated with the bin body of the cyclone separator 3 through a flue gas pipeline, the bin body of the cyclone separator 3 is also communicated with the booster fan 4 through a flue gas pipeline, and the booster fan 4 is communicated with the concentration tower 5 through a flue gas pipeline. Most of solid particles generated after denitration in the denitration reaction tower 2 are removed from the flue gas through the cyclone separator 3, and a small amount of small particle dust enters the concentration tower 5 along with the flue gas.
For the concentrating tower 5 of the present invention, a first circulation nozzle 512 is fixedly installed inside, and the first circulation nozzle 512 is positioned below the concentrating tower nozzle 511; the first circulation nozzle 512 is communicated with the bottom of the concentration tower 5 through a solution pipe located outside the concentration tower 5; the first circulation nozzle 512 can circularly spray the solution in the concentration tower 5, so that the solution can fully react with the flue gas.
A liquid outlet pump 61 is arranged on a solution pipeline of the concentration tower nozzle 511 communicated with the desulfurization absorption tower 6 and is used for controlling the amount of the sodium sulfite solution introduced into the concentration tower 5 by the desulfurization absorption tower 6 so as to supplement the sodium sulfite solution; the solution pipeline of the concentration tower 5 communicated with the sodium carbonate solution preparation device 7 is provided with an adjusting pump for controlling the amount of sodium carbonate introduced into the concentration tower 5, so that the pH value of the sodium sulfite solution can be adjusted.
The top of the concentration tower is provided with an air outlet, and the side wall of the concentration tower is provided with an air inlet communicated with the booster fan 4.
Preferably, the concentration tower 5 is made of corrosion-resistant material, or its inner wall is coated with corrosion-resistant coating, so that it has sufficient corrosion resistance.
Preferably, the concentrating tower nozzle 511 and the first circulating nozzle 512 are both pressure type conical nozzles, which can keep larger liquid drops and prevent the formation of mist, which causes the crystallization to be separated out and carried by the flue gas.
The flue gas treatment process in the concentration tower 5 is that a small amount of small-particle dust in the flue gas enters the concentration tower 5, the flue gas directly exchanges heat with a sodium sulfite solution, the temperature of the solution in the concentration tower 5 rises, the temperature of the flue gas decreases, and sodium sulfate and sodium sulfite in the flue gas are condensed, cooled and dissolved in the solution, so that the concentration of the sodium sulfite solution is improved to saturation or supersaturation.
The concentration tower 5 adopts gas-liquid two-phase countercurrent contact, the flue gas sprays downwards from the upper part of the tower from bottom to top, and the height, width or inner diameter of the concentration tower 5 needs to ensure that the gas and the liquid have enough contact time and area so that the gas and the liquid can exchange heat fully; gas-liquid two phases can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small.
The desulfurization absorption tower 6 comprises a tower body, wherein demister nozzles 65, demisters 64, a packing layer 63 and second circulating nozzles 62 are fixedly arranged in the tower body at intervals from top to bottom; the second circulating nozzle 62 is communicated with the bottom of the tower body through a solution pipeline positioned outside the tower body; the second circulation nozzle 62 is connected to the process water unit 8 via a solution line.
Preferably, the dust collector 64 is an integrated tubular dust and mist eliminator, which can reduce liquid droplet entrainment and reduce the sulfate content in the clean flue gas. The demister 64 is in communication with the process water unit 8 and may be periodically flushed with process water.
Preferably, the desulfurization absorption tower 6 is made of a corrosion-resistant material, or the inner wall thereof is coated with a corrosion-resistant coating, so that the desulfurization absorption tower has sufficient corrosion resistance.
Preferably, the demister nozzles 65 and the second circulating nozzles 62 are arranged in a layered manner, and the nozzles are pressure type conical nozzles, so that the spraying angle is large, uniform and not easy to block.
Preferably, a circulating pump is arranged on a solution pipeline of the second circulating nozzle 62 communicated with the desulfurization absorption tower 6, and the sodium carbonate absorption solution in the desulfurization absorption tower 6 can be sent to the second circulating nozzle 62 through the circulating pump. The chemical equation of the main reaction in the desulfurization absorption tower 6 is:
Na2CO3+SO2＝Na2SO3+CO2；
Na2CO3+H2O+SO2＝NaHSO3+NaHCO3；
NaHCO3+SO2＝NaHSO3+CO2；
2NaHSO3+Na2CO3＝2Na2SO3+CO2+H2O；
Na2CO3+SO3＝Na2SO4+CO2。
the desulfurization absorption tower 6 adopts gas-liquid countercurrent contact, and the absorption solution sodium carbonate flows downwards from the upper part of the tower from bottom to top of the flue gas and is dispersed in a gas phase in a liquid drop shape. The volume and the size of the desulfurization absorption tower 6 need to ensure that the gas and the liquid have enough contact time and area; gas-liquid two phases can be disturbed strongly, the operation range is wide, the operation is stable, and the resistance is small. After the flue gas after preliminary desulfurization cooling enters a desulfurization absorption tower 6, further desulfurization is carried out by utilizing a sodium carbonate solution, the concentration and the pH value of absorption liquid are controlled, and the desulfurization efficiency is ensured.
