CN111135686A - Semi-dry flue gas desulfurization device and desulfurization method - Google Patents
Semi-dry flue gas desulfurization device and desulfurization method Download PDFInfo
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- CN111135686A CN111135686A CN202010035835.6A CN202010035835A CN111135686A CN 111135686 A CN111135686 A CN 111135686A CN 202010035835 A CN202010035835 A CN 202010035835A CN 111135686 A CN111135686 A CN 111135686A
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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
- B01D53/46—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
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- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
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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
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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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
- B01D53/68—Halogens or halogen compounds
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2047—Hydrofluoric acid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention relates to the technical field of flue gas desulfurization, in particular to a semidry flue gas desulfurization device and a desulfurization method, which comprise a desulfurization section, a dust removal section and an external discharge section, wherein the inlet of the desulfurization section is connected with an original flue gas outlet, the outlet of the desulfurization section is connected with the inlet of the dust removal section, the flue gas outlet of the dust removal section is connected with a chimney, and the lower ash outlet of the dust removal section is connected with the external discharge section; the upper part of the circulating section is connected with an ash outlet at the lower part of the dust removal section; the circulation section comprises a circulation ash bin and an activation device, the inlet of the activation device is connected with the circulation ash bin, and the outlet of the activation device is connected with the desulfurization section. According to the invention, by improving the activity of the circulating ash, the desulfurization efficiency of the semi-dry process is improved, the consumption of a desulfurizing agent is reduced, the circulating amount of the circulating ash is reduced, the resistance of a desulfurization system is reduced, and the power consumption is reduced; the operation load of the rear dust remover is reduced, and the bed layer collapse phenomenon is fundamentally avoided.
Description
Technical Field
The invention relates to the technical field of flue gas desulfurization, in particular to a semidry flue gas desulfurization device and a desulfurization method.
Background
In recent years, serious haze phenomena appear in succession all over the country, and the main components of haze are as follows: inhalable particles, SO2、NOXAnd the like. SO (SO)2As one of the main pollutants of haze, the haze mainly comes from the combustion of fossil fuel (such as steel, power generation, nonferrous metals, coking, building materials, heating, garbage incineration and the like are SO2Row enlarged users). Therefore, how to effectively control and reduce SO2Has become a hot problem of social concern, and researches on the high-efficiency and energy-saving SO removal2The discharge of (2) is imperative.
At present, in domestic circulating fluidized bed desulfurization systems, circulating materials are almost recycled by adopting air chutes, heaters, fluidized fans and other modes, and only the desulfurized fly ash collected by bag-type dust collectors is simply returned to a desulfurization tower, which is also a main problem of the circulating fluidized bed desulfurization system, because the desulfurized reaction products on the outer surface of the circulating fly ash cannot be stripped in a bed layer; the reason is as follows: 1) the bed layer is a main desulfurization reaction zone and a circulating ash accumulation zone, and is also a so-called circulating ash outer surface reaction product stripping zone; the area is a spraying area, circulating ash is in a wet state due to spraying, and wet materials are not strippable (the wet materials can only be deformed and cannot be stripped); 2) the energy of the ascending gas flow in the desulfurizing tower is not enough to strip the products on the surface of the desulfurizing agent (lime).
Desulfurizing agent (lime) and SO2The reaction is completed in two stages, namely: an initial stage and a product diffusion control stage. The desulfurization reaction rate was very fast at about 46% desulfurization rate in the first 0.3 seconds of the initial stage, and the reaction rate was high in the initial stage because the desulfurization reaction did not occur on the surface of lime. And the reaction is a surface reaction, which is a 0-level surface reaction, and the reaction rate is in a linear relation with the square of the surface area of the lime. The calcium sulfite (part of calcium sulfate) product generated in the initial stage covers the surface of unreacted lime, the molar volume of the calcium sulfite product generated in the initial stage is 2.72 times that of the lime, and the reaction product covers the outer surface of the unreacted lime to form a uniform reaction product layer, SO that micropore channels in lime particles are blocked, and SO (SO) generated in the subsequent reaction is enabled to be2Must diffuse through this reaction product layer to allow the desulfurization reaction with lime to take place. But do notThe solid phase diffusion resistance is so large that the reaction rate is significantly decreased and the product diffusion rate becomes a control step. Therefore, the second stage is a product diffusion control stage, which is also a desulfurization control stage, and is a cause of a low desulfurization reaction rate and a low lime utilization rate.
