CN210057855U - Flue gas treatment system - Google Patents

Flue gas treatment system Download PDF

Info

Publication number
CN210057855U
CN210057855U CN201821808900.9U CN201821808900U CN210057855U CN 210057855 U CN210057855 U CN 210057855U CN 201821808900 U CN201821808900 U CN 201821808900U CN 210057855 U CN210057855 U CN 210057855U
Authority
CN
China
Prior art keywords
flue gas
denitration
dust
desulfurization
treated
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201821808900.9U
Other languages
Chinese (zh)
Inventor
不公告发明人
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Zhongneng Rongtai energy and Environmental Protection Technology Co.,Ltd.
Original Assignee
Beijing Zhongneng Nuotai Energy Saving And Environmental Protection Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Beijing Zhongneng Nuotai Energy Saving And Environmental Protection Co ltd filed Critical Beijing Zhongneng Nuotai Energy Saving And Environmental Protection Co ltd
Priority to CN201821808900.9U priority Critical patent/CN210057855U/en
Application granted granted Critical
Publication of CN210057855U publication Critical patent/CN210057855U/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/10Biofuels, e.g. bio-diesel
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/30Fuel from waste, e.g. synthetic alcohol or diesel

Abstract

The embodiment of the utility model provides a flue gas processing system. The flue gas treatment system comprises a denitration treatment unit, the denitration treatment unit comprises a reaction tower and an adsorbent catalytic denitration structure, and the adsorbent catalytic denitration structure is arranged in the reaction tower, so that a denitration reducing agent entering the reaction tower and nitride in the flue gas to be treated react and denitrate under the catalysis of the adsorbent catalytic denitration structure. The flue gas treatment system has good flue gas treatment effect.