The sodium carbonate solution preparation device 7 comprises a sodium carbonate solution tank 71, wherein a stirrer is fixedly arranged in the sodium carbonate solution tank 71; the sodium carbonate solution tank 71 is respectively communicated with the concentration tower 5 and the desulfurization absorption tower 6 through branched solution pipelines, the sodium carbonate solution tank 71 is also communicated with a discharging star-shaped valve weighing machine 73, and the discharging star-shaped valve weighing machine 73 is communicated with a sodium carbonate bin 72; the discharge star valve weigher 73 can control the amount of sodium carbonate solution.
The working process of the flue gas denitration and desulfurization treatment of the flue gas system provided by the utility model is as follows:
after the system is ready, 10g/ml of sodium carbonate solution is prepared in the sodium carbonate solution tank 71, the sodium carbonate solution at a certain liquid level is fed into the desulfurization absorption tower 6, and then the circulating pump on the solution pipeline communicating the desulfurization absorption tower 6 with the second circulating nozzle 62 is started to start the circulation of the sodium carbonate solution.
Starting a booster fan 4, introducing flue gas into the plasma oxidation device 1, wherein the flue gas to be treated has temperature, raising the temperature of the system after introducing the flue gas, and simultaneously adjusting the air quantity and pressure of the system to ensure that the micro negative pressure in the denitration reaction tower 2 is-0.5 to-0.5 KPa and the flow rate is 0.5 to 1 m/s.
When the flue gas at the gas inlet of the plasma oxidation device 1 reaches 100 ℃, the plasma oxidation device 1 is started, the change of the content of the nitrogen dioxide at the gas outlet of the plasma oxidation device 1 is observed, and proper voltage regulation is carried out, so that the conversion rate of the nitrogen dioxide is improved.
In practical use, the flue gas introduced in the period of time when the temperature of the flue gas at the gas inlet of the system and the plasma oxidation device 1 reaches 100 ℃ directly flows into the desulfurization absorption tower 6 along the system to implement desulfurization, so that denitration cannot be performed, but the period of time is very short, the amount of the flue gas is very small, and the flue gas can not be considered; or a circulation pipeline is arranged at a gas recovery port of the denitration reaction tower 2, so that the part of flue gas is circulated to the plasma oxidation device 1 and enters the system again for denitration treatment.
When the sodium carbonate solution in the desulfurization absorption tower 6 carries out desulfurization reaction on the flue gas, the solution after the reaction is sodium sulfite solution, and when the pH value of the sodium sulfite solution is 6-7, the liquid outlet pump 61 is started to convey the sodium sulfite solution to the concentration tower 5.
The flue gas treatment process in the concentration tower 5 is that a small amount of small-particle dust in the flue gas enters the concentration tower 5, the flue gas directly exchanges heat with a sodium sulfite solution, the temperature of the solution in the concentration tower 5 rises, the temperature of the flue gas decreases, and sodium sulfate and sodium sulfite in the flue gas are condensed, cooled and dissolved in the solution, so that the concentration of the sodium sulfite solution is improved to saturation or supersaturation. After the liquid level of the sodium sulfite solution in the concentration tower 5 reaches a set value, a circulating pump on a solution pipeline communicated with the concentration tower 5 is started, meanwhile, the pH value of the sodium sulfite solution in the concentration tower 5 is monitored to be 6-7, the concentration of the sodium sulfite solution in the concentration tower 5 is monitored, when the sodium sulfite solution is close to saturation or crystals (supersaturation) are separated out, the concentration tower liquid outlet pump is started to introduce the supersaturated sodium sulfite solution into the denitration reaction tower 2, so that the sodium sulfite solution reacts with sulfur dioxide nitrogen in the flue gas in the denitration reaction tower 2, and denitration is realized.
According to the nitrogen oxide concentration of the clean flue gas of the gas recovery port of the desulfurization absorption tower 6, the feeding amount of the reaction tower is adjusted, meanwhile, the star-shaped valve of the blanking port of the cyclone separator 3 is started to discharge, the content of sodium sulfite in the recovered material is analyzed, and the recovered material can be recycled for desulfurization when the content is high.