Therefore, in order to improve the desulfurization efficiency and the utilization rate of lime, a large amount of circulating ash is adopted to carry out circulating desulfurization reaction at the present stage, but the large amount of circulating ash in the bed layer not only increases the load of the rear bag type dust collector, so that the resistance of the desulfurization system is increased, the equipment is abraded, the established bed layer is extremely unstable, the bed layer is likely to collapse at any time, and the reliability of the desulfurization system is reduced.
From the above analysis, the main problems of the existing circulating fluidized bed semi-dry process are as follows: the reaction product covers the surface of the unreacted desulfurizer particles in the reaction process, reduces the contact area of the desulfurizer and the flue gas, and prevents SO2The reaction with the desulfurizing agent reduces the desulfurization reaction rate, prolongs the desulfurization reaction time, indirectly reduces the desulfurization efficiency and wastes a large amount of desulfurizing agent.
Disclosure of Invention
Technical problem to be solved
In order to solve the problems in the prior art, the invention provides a semidry flue gas desulfurization device and a desulfurization method.
(II) technical scheme
In order to achieve the purpose, the invention adopts the main technical scheme that:
the invention provides a semidry flue gas desulfurization device, which comprises a desulfurization section, a dust removal section and an outer discharge section, wherein the inlet of the desulfurization section is connected with an original flue gas outlet, the outlet of the desulfurization section is connected with the inlet of the dust removal section, the flue gas outlet of the dust removal section is connected with a chimney, and the lower ash outlet of the dust removal section is connected with the outer discharge section; the upper part of the circulating section is connected with an ash outlet at the lower part of the dust removal section; the circulating ash in the circulating section returns to the desulfurizing section after being activated.
According to the invention, the desulfurization section comprises a desulfurization tower, the lower part of the desulfurization tower is a raw flue gas inlet area, the middle part of the desulfurization tower is a desulfurization reaction area, and the upper part of the desulfurization tower is a reacted flue gas outlet area; the raw flue gas inlet area is connected with the outlet of the raw flue gas, the flue gas outlet area after reaction is connected with the dust removal section, and the desulfurization reaction area is respectively connected with the desulfurizer bin, the water tank and the activation device for circulating ash through pipelines.
According to the invention, the dust removal section is a bag type dust remover, an inlet of the bag type dust remover is connected with an outlet of the desulfurization section, a flue gas outlet of the bag type dust remover is connected with a chimney through a fan, and an ash outlet below the bag type dust remover is connected with the circulation section and the outward discharge section through a conveying device.
According to the invention, a layer of desulfurizer is arranged on the outer surface of the filter bag of the bag type dust collector and is used for carrying out desulfurization reaction with the unreacted flue gas in the desulfurization section.
According to the invention, the circulating section comprises a circulating ash bin and an activating device, the upper part of the circulating ash bin is connected with the dust removal section through a conveying device, the lower part of the circulating ash bin is connected with the activating device, and the activating device is connected with the desulfurization section through a pipeline.
According to the invention, the outlet of the circulating ash bin is provided with a quantitative conveying device, and the quantitative conveying device is connected with the activating device.
According to the invention, the activation device is a pulverizer, the inlet of the pulverizer is connected with the outlet of the circulating ash bin, and the outlet of the pulverizer is connected with the desulfurizing tower of the desulfurizing section.
The invention also provides a desulfurization method using the semidry flue gas desulfurization device, which specifically comprises the following steps:
1) a desulfurization section: raw flue gas enters from the bottom of the desulfurization tower, and in the tower, the raw flue gas is contacted with a desulfurizing agent in a fluidized state, and desulfurization reaction is completed under the action of water spray;
2) a dust removal section: conveying the flue gas reacted in the step 1) from the upper part of the desulfurizing tower to a bag type dust collector through a pipeline for dust removal, discharging the flue gas subjected to dust removal through a chimney by a fan, wherein one part of the desulfurized ash collected by the bag type dust collector enters an external discharge section to become external discharge ash, and the other part of the desulfurized ash enters a circulation section to become circulation ash;
3) a circulation section: and 2) the circulating ash entering the circulating section in the step 2) firstly enters a circulating ash bin, then enters an activating device through a quantitative conveying device for activation treatment, and the activated circulating ash returns to the desulfurizing tower for desulfurization reaction.