Description

Flue gas treatment system
Technical Field
The embodiment of the utility model provides a relate to environmental protection equipment technical field, especially relate to a flue gas processing system.
Background
At present, domestic garbage treatment adopts an incineration reduction and energy regeneration mode, which is a great trend. The garbage incineration can reduce the pollution of garbage stacking to the environment to the maximum extent, and meanwhile, the power generation can be realized to realize energy regeneration. However, the flue gas generated in the incineration process still contains substances which are still harmful to the environment, such as sulfur dioxide (sulfur for short), nitrogen oxide (nitrate for short), dust, dioxin and the like, and further treatment of the incineration flue gas, desulfurization and denitrification and the like are needed to avoid the direct emission of the incineration flue gas and harm the environment.
In the prior art, when denitration treatment is performed on waste incineration flue gas, an SCR (selective catalytic reduction denitration) process is mainly adopted, and the method is a denitration method after a furnace, and mainly utilizes the principle that a reducing agent (NH3) selectively reacts with NOx to generate N2 and H2O under the action of a metal catalyst instead of being oxidized by O2.
Most of the existing SCR denitration systems adopt high-temperature catalysis, and the reaction temperature range is 315-400 ℃. The temperature of flue gas after waste incineration in the prior art reaching the SCR denitration system is usually lower than a reaction temperature, and in order to ensure that the temperature can be in a reaction temperature range during SCR denitration, an SGH (steam generator) device needs to be arranged in front of the SCR denitration system to reheat the flue gas, so that the temperature of the flue gas can be raised to a proper reaction temperature. The heating of flue gas by SGH requires the consumption of a large amount of steam, so that the running cost is high. When the SCR is used for denitration, the catalyst is easy to be poisoned and lose efficacy, the service life is short, and the catalyst needs to be treated according to danger waste after the service life is over, so that the operation cost is further increased.
SUMMERY OF THE UTILITY MODEL
In view of this, the embodiment of the present invention provides a flue gas treatment system to solve some or all of the above problems.
According to the utility model discloses in the first aspect of the embodiment, a flue gas processing system is provided, and it includes the denitration processing unit, and the denitration processing unit includes reaction tower and adsorbent catalysis denitration structure, and adsorbent catalysis denitration structure sets up in the reaction tower, makes the nitride in the denitration reductant in the entering reaction tower and the flue gas of pending react and the denitration under the catalysis of adsorbent catalysis denitration structure.
Optionally, the flue gas treatment system further comprises a granulator, which is connected with the reaction tower and produces the dust conveyed by the reaction tower into fuel particles.
Optionally, the flue gas treatment system further includes a dust remover, and the dust remover is located at the front end of the denitration treatment unit along the flow direction of the flue gas to be treated, so as to perform dust removal treatment on the flue gas to be treated before the denitration treatment unit.
Optionally, the granulator is connected with a dust remover, and dust conveyed by the dust remover is manufactured into fuel particles; or the granulator is respectively connected with the reaction tower and the dust remover of the denitration treatment unit, and the dust conveyed by the reaction tower and the dust remover is made into fuel particles.
Optionally, the flue gas treatment system further comprises a pre-denitration unit, and the pre-denitration unit is located at the front end of the dust remover along the flow direction of the flue gas to be treated and performs pre-denitration treatment on the flue gas to be treated.
Optionally, the flue gas treatment system further comprises a desulfurization treatment unit, the desulfurization treatment unit is positioned at the front end of the dust remover along the flow direction of the flue gas to be treated, and is used for performing desulfurization treatment on the flue gas to be treated; or the desulfurization treatment unit is positioned at the front end of the denitration treatment unit and is used for performing desulfurization treatment on the flue gas to be treated before entering the denitration treatment unit.
Optionally, the desulfurization treatment unit comprises a desulfurization tower and an absorption slurry spraying structure, the absorption slurry spraying structure is arranged in the desulfurization tower and sprays absorption slurry into the desulfurization tower, and the flue gas to be treated enters the desulfurization tower to contact with the sprayed absorption slurry and reacts for desulfurization.
Optionally, the denitration treatment unit further comprises a reducing agent conveying part, and the reducing agent conveying part is connected with the reaction tower and conveys the denitration reducing agent into the reaction tower.
Alternatively, the denitration reducing agent includes NH3 gas, the reducing agent delivery section includes an NH3 delivery source, an air source, and a mixer that is connected to the NH3 delivery source and the air source, respectively, and mixes the NH3 gas and the air within the mixer.
Optionally, a heater is further disposed between the air source and the mixer, and the heater heats the gas input by the air source.
Optionally, the sorbent catalytic denitration structure comprises an active coke catalytic denitration structure.
According to the utility model discloses a second aspect provides a flue gas processing system, including flue gas purification portion and the granulator of being connected with flue gas purification portion, flue gas purification portion carries out desulfurization treatment, denitration treatment and dust removal treatment to the flue gas of handling and handles at least one in, and the granulator acquires the dust of flue gas purification portion output to with dust generation fuel granule.
Optionally, the flue gas cleaning section comprises: the denitration treatment unit comprises a reaction tower and an adsorbent catalytic denitration structure arranged in the reaction, the adsorbent catalytic denitration structure enables a denitration reducing agent entering the reaction tower and nitrides in the to-be-treated flue gas to react and denitrate under the catalysis of the adsorbent catalytic denitration structure, the granulator is connected with the reaction tower, and dust conveyed by the reaction tower is made into fuel particles.
Optionally, the flue gas purification part comprises a dust remover, the dust remover is positioned at the front end of the denitration treatment unit along the flow direction of the flue gas to be treated so as to remove dust from the flue gas to be treated before the denitration treatment unit, and the granulator is connected with the dust remover and produces the dust conveyed by the dust remover into fuel particles.
Alternatively, when the flue gas cleaning section includes a denitration treatment unit and a dust remover, the pelletizer is connected to the reaction tower of the denitration treatment unit and the dust remover, respectively, and manufactures dust conveyed by the reaction tower and the dust remover into fuel particles.
Optionally, the flue gas purification part further comprises a pre-denitration unit, the pre-denitration unit is positioned at the front end of the dust remover along the flow direction of the flue gas to be treated, and the pre-denitration unit is used for performing pre-denitration treatment on the flue gas to be treated.
Optionally, the flue gas treatment system further includes a desulfurization treatment unit, and the desulfurization treatment unit is located at the front end of the dust remover along the flow direction of the flue gas to be treated and performs desulfurization treatment on the flue gas to be treated.
Optionally, the desulfurization treatment unit comprises a desulfurization tower and an absorption slurry spraying structure, the absorption slurry spraying structure is arranged in the desulfurization tower and sprays absorption slurry into the desulfurization tower, and the flue gas to be treated enters the desulfurization tower to contact with the sprayed absorption slurry and reacts for desulfurization.
Optionally, the denitration treatment unit further comprises a reducing agent conveying part, and the reducing agent conveying part is connected with the reaction tower and conveys the denitration reducing agent into the reaction tower.
Alternatively, the denitration reducing agent includes NH3 gas, the reducing agent delivery section includes an NH3 delivery source, an air source, and a mixer that is connected to the NH3 delivery source and the air source, respectively, and mixes the NH3 gas and the air within the mixer.
Optionally, a heater is further disposed between the air source and the mixer, and the heater heats the gas input by the air source.
Optionally, the sorbent catalytic denitration structure comprises an active coke catalytic denitration structure.
According to the embodiment of the utility model provides a flue gas treatment system, this flue gas treatment system include denitration treatment unit, are provided with adsorbent catalytic denitration structure in denitration treatment unit's the reaction tower, utilize harmful substance such as nitride in the catalytic action, denitration action and the adsorption cooperation denitration reductant desorption pending flue gas of adsorbent catalytic denitration structure, realize the processing of the flue gas of handling. Denitration treatment is carried out through the adsorbent catalytic denitration structure, and the problem that a metal catalyst subjected to SCR denitration treatment is easy to poison and lose efficacy is solved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments described in the embodiments of the present invention, and other drawings can be obtained by those skilled in the art according to the drawings.
Fig. 1 is a schematic process flow diagram of a flue gas treatment system according to an embodiment of the present invention.
Fig. 2 is a schematic structural diagram of a desulfurization treatment unit of a flue gas treatment system according to an embodiment of the present invention.