It should be noted that the concentration tower 5 may initially contain some sodium sulfite solution, or may be empty, but the concentration of the sodium sulfite solution in the concentration tower 5 should be greater than that in the desulfurization absorption tower 6.
The flue gas treatment system can effectively remove sulfur-containing and nitrogen-containing harmful substances in the flue gas, the removal rate of sulfur dioxide reaches over 99 percent, and the removal rate of nitrogen oxide is over 70 percent, so that the risk of environmental pollution caused by flue gas emission is reduced. The flue gas treatment system has the advantages of simple structure, easy manufacture, safe and reliable use and convenient implementation, popularization and application. The process can be shortened, the investment cost is reduced, the product sodium sulfate of desulfurization and denitrification can be used for other industrial raw materials without evaporation, crystallization and filtration, no wastewater is discharged, and the method has good practical application prospect.
In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc., indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the utility model. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (8)
1. A flue gas treatment system for semi-dry desulfurization and denitrification is characterized by comprising a plasma oxidation device (1), a denitrification reaction tower (2), a concentration tower (5), a desulfurization absorption tower (6) and a sodium carbonate liquid preparation device (7);
the denitration reaction tower (2) is respectively communicated with the plasma oxidation device (1) and the concentration tower (5) through two flue gas pipelines, a solution atomizer (22) is fixedly installed in the denitration reaction tower (2), and the solution atomizer (22) is communicated with the concentration tower (5) through a solution pipeline;
a concentration tower nozzle (511) is fixedly arranged in the concentration tower (5), and the concentration tower nozzle (511) is communicated with the desulfurization absorption tower (6) through a solution pipeline; the concentration tower (5) is also communicated with the desulfurization absorption tower (6) through a flue gas pipeline;
the sodium carbonate liquid preparation device (7) is respectively communicated with the concentration tower (5) and the desulfurization absorption tower (6) through two solution pipelines;
and a gas recovery port is also arranged on the desulfurization absorption tower (6).
2. The flue gas treatment system for semi-dry desulfurization and denitrification according to claim 1, wherein a first circulating nozzle (512) is fixedly installed in the concentration tower (5), and the first circulating nozzle (512) is positioned below the concentration tower nozzle (511);
the first circulation nozzle (512) is communicated with the bottom of the concentration tower (5) through a solution pipeline positioned outside the concentration tower (5).
3. The semi-dry desulfurization and denitrification flue gas treatment system according to claim 1, further comprising a cyclone separator (3) and a booster fan (4), wherein the cyclone separator (3) and the booster fan (4) are arranged on a flue gas pipeline of the denitrification reaction tower (2) communicated with the concentration tower (5), and the booster fan (4) is positioned between the cyclone separator (3) and the concentration tower (5).
4. The flue gas treatment system for semi-dry desulfurization and denitrification according to claim 1, wherein the desulfurization absorption tower (6) comprises a tower body, and a demister nozzle (65), a demister (64), a packing layer (63) and a second circulating nozzle (62) are fixedly arranged in the tower body at intervals from top to bottom;
the second circulating nozzle (62) is communicated with the bottom of the tower body through a solution pipeline positioned outside the tower body.
5. The flue gas treatment system for semi-dry desulfurization and denitrification according to claim 4, further comprising a process water device (8), wherein the process water device (8) is communicated with the second circulating nozzle (62) through a solution pipeline.
6. The flue gas treatment system for semi-dry desulfurization and denitrification according to claim 1, wherein the sodium carbonate solution preparation device (7) comprises a sodium carbonate solution tank (71), and a stirrer is fixedly installed in the sodium carbonate solution tank (71);
the sodium carbonate solution tank (71) is respectively communicated with the concentration tower (5) and the desulfurization absorption tower (6) through two solution pipelines, the sodium carbonate solution tank (71) is also communicated with a discharging star-shaped valve weighing machine (73), and the discharging star-shaped valve weighing machine (73) is communicated with a sodium carbonate bin (72).
7. The flue gas treatment system for semi-dry desulfurization and denitrification according to claim 6, wherein the concentration of the sodium carbonate solution in the sodium carbonate solution tank (71) is 10-20 g/ml.
8. The flue gas treatment system for semi-dry desulfurization and denitrification according to any one of claims 1 to 6, wherein the concentration tower (5) and the desulfurization absorption tower (6) are respectively and fixedly provided with a pH detection device.
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| CN113680194A (en) * | 2021-09-15 | 2021-11-23 | 北京清新环境技术股份有限公司 | Flue gas treatment system and flue gas treatment method for semi-dry desulfurization and denitrification |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113680194A (en) * | 2021-09-15 | 2021-11-23 | 北京清新环境技术股份有限公司 | Flue gas treatment system and flue gas treatment method for semi-dry desulfurization and denitrification |
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