According to the invention, the activating device in the step 3) is a pulverizer, and the activating treatment is as follows: and grinding the circulating ash collected by the bag type dust collector by a pulverizer to reduce the particle size of the circulating ash from 150 meshes to 600-1000 meshes, and returning the ground circulating ash to the desulfurizing tower again.
According to the invention, the particle size of the circulating ash after being ground by the pulverizer is 800-900 meshes.
(III) advantageous effects
The invention has the beneficial effects that: according to the invention, by improving the activity of the circulating ash, the desulfurization efficiency of the semi-dry process is improved, the consumption of a desulfurizing agent is reduced, the circulating amount of the circulating ash is reduced, the resistance of a desulfurization system is reduced, and the power consumption is reduced; the operation load of the rear dust remover is reduced, and the service life of the dust remover is prolonged; and fundamentally avoids the occurrence of bed collapse phenomenon.
Drawings
FIG. 1 is a structural view of a semidry flue gas desulfurization apparatus according to the present invention.
[ description of reference ]
1: a desulfurizing tower; 2: a desulfurizer bin; 3: a quantitative conveying device; 4: a water tank; 5: a water pump; 6: a bag type dust collector; 7: a conveying device; 8: circulating an ash bin; 9: discharging the ash out of an ash bin; 10: an outer discharge conveyor; 11: an activation device; 12: a fan; 13: a chimney; 14: an original flue gas inlet pipeline.
Detailed Description
For the purpose of better explaining the present invention and to facilitate understanding, the present invention will be described in detail by way of specific embodiments with reference to the accompanying drawings. The described embodiments are only some embodiments of the invention, not all embodiments.
As shown in fig. 1, the invention provides a semidry flue gas desulfurization device, which comprises a desulfurization section, a dust removal section, an external discharge section and a circulation section, wherein the desulfurization section mainly comprises a desulfurization tower 1, the dust removal section is a bag type dust collector 6, the external discharge section comprises an external ash discharge bin 9, and the circulation section comprises a circulating ash bin 8 and an activation device 11. The lower part of the desulfurizing tower 1 is connected with an original flue gas inlet pipeline 14, and a desulfurizing reaction zone of the desulfurizing tower 1 is respectively connected with a desulfurizing agent bin 2, a water tank 4 and an activating device 11 through pipelines; the lower part of the desulfurizer bin 2 is provided with a quantitative conveying device 3, and the desulfurizer is conveyed into the desulfurizing tower 1 through the quantitative conveying device 3; a water pump 5 is arranged between the water tank 4 and the desulfurizing tower 1. The original flue gas in the desulfurizing tower 1 and a desulfurizing agent are subjected to a desulfurization reaction, the reacted flue gas is conveyed into a bag type dust collector 6 from the upper part of the desulfurizing tower 1 through a pipeline, and the flue gas subjected to dust collection is conveyed to a chimney 13 through a fan 12 to be discharged. And one part of the desulfurization ash collected by the bag-type dust collector 6 is conveyed to an external ash discharge bin 9 for external discharge treatment through a conveying device 7, and the other part of the desulfurization ash is conveyed to a circulating ash bin 8 for circulating reaction. An outer discharge conveyor 10 is arranged at the lower part of the outer ash discharge bin 9, and the outer ash discharge in the outer ash discharge bin 9 is discharged through the outer discharge conveyor 10. The lower part of the circulating ash bin 8 is provided with an activating device 11, the activating device 11 is a pulverizer, and circulating ash in the circulating ash bin 8 is pulverized by the pulverizer, so that the particle size of the circulating ash is reduced from about 150 meshes to 600-1000 meshes, and the preferable mesh number is 800-900 meshes. The grinded circulating ash returns to the desulfurizing tower 1 again for desulfurization reaction.
The conveying device 7 is used for conveying the desulfurized ash to the circulating ash bin 8 and the outer ash discharge bin 9.
In the process of grinding the circulating ash, on one hand, the particle diameter of the circulating ash is reduced, the specific surface area is increased, and on the other hand, a desulfurization reaction product generated in the desulfurization process is ground from the surface of the circulating ash, so that the activity of the desulfurization circulating ash is improved, the desulfurization reaction is changed from a product diffusion control stage to a 0-level surface reaction in an initial stage, and the effects of improving the desulfurization efficiency and the utilization rate of a desulfurizing agent are achieved.