Fig. 3 is a schematic structural diagram of a denitration processing unit of a flue gas processing system according to the utility model.
Description of reference numerals:
10. a pre-denitration unit; 20. a desulfurization treatment unit; 21. a desulfurizing tower; 22. a slurry absorption spray structure; 23. a slurry delivery structure; 24. a demisting and dedusting structure; 25. a slurry space; 30. a dust remover; 40. an induced draft fan; 50. a denitration treatment unit; 51. a main fan; 52. an air source; 53. a booster fan; 54. a reaction tower; 55. a mixer; 56. a heater; 57. an air pump; 60. and (4) a granulator.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the embodiments of the present invention, the technical solution of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person having ordinary skill in the art should belong to the scope protected by the embodiments of the present invention.
The embodiment of the present invention will be further described with reference to the accompanying drawings.
As shown in fig. 1, according to the utility model discloses an embodiment, flue gas processing system includes denitration processing unit 50, and denitration processing unit 50 includes reaction tower 54 and adsorbent catalysis denitration structure, and adsorbent catalysis denitration structure sets up in reaction tower 54, and the nitride in the denitration reductant in the entering reaction tower 54 and the flue gas of treating is reacted and is denitrated under the catalysis of adsorbent catalysis denitration structure.
This flue gas processing system includes denitration processing unit 50, is provided with adsorbent catalysis denitration structure in denitration processing unit 50's the reaction tower 54, utilizes the catalytic action of adsorbent catalysis denitration structure, denitration effect and adsorption cooperation denitration reductant desorption to treat harmful substance such as nitride in the flue gas, realizes the processing of the flue gas of treating. Denitration treatment is carried out through the adsorbent catalytic denitration structure, and the problem that a metal catalyst subjected to SCR denitration treatment is easy to poison and lose efficacy is solved.
Optionally, in this embodiment, the adsorbent catalytic denitration structure is an active coke catalytic denitration structure. The denitration reducing agent may be NH3 gas and/or ammonia water, and the NH3 gas and/or ammonia water may be sprayed into the absorption tower 54 to react.
Because the reaction temperature interval of the active coke denitration is 60-150 ℃, compared with the existing SCR denitration treatment which needs the reaction temperature of more than 300 ℃, the reaction temperature of the active coke for denitration treatment is low, and the flue gas to be treated does not need to be reheated during the reaction, so that the flue gas treatment system does not need to be provided with a reheating device (SGH device) for heating the flue gas to be treated, the heating steam is saved, and the equipment cost is reduced.
In addition, the active coke has a strong dioxin adsorption function, so that the catalytic denitration by using the active coke can adsorb dioxin without spraying active carbon powder, and the process and the cost in the flue gas treatment process are reduced.
As shown in fig. 1, in this embodiment, the flue gas treatment system is used for flue gas treatment after waste incineration. Of course, in other embodiments, the system may be applied to other application scenarios requiring gas treatment.
To burning the flue gas and handling the scene, the utility model discloses a flue gas processing system of embodiment still includes granulator 60, and granulator 60 is connected with reaction tower 54 to make the dust that reaction tower 54 carried for the fuel granule. The scraps and the like generated during the reaction of the active coke can be produced into fuel particles by the pelletizer 60 and burned again as fuel, so that the dioxin adsorbed and adhered thereon can be treated without polluting the environment and the treatment cost is lower.
Optionally, the flue gas treatment system further comprises a dust remover 30, and the dust remover 30 is located at the front end of the denitration treatment unit 50 along the flow direction of the flue gas to be treated, so as to perform dust removal treatment on the flue gas to be treated before the denitration treatment unit 50. The dust remover 30 can be used for removing dust particles and the like in the flue gas to be treated, and the dust and the like are prevented from entering the denitration treatment unit 50 along with the flue gas to be treated, so that the dust blocks the active coke catalytic denitration structure.
When the flue gas treatment system includes the dust separator 30, the granulator 60 may be connected to the dust separator 30 and produce the dust conveyed by the dust separator 30 into fuel particles. The fuel particles can be used as fuel for combustion, so that the fly ash discharge treatment is not needed to be carried out on the dust collected by the dust remover 30, the working procedure is saved, and the environmental pollution is avoided.
Alternatively, the pelletizer 60 may be connected to the reaction tower 54 and the dust remover 30, respectively, and manufactures the dust conveyed by the reaction tower 54 and the dust remover 30 into fuel pellets. Thus, the fly ash of the dust remover 30 and dust, scraps and the like generated in the operation process of the active coke are made into particles through a granulation technology, and then the particles are returned to the garbage incinerator for burning again, so that dioxin adsorbed in the particles is thoroughly eliminated, the fly ash is not generated in the whole process and is discharged outside, and the environment protection is facilitated.
Optionally, in this embodiment, the flue gas treatment system further includes at least one of the pre-denitration unit 10, the desulfurization treatment unit 20, and the induced draft fan 40 according to the flue gas treatment requirement.
For example, in the present embodiment, the flue gas treatment system includes a pre-denitration unit 10, a desulfurization treatment unit 20, a dust collector 30, an induced draft fan 40, and a denitration treatment unit 50, which are sequentially arranged along the flow direction of the flue gas to be treated. Therefore, the flue gas to be treated can be fully treated, the cleanliness of the discharged gas is ensured, and the environmental pollution is avoided.
Of course, the flue gas treatment system of this embodiment is only used as a preferred mode, and in other embodiments, one or more units in the flue gas treatment system may be reduced, omitted, or replaced as needed, which is not limited in this embodiment.
The following describes each unit of the flue gas treatment system of the present embodiment in detail:
specifically, the pre-denitration unit 10 is used for pre-denitration treatment of flue gas to be treated, and the pre-denitration unit 10 may include an SNCR (selective non-catalytic) denitration treatment unit. It is a denitration treatment unit in the stove, can set up in burning furnace to carry out the preliminary denitration treatment in the stove to the flue gas after burning. For example, a reducing agent (such as ammonia water, urea solution, etc.) is sprayed into the furnace in a proper temperature range, and the denitration treatment is realized by utilizing the principle that the reducing agent and NOx in the flue gas are reduced and removed and are converted into nitrogen, water, etc.
According to the requirement, the flue gas to be treated discharged after passing through the pre-denitration unit 10 can flow into the desulfurization treatment unit 20, so as to perform desulfurization treatment on the flue gas to be treated in the desulfurization treatment unit 20, and remove sulfide (SOx) in the flue gas to be treated.
Of course, the flue gas treatment system may only include the denitration treatment unit 50 and the desulfurization treatment unit 20, and along the flow direction of the flue gas to be treated, the desulfurization treatment unit (20) is located at the front end of the denitration treatment unit (50), and performs desulfurization treatment on the flue gas to be treated before entering the denitration treatment unit (50), SO that the problems that when denitration is performed by using activated coke, if the flue gas to be treated contains a large amount of SO2, the SO2 reacts with injected ammonia to generate ammonium salts such as ammonium bisulfate, ammonium sulfate and ammonium sulfite, and due to the fact that the generated ammonium salts have great viscosity, equipment blockage, resistance increase, efficiency decrease and the system cannot be operated in severe cases can be solved.
By arranging the desulfurization treatment unit 20 before the denitration treatment unit 50, the problem is solved, and the requirements of desulfurization and denitration of the flue gas to be treated are met.
The desulfurization processing unit 20 may select different desulfurization processes such as wet desulfurization (including ammonia process, limestone wet process, magnesium process, sodium process, etc.), dry desulfurization, etc., which is not limited in this embodiment.
Different desulfurization treatment units can be arranged according to different requirements, such as different occupied space, different equipment cost and the like. In the present embodiment, there is provided a desulfurization treatment unit 20 including a desulfurization tower 21, an absorption slurry spray structure 22, and the like.
As shown in fig. 2, the desulfurization tower 21 provides a reaction space for desulfurization treatment. The bottom of the desulfurization tower 21 is a slurry space 25 in which the absorption slurry is placed. The absorption slurry spraying structure 22 is arranged in the desulfurization tower 21 and sprays absorption slurry into the desulfurization tower 21, so that the flue gas to be treated enters the desulfurization tower (21) to contact with the sprayed absorption slurry and react for desulfurization.
Optionally, the desulfurization treatment unit 20 further includes a slurry transport structure 23 that is connected to the absorption slurry spray structure 22 and transports the absorption slurry in the slurry space 25 into the absorption slurry spray structure 22 so that the absorption slurry spray structure 22 can spray the absorption slurry.
The absorption slurry may be a slurry of limestone or lime, or the like.