Since the specific surface area of the circulating ash is increased, the reaction capacity is increased and the desulfurization efficiency is improved. Under the condition of the same desulfurization efficiency, the circulating amount of circulating ash can be reduced, the running resistance of the desulfurization tower is reduced, the running power consumption is reduced, the bed layer bed collapse phenomenon is fundamentally avoided, and the biggest hidden trouble of the semi-dry desulfurization of the circulating fluidized bed is solved. The running stability and feasibility of the device are improved. In addition, the circulation amount of circulating ash is reduced, the dust load entering the dust remover is reduced, and the service life of the filter bag is prolonged.
The desulfurization reaction principle of the invention is as follows:
Ca(OH)2+SO2＝CaSO3·1/2H2O+1/2H2O (1)
Ca(OH)2+SO3＝CaSO4·1/2H2O+1/2H2O (2)
CaSO3·1/2H2O+1/2O2＝CaSO4·1/2H2O (3)
Ca(OH)2+CO2＝CaCO3+H2O (4)
2Ca(OH)2+2HCl＝CaCl2·Ca(OH)2·2H2O (5)
Ca(OH)2+2HF＝CaF2+2H2O (6)
the invention also provides a semidry flue gas desulfurization method capable of improving the activity of circulating ash, the desulfurizer adopted by the invention is lime, the raw flue gas enters the desulfurizing tower 1, the flue gas in the desulfurizing tower 1 is contacted with the desulfurizer material in a fluidized state, and under the combined action of water spraying, temperature reduction, humidification and the like, wherein HF and SO3、SO2And the acidic pollutants and the desulfurizer are removed after reaction. Meanwhile, in the turbulent fluidized bed tower, fine dust particles and heavy metals (mercury, cadmium and other substances) in the flue gas are converged into thicker particles through coagulation, the particles enter the bag type dust collector 6 at the rear part through a pipeline, and because the outer surface of a filter bag of the bag type dust collector 6 adsorbs an unreacted desulfurizer dust layer, the flue gas is further reacted with the dust layer on the surface of the filter bag when being filtered by the filter bag, and the second desulfurization and gas-solid separation process is completed in the bag type dust collector 6. The purified flue gas is discharged from the bag filter 6.
The solid particles trapped by the bag filter 6 still contain partial incompletely reacted desulfurizer, and the surface of the incompletely reacted desulfurizer is coated with a layer of desulfurization reaction product, so that the desulfurization reaction rate is influenced. Therefore, a part of the desulfurizer particles which are not completely reacted and collected by the bag-type dust collector 6 are conveyed into the circulating ash bin 8 through the conveying device 7, and the other part of the desulfurizer particles are conveyed into the outer ash bin 9 through the conveying device 7. The desulfurizer particles which enter the circulating ash bin 8 and are not completely reacted are circulating ash, the circulating ash enters the activating device 11 through a star-shaped ash discharge valve at the bottom of the circulating ash bin 8, the activating device 11 is a pulverizer, and the pulverizer in the grinding process reduces the particle size of the circulating ash and increases the specific surface area on one hand, and strips the desulfurization reaction product generated in the desulfurization process from the surface of the circulating ash on the other hand, so that the reaction activity of the circulating ash is improved, and the effects of improving the desulfurization efficiency and the utilization rate of the desulfurizer are achieved. The equipment abrasion is reduced, and the operation cost is reduced.
The activated circulating ash returns to the desulfurizing tower 1 again to participate in the desulfurizing reaction, and the circulating is repeated for a plurality of times. And discharging a small amount of redundant circulating ash.
Example 1:
the main design technical parameters of a coke oven flue gas desulfurization process are as follows:
flue gas amount: 200000Nm3/h；
Inlet SO2Concentration: 300mg/m3；
Inlet flue gas temperature: 150 ℃ and 180 ℃;
outlet SO2Concentration: < 30mg/m3；
Outlet dust concentration: less than 10mg/m3；
Outlet flue gas temperature: 120 ℃ is adopted.
In the embodiment, a semi-dry flue gas desulfurization device is adopted for desulfurization, coke oven flue gas is introduced into a denitration device from a combustion chamber through an underground flue to be denitrated and then enters the desulfurization device, and lime in a desulfurization tower and SO in the flue gas2The reaction generates calcium sulfite and calcium sulfate, the flue gas after the reaction is introduced into a bag type dust collector through a pipeline, and the secondary desulfurization and gas-solid separation process is completed in the bag type dust collector. A part of the incompletely reacted desulfurizer captured by the bag type dust collector is conveyed into a circulating ash bin by a conveying device and is circulatedThe bottom of the annular ash bin is provided with the circulating ash activating device, circulating ash is activated by the activating device, on one hand, the particle size is reduced, the specific surface area is increased, and on the other hand, a desulfurization reaction product generated in the desulfurization process is stripped from the surface of the circulating ash, so that the reaction capacity of the circulating ash is improved, and the effects of improving the desulfurization efficiency and the utilization rate of a desulfurizing agent are achieved.
And returning the activated circulating ash to the desulfurizing tower again to participate in desulfurization reaction, and circulating for many times. And discharging the rest of the circulating ash.
By adopting the semi-dry desulfurization process, the main technical parameters of the desulfurization system are as follows:
Ca/S: less than 1.2 (original circulating fluidized bed desulfurization Ca/S: 1.6);
desulfurization degree: 97 percent;
outlet SO2Concentration: less than 10mg/m3；
Outlet dust concentration: less than 10mg/m3；
Resistance of the desulfurizing tower: less than 900Pa (resistance of the desulfurizing tower of the original circulating fluidized bed: 2000 Pa);
resistance of bag collector: < 1200 Pa;
resistance of a desulfurization system: < 2800Pa (resistance of the original circulating fluidized bed desulfurization system: 4000 Pa);
the power consumption is reduced: 142 KW/h;
the annual power consumption is reduced: 1243920KW/h (365 days);
reducing the lime amount: 26.9 Kg/h;
saving lime in years: 235.64 tons/year (365 days);
annual operating cost saving: electricity charge plus lime
1243920 × 0.8 yuan +235.64 × 550 yuan is 112.47 ten thousand yuan;
wherein: the electric charge is calculated according to 0.8 yuan, and the lime is calculated according to 550 yuan;
the service life of the filter bag is prolonged: and 8 months.
Example 2:
the main design technical parameters of a certain gas boiler are as follows:
flue gas amount: 2-160000Nm3/h；
Inlet SO2Concentration: < 300mg/m3；
Inlet flue gas temperature: 140-170 ℃;
outlet SO2Concentration: less than 20mg/m3；
Outlet dust concentration: less than 5mg/m3；
Outlet flue gas temperature: at 100 ℃.
In the embodiment, a semidry flue gas desulfurization device is adopted for desulfurization, flue gas enters the desulfurization device from a boiler induced draft fan, and lime in a desulfurization tower and SO in the original flue gas2The reaction generates calcium sulfite and calcium sulfate, the flue gas after the reaction is introduced into a bag type dust collector through a pipeline, and the secondary desulfurization and gas-solid separation process is completed in the bag type dust collector. A part of incompletely reacted desulfurizer collected by the bag type dust collector is conveyed into the circulating ash bin by the conveying device, the circulating ash activating device is arranged at the bottom of the circulating ash bin, and the circulating ash is activated by the activating device, so that the particle size is reduced, the specific surface area is increased, and a desulfurization reaction product generated in the desulfurization process is stripped from the surface of the circulating ash, so that the reaction capacity of the circulating ash is improved, and the effects of improving the desulfurization efficiency and the utilization rate of the desulfurizer are achieved.
And returning the activated circulating ash to the desulfurizing tower again to participate in desulfurization reaction, and circulating for many times. And discharging the rest of the circulating ash.
By adopting the semi-dry desulfurization process, the main technical parameters of the desulfurization system are as follows:
Ca/S: less than 1.2 (original circulating fluidized bed desulfurization Ca/S: 1.6);
desulfurization degree: 97 percent;
outlet SO2Concentration: less than 20mg/m3；
Outlet dust concentration: less than 5mg/m3；
Resistance of the desulfurizing tower: less than 900Pa (resistance of the desulfurizing tower of the original circulating fluidized bed: 2000 Pa);
resistance of bag collector: < 1200 Pa;
resistance of a desulfurization system: < 2700Pa (resistance of the original circulating fluidized bed desulfurization system: 4300 Pa);
the power consumption is reduced: 270 KW/h;
the annual power consumption is reduced: 1944000KW/h (300 days);
reducing the lime amount: 41.44 Kg/h;
saving lime in years: 298.368 tons/year (300 days);
annual operating cost saving: electricity charge plus lime
1944000 × 0.8 yuan +298.368 × 550 yuan ═ 171.93 ten thousand yuan;
wherein: the electric charge is calculated according to 0.8 yuan, and the lime is calculated according to 550 yuan;
the service life of the filter bag is prolonged: for 10 months.