The absorbent slurry spray structure 22 may be one or more as desired. When the absorbing slurry spraying structure 22 is plural, the slurry transport structure 23 is connected to one or more of the plural absorbing slurry spraying structures 22, respectively, and transports the absorbing slurry thereto.
Optionally, a demisting and dedusting structure 24 may be further disposed in the desulfurizing tower 21, and is configured to perform dedusting and demisting treatment on the desulfurized flue gas to be treated, so as to remove at least a part of dust and mist droplets.
Alternatively, the mist and dust removing structure 24 may be a cyclonic wet electrostatic precipitation mist removal structure.
The flue gas to be treated after the desulfurization treatment flows out from the desulfurization treatment unit 20 enters the dust remover 30 for dust removal. In this embodiment, the dust collector 30 may be a bag-type dust collector, and the bag-type dust collector is used to filter the flue gas to be processed, so that dust and the like are left in the bag-type dust collector, and the gas passes through the dust collector 30.
The bag-type dust collector can be internally provided with activated carbon for adsorption, or can be not provided with activated carbon for adsorption.
The dust collector 30 may be other wet or dry dust collectors, such as an electrostatic dust collector, a wet cyclone dust collector, etc., according to different requirements.
The induced draft fan 40 provides power for the flow of the flue gas to be treated, and the flue gas is forced to flow. The induced draft fan 40 may be a centrifugal fan, an axial flow fan, or the like. The induced draft fan 40 may be disposed at any suitable position according to the necessity, and is not necessarily disposed between the dust separator 30 and the denitration treatment unit 50, and may be disposed before the dust separator 30.
The flue gas to be treated flowing out of the dust collector 30 enters the denitration treatment unit 50 for denitration treatment.
As shown in fig. 3, a main blower 51 and a booster blower 53 are connected to an air inlet of the reaction tower 54 of the denitration treatment unit 50 to introduce the flue gas to be treated into the reaction tower 54. The induced draft fan 40 may be provided or the induced draft fan 40 may be omitted depending on the power of the main fan 51 and the booster fan 53. For example, if the power of the main blower 51 and the booster blower 53 is sufficiently large, the induced draft fan 40 may be omitted.
An air source inlet branch is also connected between the main fan 51 and the booster fan 53 and used for supplementing air to the flue gas to be treated. The air source intake branch is connected to an air source 52.
As shown in fig. 3, in this embodiment, when the denitration reducing agent includes NH3 gas, the denitration processing unit 50 further includes a reducing agent delivery unit, which is connected to the reaction tower 54 and delivers NH3 gas into the reaction tower 54, so that the NH3 gas reacts with the nitride and the like in the flue gas to be processed at the adsorbent catalytic denitration structure in the reaction tower 54, and is converted into nitrogen, water and the like.
In the present embodiment, the reducing agent supply unit includes an NH3 supply source, an air source, and a mixer 55, and the mixer 55 is configured to mix NH3 gas supplied from the NH3 supply source with air in an appropriate ratio and supply the mixture into the reaction tower 54 to perform a denitration reaction. The mixer 55 is connected to a NH3 delivery source and an air source, respectively, and mixes the incoming NH3 gas with the incoming air within the mixer 55.
An air pump 57 is provided between the mixer 55 and the air source for feeding air into the mixer 55.
Optionally, in order to make the temperature of the NH3 gas appropriate and ensure that the temperature of the denitration reaction is appropriate, a heater 56 is further provided between the air pump 57 and the mixer 55, and the heater 56 is used for heating the air. The heated air is further mixed with NH3 gas supplied from an NH3 supply source in the mixer 55, thereby ensuring the temperature of the mixed NH3 gas.
The denitration principle by using NH3 gas and active coke is as follows:
the active coke has more macropores (the diameter is more than 50nm), mesopores (the diameter is 2.0-50 nm) and fewer micropores (the diameter is less than 2nm), and pores exist in the active coke in a coherent form, so that the active coke has better structural strength, is not easy to break and has longer service life.
The active coke has two action mechanisms when adsorbing pollutants, one is physical adsorption and the other is chemical adsorption.
The physical adsorption depends on the characteristic of large specific surface area of the active coke, the pollutants in the flue gas to be treated are trapped in the active coke, and the pollutant molecules are limited in the active coke by utilizing the characteristic that the sizes of micropores and molecular radii are equivalent. For example, dioxin is adsorbed by active coke.
The chemical adsorption depends on C atoms with defects on crystal lattices, oxygen-containing functional groups and polar surface oxides on the surface of the active coke, and by utilizing the chemical characteristics of the C atoms, the oxygen-containing functional groups and the polar surface oxides, pollutants are fixed on the inner surface of the active coke in a targeted manner to play a catalytic role.
Specifically, after NOx in the flue gas to be treated is adsorbed by the active coke, the NOx and surrounding H2O and O2 generate adsorbed HNO2 under the catalytic action of the active coke, and the adsorbed HNO reacts with introduced NH3 to generate NH4NO 2. NH4NO2 is unstable in chemical property and is easily decomposed into N2 and H2O under the catalytic action of active coke, so that the aim of denitration is fulfilled.
The denitration reaction by using the activated coke comprises the following steps:
2NO+2NH3+O2→2N2+3H2O
non-SCR (direct reaction with reducing substance formed at the time of desorption)
NO+C…Red→N2C-Red is on the surface of active carbonReduced matter
The denitration efficiency of catalytic denitration by using the activated coke can reach 90%, so that the denitration treatment unit 50 and the pre-denitration unit 10 can ensure the denitration rate close to 100% and the denitration effect.
In conclusion, the flue gas treatment system can adapt to denitration of complex gases, adopts the active coke to catalyze denitration, has small sensitivity and high mechanical strength of the active coke, is suitable for catalyst carriers, has stable chemical performance and simple regeneration conditions, and can effectively adsorb harmful substances in the flue gas to be treated.
The problems that the activated carbon has more micropores, huge micropores are basically and directly communicated with the surface, the mechanical strength is low, and the activated carbon is easy to break are solved, and the problem that the actual utilization rate of the pores is low due to the fact that broken activated carbon powder easily blocks the pores is further avoided. Because the activated carbon is not used, the problems of serious crushing condition and high loss rate in the regeneration of the activated carbon can be avoided.
In addition, the denitration temperature of the flue gas treatment system is low, the temperature of 80-110 ℃ is an optimal reaction temperature range, the energy consumption is low, steam heating is not needed in the operation process, and the problem of high energy consumption caused by the fact that the low-temperature SCR denitration operation temperature generally reaches 200 ℃ is solved.
In the process route, the denitration treatment unit 50 is installed after the desulfurization treatment unit 20, and only denitration is performed, and the loss of active coke is small.
The flue gas temperature is higher after the denitration of the active coke, and no white smoke is discharged.
The active coke has the functions of dedusting and removing dioxin, has a further purification function on clean flue gas to be treated, does not need to be provided with an active carbon injection system, and saves the cost.
The active coke is a non-hazardous product, if the catalytic function is finally lost, the active coke can be used as fuel for combustion, so that the operation cost is low, the daily denitration is only the consumption of ammonia gas, and no byproduct is generated in the denitration process and water is not consumed.
The granulating machine is used for granulating, so that the whole process has no discharge of fly ash and no secondary pollution.
And (3) utilizing a granulator to granulate the fly ash, collecting the flue gas fly ash collected by the bag-type dust collector and the dust generated by the active coke in the operation process, and then conveying the collected flue gas fly ash and the dust to the granulator to change the fine dust into granules. The granular substances enter an incinerator again to be burnt to remove dioxin contained in the granular substances, so that the granular substances have no toxicity. Meanwhile, granulation can prevent the fly ash from being changed into fly ash again in the combustion process and entering a flue gas system to form dead circulation. Combustible particles generated by fly ash granulation enter the furnace slag after being re-combusted, and can be comprehensively utilized as building materials.
Utilize this flue gas processing system to get rid of the solid particle dust, nitride (NOx), sulphide (SOx) and dioxin etc. that contain effectively in the flue gas that produces after the msw incineration, owing to utilize the burnt catalytic denitration of activity to handle behind the sack cleaner, its reaction temperature is lower for the flue gas temperature that the sack cleaner discharged just satisfies the burnt denitration technology needs of activity, consequently can need not to use flue gas reheating equipment (SGH), has saved equipment cost.
According to the utility model discloses an on the other hand provides a flue gas processing system, its include flue gas purification portion and with granulator (60) that flue gas purification portion connects, flue gas purification portion carries out desulfurization treatment, denitration treatment and dust removal treatment in at least one processing to the flue gas of handling, granulator (60) acquire the dust of flue gas purification portion output, and will the dust generates the fuel granule.
This flue gas processing system includes gas cleaning portion and granulator 60, and gas cleaning portion can carry out purification treatment to the flue gas of handling, guarantees to satisfy the emission demand, avoids or reduces the influence to the environment. The fly ash, dust and the like collected and/or generated by the flue gas purification part in the flue gas treatment process can be manufactured into fuel particles by utilizing the granulator 60, the fuel particles can be used as fuel for repeated combustion, and the waste after combustion can be treated along with the furnace ash, so that the fly ash discharge treatment process is avoided, the treatment process is reduced, and the flue gas treatment cost is reduced.
Optionally, in this embodiment, the flue gas treatment system further includes a denitration treatment unit 50, where the denitration treatment unit 50 includes a reaction tower 54 and an adsorbent catalytic denitration structure, the adsorbent catalytic denitration structure is disposed in the reaction tower 54, and the denitration reducing agent entering the reaction tower 54 and the nitride in the flue gas to be treated react and denitrate under the catalysis of the adsorbent catalytic denitration structure.
The denitration treatment unit 50 is used for performing denitration treatment on flue gas to eliminate nitride (NOx) in the flue gas and avoid environmental pollution, and harmful substances such as nitride in the flue gas to be treated are removed by utilizing the catalytic action, the denitration action and the adsorption action of the adsorbent catalytic denitration structure, so that the treatment of the flue gas to be treated is realized. Denitration treatment is carried out through the adsorbent catalytic denitration structure, and the problem that a metal catalyst subjected to SCR denitration treatment is easy to poison and lose efficacy is solved.
In this embodiment, the adsorbent catalytic denitration structure is an active coke catalytic denitration structure. The denitration reducing agent may be NH3 gas and/or ammonia water, and the NH3 gas and/or ammonia water may be sprayed into the absorption tower 54 to react.
Because the reaction temperature interval of the active coke denitration is 60-150 ℃, compared with the existing SCR denitration treatment which needs the reaction temperature of more than 300 ℃, the reaction temperature of the active coke for denitration treatment is low, and the flue gas to be treated does not need to be reheated during the reaction, so that the flue gas treatment system does not need to be provided with a reheating device (SGH device) for heating the flue gas to be treated, the heating steam is saved, and the equipment cost is reduced.
In addition, the active coke has a strong dioxin adsorption function, so that the catalytic denitration by using the active coke can adsorb dioxin without spraying active carbon powder, and the process and the cost in the flue gas treatment process are reduced.
As shown in fig. 1, in this embodiment, the flue gas treatment system is used for flue gas treatment after waste incineration. Of course, in other embodiments, the system may be applied to other application scenarios requiring gas treatment.
To burning the flue gas and handling the scene, the granulator 60 of the embodiment of the present invention is connected with the reaction tower 54 to make the dust that the reaction tower 54 carried into fuel particles. The scraps and the like generated during the reaction of the active coke can be produced into fuel particles by the pelletizer 60 and burned again as fuel, so that the dioxin adsorbed and adhered thereon can be treated without polluting the environment and the treatment cost is lower.
Optionally, the flue gas treatment system further comprises a dust remover 30, and the dust remover 30 is located at the front end of the denitration treatment unit 50 along the flow direction of the flue gas to be treated, so as to perform dust removal treatment on the flue gas to be treated before the denitration treatment unit 50. The dust remover 30 can be used for removing dust particles and the like in the flue gas to be treated, and the dust and the like are prevented from entering the denitration treatment unit 50 along with the flue gas to be treated, so that the dust blocks the active coke catalytic denitration structure.
When the flue gas treatment system includes the dust separator 30, the granulator 60 may be connected to the dust separator 30 and produce the dust conveyed by the dust separator 30 into fuel particles. The fuel particles can be used as fuel for combustion, so that the fly ash discharge treatment is not needed to be carried out on the dust collected by the dust remover 30, the working procedure is saved, and the environmental pollution is avoided.
Alternatively, the pelletizer 60 may be connected to the reaction tower 54 and the dust remover 30, respectively, and manufactures the dust conveyed by the reaction tower 54 and the dust remover 30 into fuel pellets. Thus, the fly ash of the dust remover 30 and dust, scraps and the like generated in the operation process of the active coke are made into particles through a granulation technology, and then the particles are returned to the garbage incinerator for burning again, so that dioxin adsorbed in the particles is thoroughly eliminated, the fly ash is not generated in the whole process and is discharged outside, and the environment protection is facilitated.
Optionally, in this embodiment, the flue gas treatment system further includes at least one of the pre-denitration unit 10, the desulfurization treatment unit 20, and the induced draft fan 40 according to the flue gas treatment requirement.
For example, in the present embodiment, the flue gas treatment system includes a pre-denitration unit 10, a desulfurization treatment unit 20, a dust collector 30, an induced draft fan 40, and a denitration treatment unit 50, which are sequentially arranged along the flow direction of the flue gas to be treated. Therefore, the flue gas to be treated can be fully treated, the cleanliness of the discharged gas is ensured, and the environmental pollution is avoided.
Of course, the flue gas treatment system of this embodiment is only used as a preferred mode, and in other embodiments, one or more units in the flue gas treatment system may be reduced, omitted, or replaced as needed, which is not limited in this embodiment.
The following describes each unit of the flue gas treatment system of the present embodiment in detail:
specifically, the pre-denitration unit 10 is used for pre-denitration treatment of flue gas to be treated, and the pre-denitration unit 10 may include an SNCR (selective non-catalytic) denitration treatment unit. It is a denitration treatment unit in the stove, can set up in burning furnace to carry out the preliminary denitration treatment in the stove to the flue gas after burning. For example, a reducing agent (such as ammonia water, urea solution, etc.) is sprayed into the furnace in a proper temperature range, and the denitration treatment is realized by utilizing the principle that the reducing agent and NOx in the flue gas are reduced and removed and are converted into nitrogen, water, etc.
According to the requirement, the flue gas to be treated discharged after passing through the pre-denitration unit 10 can flow into the desulfurization treatment unit 20, so as to perform desulfurization treatment on the flue gas to be treated in the desulfurization treatment unit 20, and remove sulfide (SOx) in the flue gas to be treated.
Certainly, the flue gas treatment system may only include the denitration treatment unit 50 and the desulfurization treatment unit 20, and along the flow direction of the flue gas to be treated, the desulfurization treatment unit 20 is located at the front end of the denitration treatment unit 50, and performs desulfurization treatment on the flue gas to be treated before entering the denitration treatment unit 50, SO that the problem that when denitration is performed by using activated coke, if the flue gas to be treated contains a large amount of SO2, the SO2 reacts with the injected ammonia to generate ammonium salts such as ammonium bisulfate, ammonium sulfate, ammonium sulfite and the like, and due to the fact that the generated ammonium salts have great viscosity, equipment blockage, resistance increase, efficiency decrease and the system cannot be operated in severe cases can be solved.
By arranging the desulfurization treatment unit 20 before the denitration treatment unit 50, the problem is solved, and the requirements of desulfurization and denitration of the flue gas to be treated are met.
The desulfurization processing unit 20 may select different desulfurization processes such as wet desulfurization (including ammonia process, limestone wet process, magnesium process, sodium process, etc.), dry desulfurization, etc., which is not limited in this embodiment.
Different desulfurization treatment units can be arranged according to different requirements, such as different occupied space, different equipment cost and the like. In the present embodiment, there is provided a desulfurization treatment unit 20 including a desulfurization tower 21, an absorption slurry spray structure 22, and the like.
As shown in fig. 2, the desulfurization tower 21 provides a reaction space for desulfurization treatment. The bottom of the desulfurization tower 21 is a slurry space 25 in which the absorption slurry is placed. The absorption slurry spraying structure 22 is arranged in the desulfurization tower 21 and sprays absorption slurry into the desulfurization tower 21, so that the flue gas to be treated enters the desulfurization tower (21) to contact with the sprayed absorption slurry and react for desulfurization.
Optionally, the desulfurization treatment unit 20 further includes a slurry transport structure 23 that is connected to the absorption slurry spray structure 22 and transports the absorption slurry in the slurry space 25 into the absorption slurry spray structure 22 so that the absorption slurry spray structure 22 can spray the absorption slurry.
The absorption slurry may be a slurry of limestone or lime, or the like.
The absorbent slurry spray structure 22 may be one or more as desired. When the absorbing slurry spraying structure 22 is plural, the slurry transport structure 23 is connected to one or more of the plural absorbing slurry spraying structures 22, respectively, and transports the absorbing slurry thereto.
Optionally, a demisting and dedusting structure 24 may be further disposed in the desulfurizing tower 21, and is configured to perform dedusting and demisting treatment on the desulfurized flue gas to be treated, so as to remove at least a part of dust and mist droplets.
Alternatively, the mist and dust removing structure 24 may be a cyclonic wet electrostatic precipitation mist removal structure.