It should be understood that the above description of specific embodiments of the present invention is only for the purpose of illustrating the technical lines and features of the present invention, and is intended to enable those skilled in the art to understand the contents of the present invention and to implement the present invention, but the present invention is not limited to the above specific embodiments. It is intended that all such changes and modifications as fall within the scope of the appended claims be embraced therein.
Claims (10)
1. A semidry flue gas desulfurization device comprises a desulfurization section, a dust removal section and an external discharge section, wherein an inlet of the desulfurization section is connected with an original flue gas outlet, an outlet of the desulfurization section is connected with an inlet of the dust removal section, a flue gas outlet of the dust removal section is connected with a chimney, and an ash outlet at the lower part of the dust removal section is connected with the external discharge section; the method is characterized in that:
the upper part of the circulating section is connected with an ash outlet at the lower part of the dust removal section;
the circulation section comprises a circulation ash bin and an activation device, the inlet of the activation device is connected with the circulation ash bin, and the outlet of the activation device is connected with the desulfurization section.
2. The semidry flue gas desulfurization device according to claim 1, wherein: the desulfurization section comprises a desulfurization tower, the lower part of the desulfurization tower is a raw flue gas inlet area, the middle part of the desulfurization tower is a desulfurization reaction area, and the upper part of the desulfurization tower is a reacted flue gas outlet area; the raw flue gas inlet area is connected with a raw flue gas inlet pipeline, the flue gas outlet area after reaction is connected with a dust removal section, and the desulfurization reaction area is respectively connected with a desulfurizer bin, a water tank and an activation device through pipelines.
3. The semidry flue gas desulfurization device according to claim 1, wherein: the dust removal section comprises a bag type dust remover, and an ash outlet at the lower part of the bag type dust remover is connected with the circulation section and the outer discharge section through a conveying device.
4. The semidry flue gas desulfurization device according to claim 3, wherein: and a layer of desulfurizer is arranged on the outer surface of the filter bag of the bag type dust collector and is used for carrying out desulfurization reaction with the unreacted flue gas in the desulfurization section.
5. The semidry flue gas desulfurization device according to claim 1, wherein: the upper part of the circulating ash bin is connected with the dust removal section through a conveying device, the lower part of the circulating ash bin is connected with an activating device, and the activating device is connected with the desulfurization section through a pipeline.
6. The semidry flue gas desulfurization device according to claim 5, wherein: and a quantitative conveying device is arranged at an outlet at the lower part of the circulating ash bin and is connected with the activating device.
7. The semidry flue gas desulfurization device according to claim 5, wherein: the activation device is a pulverizer, an inlet of the pulverizer is connected with an outlet of the circulating ash bin, and an outlet of the pulverizer is connected with a desulfurization tower of the desulfurization section.
8. A method for performing desulfurization by using the semidry flue gas desulfurization apparatus according to any one of claims 1 to 7, characterized in that: the method comprises the following steps:
1) a desulfurization section: raw flue gas enters from the bottom of the desulfurization tower, and in the tower, the raw flue gas is contacted with a desulfurizing agent in a fluidized state, and desulfurization reaction is completed under the action of water spray;
2) a dust removal section: conveying the flue gas reacted in the step 1) from the upper part of the desulfurizing tower to a bag type dust collector through a pipeline for dust removal, discharging the flue gas subjected to dust removal through a chimney by a fan, wherein one part of the desulfurized ash collected by the bag type dust collector enters an external discharge section to become external discharge ash, and the other part of the desulfurized ash enters a circulation section to become circulation ash;
3) a circulation section: and 2) the circulating ash entering the circulating section in the step 2) firstly enters a circulating ash bin, then enters an activating device through a quantitative conveying device for activation treatment, and the activated circulating ash returns to the desulfurizing tower for desulfurization reaction.
9. The method of claim 8, wherein: the activating device in the step 3) is a pulverizer, and the activating treatment is as follows: and grinding the circulating ash collected by the bag type dust collector by a pulverizer to reduce the particle size of the circulating ash from 150 meshes to 600-1000 meshes, and returning the ground circulating ash to the desulfurizing tower again.
10. The method of claim 9, wherein: the particle size of the circulating ash after being ground by the pulverizer is 800-900 meshes.
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