The flue gas to be treated after the desulfurization treatment flows out from the desulfurization treatment unit 20 enters the dust remover 30 for dust removal. In this embodiment, the dust collector 30 may be a bag-type dust collector, and the bag-type dust collector is used to filter the flue gas to be processed, so that dust and the like are left in the bag-type dust collector, and the gas passes through the dust collector 30.
The bag-type dust collector can be internally provided with activated carbon for adsorption, or can be not provided with activated carbon for adsorption.
The dust collector 30 may be other wet or dry dust collectors, such as an electrostatic dust collector, a wet cyclone dust collector, etc., according to different requirements.
The induced draft fan 40 provides power for the flow of the flue gas to be treated, and the flue gas is forced to flow. The induced draft fan 40 may be a centrifugal fan, an axial flow fan, or the like. The induced draft fan 40 may be disposed at any suitable position according to the necessity, and is not necessarily disposed between the dust separator 30 and the denitration treatment unit 50, and may be disposed before the dust separator 30.
The flue gas to be treated flowing out of the dust collector 30 enters the denitration treatment unit 50 for denitration treatment.
As shown in fig. 3, a main blower 51 and a booster blower 53 are connected to an air inlet of the reaction tower 54 of the denitration treatment unit 50 to introduce the flue gas to be treated into the reaction tower 54. The induced draft fan 40 may be provided or the induced draft fan 40 may be omitted depending on the power of the main fan 51 and the booster fan 53. For example, if the power of the main blower 51 and the booster blower 53 is sufficiently large, the induced draft fan 40 may be omitted.
An air source inlet branch is also connected between the main fan 51 and the booster fan 53 and used for supplementing air to the flue gas to be treated. The air source intake branch is connected to an air source 52.
As shown in fig. 3, in this embodiment, when the denitration reducing agent includes NH3 gas, the denitration processing unit 50 further includes a reducing agent delivery unit, which is connected to the reaction tower 54 and delivers NH3 gas into the reaction tower 54, so that the NH3 gas reacts with the nitride and the like in the flue gas to be processed at the adsorbent catalytic denitration structure in the reaction tower 54, and is converted into nitrogen, water and the like.
In this embodiment, the reducing agent supply unit includes an NH3 supply source, an air source, and a mixer 55, and the mixer 55 is configured to mix NH3 supplied from the NH3 supply source with air in an appropriate ratio and supply the mixture into the reaction tower 54 to perform a denitration reaction. The mixer 55 is connected to a NH3 delivery source and an air source, respectively, and mixes the incoming NH3 gas with the incoming air within the mixer 55.
An air pump 57 is provided between the mixer 55 and the air source for feeding air into the mixer 55.
Optionally, in order to make the temperature of the NH3 gas appropriate and ensure that the temperature of the denitration reaction is appropriate, a heater 56 is further provided between the air pump 57 and the mixer 55, and the heater 56 is used for heating the air. The heated air is further mixed with NH3 gas supplied from the reducing agent supply source in the mixer 55, and the temperature of the mixed NH3 gas is ensured.
The denitration principle by using NH3 gas and active coke is as follows:
the active coke has more macropores (the diameter is more than 50nm), mesopores (the diameter is 2.0-50 nm) and fewer micropores (the diameter is less than 2nm), and pores exist in the active coke in a coherent form, so that the active coke has better structural strength, is not easy to break and has longer service life.
The active coke has two action mechanisms when adsorbing pollutants, one is physical adsorption and the other is chemical adsorption.
The physical adsorption depends on the characteristic of large specific surface area of the active coke, the pollutants in the flue gas to be treated are trapped in the active coke, and the pollutant molecules are limited in the active coke by utilizing the characteristic that the sizes of micropores and molecular radii are equivalent. For example, dioxin is adsorbed by active coke.
The chemical adsorption depends on C atoms with defects on crystal lattices, oxygen-containing functional groups and polar surface oxides on the surface of the active coke, and by utilizing the chemical characteristics of the C atoms, the oxygen-containing functional groups and the polar surface oxides, pollutants are fixed on the inner surface of the active coke in a targeted manner to play a catalytic role.
Specifically, after NOx in the flue gas to be treated is adsorbed by the active coke, the NOx and surrounding H2O and O2 generate adsorbed HNO2 under the catalytic action of the active coke, and the adsorbed HNO reacts with introduced NH3 to generate NH4NO 2. NH4NO2 is unstable in chemical property and is easily decomposed into N2 and H2O under the catalytic action of active coke, so that the aim of denitration is fulfilled.
The denitration reaction by using the activated coke comprises the following steps:
2NO+2NH3+O2→2N2+3H2O
non-SCR (direct reaction with reducing substance formed at the time of desorption)
NO + C … Red → N2C-Red which is a reducing substance on the surface of the activated carbon
The denitration efficiency of catalytic denitration by using the activated coke can reach 90%, so that the denitration treatment unit 50 and the pre-denitration unit 10 can ensure the denitration rate close to 100% and the denitration effect.
In conclusion, the flue gas treatment system can adapt to denitration of complex gases, adopts the active coke to catalyze denitration, has small sensitivity and high mechanical strength of the active coke, is suitable for catalyst carriers, has stable chemical performance and simple regeneration conditions, and can effectively adsorb harmful substances in the flue gas to be treated.
The problems that the activated carbon has more micropores, huge micropores are basically and directly communicated with the surface, the mechanical strength is low, and the activated carbon is easy to break are solved, and the problem that the actual utilization rate of the pores is low due to the fact that broken activated carbon powder easily blocks the pores is further avoided. Because the activated carbon is not used, the problems of serious crushing condition and high loss rate in the regeneration of the activated carbon can be avoided.
In addition, the denitration temperature of the flue gas treatment system is low, the temperature of 80-110 ℃ is an optimal reaction temperature range, the energy consumption is low, steam heating is not needed in the operation process, and the problem of high energy consumption caused by the fact that the low-temperature SCR denitration operation temperature generally reaches 200 ℃ is solved.
In the process route, the denitration treatment unit 50 is installed after the desulfurization treatment unit 20, and only denitration is performed, and the loss of active coke is small.
The flue gas temperature is higher after the denitration of the active coke, and no white smoke is discharged.
The active coke has the functions of dedusting and removing dioxin, has a further purification function on clean flue gas to be treated, does not need to be provided with an active carbon injection system, and saves the cost.
The active coke is a non-hazardous product, if the catalytic function is finally lost, the active coke can be used as fuel for combustion, so that the operation cost is low, the daily denitration is only the consumption of ammonia gas, and no byproduct is generated in the denitration process and water is not consumed.
The granulating machine is used for granulating, so that the whole process has no discharge of fly ash and no secondary pollution.
And (3) utilizing a granulator to granulate the fly ash, collecting the flue gas fly ash collected by the bag-type dust collector and the dust generated by the active coke in the operation process, and then conveying the collected flue gas fly ash and the dust to the granulator to change the fine dust into granules. The granular substances enter an incinerator again to be burnt to remove dioxin contained in the granular substances, so that the granular substances have no toxicity. Meanwhile, granulation can prevent the fly ash from being changed into fly ash again in the combustion process and entering a flue gas system to form dead circulation. Combustible particles generated by fly ash granulation enter the furnace slag after being re-combusted, and can be comprehensively utilized as building materials.
Utilize this flue gas processing system to get rid of the solid particle dust, nitride (NOx), sulphide (SOx) and dioxin etc. that contain effectively in the flue gas that produces after the msw incineration, owing to utilize the burnt catalytic denitration of activity to handle behind the sack cleaner, its reaction temperature is lower for the flue gas temperature that the sack cleaner discharged just satisfies the burnt denitration technology needs of activity, consequently can need not to use flue gas reheating equipment (SGH), has saved equipment cost.
Those of ordinary skill in the art will appreciate that the various illustrative elements and method steps described in connection with the embodiments disclosed herein may be implemented as electronic hardware, or combinations of computer software and electronic hardware. Whether such functionality is implemented as hardware or software depends upon the particular application and design constraints imposed on the implementation. Skilled artisans may implement the described functionality in varying ways for each particular application, but such implementation decisions should not be interpreted as causing a departure from the scope of the present embodiments.
The above embodiments are only used for illustrating the embodiments of the present invention, and are not intended to limit the embodiments of the present invention, and those skilled in the relevant art can make various changes and modifications without departing from the spirit and scope of the embodiments of the present invention, and therefore all equivalent technical solutions also belong to the scope of the embodiments of the present invention, and the scope of patent protection of the embodiments of the present invention should be defined by the claims.

Claims (21)

1. The utility model provides a flue gas treatment system, its characterized in that includes denitration treatment unit (50), denitration treatment unit (50) include reaction tower (54) and adsorbent catalysis denitration structure, adsorbent catalysis denitration structure sets up in reaction tower (54), make and get into denitration reductant in reaction tower (54) and the nitride in the flue gas that treats processing react and the denitration under the catalysis of adsorbent catalysis denitration structure, adsorbent catalysis denitration structure includes active burnt catalysis denitration structure.
2. The flue gas treatment system of claim 1, further comprising a granulator (60), the granulator (60) being connected to the reaction tower (54) and producing the dust conveyed by the reaction tower (54) into fuel particles.
3. The flue gas treatment system according to claim 1 or 2, further comprising a dust separator (30), wherein the dust separator (30) is located at the front end of the denitration treatment unit (50) in the flow direction of the flue gas to be treated, so as to perform dust removal treatment on the flue gas to be treated before the denitration treatment unit (50).
4. A flue gas treatment system according to claim 3, wherein a granulator (60) is connected to the dust separator (30) and produces dust conveyed by the dust separator (30) as fuel particles; alternatively, the granulator (60) is connected to the reaction tower (54) of the denitration treatment unit (50) and the dust remover (30), respectively, and produces the dust conveyed by the reaction tower (54) and the dust remover (30) into fuel particles.
5. The flue gas treatment system according to claim 3, further comprising a pre-denitration unit (10), wherein the pre-denitration unit (10) is located at the front end of the deduster along the flow direction of the flue gas to be treated, and performs pre-denitration treatment on the flue gas to be treated.
6. The flue gas treatment system according to claim 3, further comprising a desulfurization treatment unit (20), wherein the desulfurization treatment unit (20) is located at the front end of the dust remover (30) in the flow direction of the flue gas to be treated, and performs desulfurization treatment on the flue gas to be treated; or the desulfurization unit (20) is positioned at the front end of the denitration unit (50) and performs desulfurization treatment on the flue gas to be treated before entering the denitration unit (50).
7. The flue gas treatment system according to claim 6, wherein the desulfurization treatment unit (20) comprises a desulfurization tower (21) and an absorption slurry spraying structure (22), the absorption slurry spraying structure (22) is arranged in the desulfurization tower (21) and sprays absorption slurry into the desulfurization tower (21), and the flue gas to be treated enters the desulfurization tower (21) to contact with the sprayed absorption slurry and react for desulfurization.
8. The flue gas treatment system according to claim 1 or 2, wherein the denitration treatment unit (50) further includes a reducing agent delivery portion that is connected to the reaction tower (54) and that delivers the denitration reducing agent into the reaction tower (54).
9. The flue gas treatment system according to claim 8, wherein the denitration reductant comprises NH3 gas, and the reductant delivery section comprises an NH3 delivery source, an air source, and a mixer (55), the mixer (55) being connected to the NH3 delivery source and the air source, respectively, and mixing NH3 gas and air within the mixer (55).
10. The flue gas treatment system according to claim 9, wherein a heater is further provided between the air source and the mixer (55), the heater heating the gas input by the air source.
11. The flue gas treatment system is characterized by comprising a flue gas purification part and a granulator (60) connected with the flue gas purification part, wherein the flue gas purification part performs at least one of desulfurization treatment, denitration treatment and dust removal treatment on flue gas to be treated, and the granulator (60) obtains dust output by the flue gas purification part and generates the dust into fuel particles.
12. The flue gas treatment system of claim 11, wherein the flue gas cleaning section comprises:
the denitration treatment unit (50) comprises a reaction tower (54) and an adsorbent catalytic denitration structure arranged in the reaction tower (54), the adsorbent catalytic denitration structure enables denitration reducing agents entering the reaction tower (54) and nitrides in flue gas to be treated to react and denitrate under the catalysis of the adsorbent catalytic denitration structure, and the granulator (60) is connected with the reaction tower (54) and is used for manufacturing dust conveyed by the reaction tower (54) into fuel particles.
13. The flue gas treatment system according to claim 12, wherein the flue gas cleaning section comprises a dust collector (30), the dust collector (30) is located at a front end of the denitration treatment unit (50) in a flow direction of the flue gas to be treated to dust-collect the flue gas to be treated before the denitration treatment unit (50), and the granulator (60) is connected to the dust collector (30) and produces dust conveyed by the dust collector (30) into fuel particles.
14. The flue gas treatment system according to claim 13, wherein when the flue gas purification section includes the denitration treatment unit (50) and the dust remover (30), the granulator (60) is connected to the reaction tower (54) of the denitration treatment unit (50) and the dust remover (30), respectively, and produces the dust conveyed by the reaction tower (54) and the dust remover (30) into fuel particles.
15. The flue gas treatment system according to claim 13, wherein the flue gas purification section further comprises a pre-denitration unit (10), and the pre-denitration unit (10) is located at a front end of the dust collector (30) in a flow direction of the flue gas to be treated, and performs pre-denitration treatment on the flue gas to be treated.
16. The flue gas treatment system according to claim 13, further comprising a desulfurization treatment unit (20), wherein the desulfurization treatment unit (20) is located at a front end of the dust collector (30) in a flow direction of the flue gas to be treated, and performs desulfurization treatment on the flue gas to be treated.
17. The flue gas treatment system according to claim 16, wherein the desulfurization treatment unit (20) comprises a desulfurization tower (21) and an absorption slurry spraying structure (22), the absorption slurry spraying structure (22) is arranged in the desulfurization tower (21) and sprays absorption slurry into the desulfurization tower (21), and the flue gas to be treated enters the desulfurization tower (21) to contact with the sprayed absorption slurry and react for desulfurization.
18. The flue gas treatment system according to claim 13, wherein the denitration treatment unit (50) further includes a reducing agent delivery portion that is connected to the reaction tower (54) and that delivers the denitration reducing agent into the reaction tower (54).
19. The flue gas treatment system according to claim 18, wherein the denitration reductant comprises NH3 gas, and the reductant delivery section comprises an NH3 delivery source, an air source, and a mixer (55), the mixer (55) being connected to the NH3 delivery source and the air source, respectively, and mixing NH3 gas and air within the mixer (55).
20. The flue gas treatment system according to claim 19, wherein a heater is further provided between the air source and the mixer (55), the heater heating the gas input by the air source.
21. The flue gas treatment system of any of claims 13-20, wherein the sorbent catalytic denitrification structure comprises an active coke catalytic denitrification structure.
CN201821808900.9U 2018-11-02 2018-11-02 Flue gas treatment system Active CN210057855U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201821808900.9U CN210057855U (en) 2018-11-02 2018-11-02 Flue gas treatment system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201821808900.9U CN210057855U (en) 2018-11-02 2018-11-02 Flue gas treatment system

Publications (1)

Publication Number Publication Date
CN210057855U true CN210057855U (en) 2020-02-14

Family

ID=69426383

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201821808900.9U Active CN210057855U (en) 2018-11-02 2018-11-02 Flue gas treatment system

Country Status (1)

Country Link
CN (1) CN210057855U (en)

Similar Documents

Publication Publication Date Title
CN102459833B (en) Combustion flue gas NOX treatment
KR101298305B1 (en) Apparatus for removing of trace of toxic substance from exhaust gas and method of operating the same
CN103990362A (en) Method and device for removing sulfur, nitre and mercury in smoke
CN102772986B (en) Flue gas desulfurization and denitration integrated process
CN104759192A (en) Low-cost coal-fired flue gas various pollutant ultralow emission system and low-cost coal-fired flue gas various pollutant ultralow emission method
CN107376639B (en) Hazardous waste incineration flue gas purification method
CN109569228A (en) The exhaust system and technique of flue gas of garbage furnace
CN110860196A (en) Desulfurization and denitrification system for cement flue gas
CN210814645U (en) Waste incineration flue gas ultralow emission purification system
CN102294171A (en) Flue gas purifying system
CN110756033A (en) Deep purification treatment system and process for waste incineration power station flue gas
CN204582930U (en) A kind of low cost coal-fired flue-gas multiple pollutant minimum discharge system
CN210278758U (en) Super-clean emission treatment device for flue gas of household garbage incinerator
CN104607015A (en) Multi-pollutant co-purification method and multi-pollutant co-purification system for sintering flue gas
CN202136916U (en) Flue gas purification system
CN203829899U (en) Smoke desulfurization denitration and demercuration device
CN210057855U (en) Flue gas treatment system
CN212999279U (en) Flue gas treatment system for efficiently utilizing carbon monoxide
CN108043210A (en) A kind of desulfurization of coke oven flue gas and dedusting denitrification integral system
CN201327042Y (en) Device for removing nitrogen oxide and dioxin in waste gas of low ash zone of burning facility
CN111545026A (en) Low-temperature efficient desulfurization and denitrification device and method for flue gas
CN210278800U (en) Low-temperature catalyst denitration dust removal equipment with pottery fine filter tube
CN111389117A (en) Active coke regeneration waste gas treatment device and method
CN110876886A (en) Waste incineration flue gas purification method and system
CN101444701B (en) Equipment for removing nitrogen oxides and dioxin in waste gas at low-ash area of burning facility

Legal Events

Date Code Title Description
GR01 Patent grant
GR01 Patent grant
TR01 Transfer of patent right
TR01 Transfer of patent right

Effective date of registration: 20220107

Address after: 100160 room 08, 5 / F, 101, building 5, zone 3, No. 186, South Fourth Ring West Road, Fengtai District, Beijing

Patentee after: Beijing Zhongneng Rongtai energy and Environmental Protection Technology Co.,Ltd.

Address before: 100097 room 321, Guan Fang building, 18 Changhua Road, Haidian District, Beijing.

Patentee before: BEIJING ZHONGNENG NUOTAI ENERGY SAVING AND ENVIRONMENTAL PROTECTION Co.,Ltd.