CN220443550U - Multi-pollution co-treatment system - Google Patents
Multi-pollution co-treatment system Download PDFInfo
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- CN220443550U CN220443550U CN202320330011.0U CN202320330011U CN220443550U CN 220443550 U CN220443550 U CN 220443550U CN 202320330011 U CN202320330011 U CN 202320330011U CN 220443550 U CN220443550 U CN 220443550U
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- flue gas
- desulfurization
- reaction tower
- dust
- particle separation
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- 238000011278 co-treatment Methods 0.000 title abstract description 9
- 239000002245 particle Substances 0.000 claims abstract description 83
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 72
- 230000023556 desulfurization Effects 0.000 claims abstract description 72
- 238000006243 chemical reaction Methods 0.000 claims abstract description 69
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000003546 flue gas Substances 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 44
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 36
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 28
- 239000000843 powder Substances 0.000 claims description 11
- 239000000428 dust Substances 0.000 abstract description 56
- 238000007599 discharging Methods 0.000 abstract description 12
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract description 7
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 7
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 238000009825 accumulation Methods 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 239000003054 catalyst Substances 0.000 abstract 1
- 239000000463 material Substances 0.000 description 19
- 239000002956 ash Substances 0.000 description 17
- 238000000034 method Methods 0.000 description 15
- 239000003463 adsorbent Substances 0.000 description 11
- 239000006227 byproduct Substances 0.000 description 8
- 239000010881 fly ash Substances 0.000 description 7
- 238000001179 sorption measurement Methods 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a multi-pollution co-treatment system. The system at least comprises a desulfurization reaction tower, a reaction tower and a reaction tower, wherein the reaction tower is connected with the reaction tower in sequence a particle separation and returning system and a secondary mixing reactor; desulfurizing agent for desulfurization reaction the grain diameter range of the catalyst is 0.5-3 mm; the particle separation system has a particle size of greater than 0.5 the particle separation efficiency of mm is more than 99%. The utility model is used for desulfurization and dust removal under the condition of high-dust industrial flue gas, and the cooperative treatment of multiple pollutants such as dioxin, heavy metal and the like, and by utilizing the particle size difference of the desulfurizing agent and the flue gas dust and separating, the influence of high-concentration flue gas dust accumulation on the semi-dry desulfurization reaction of the circulating fluidized bed is avoided, the utilization rate of the desulfurizing agent and the purity of the desulfurized ash are improved, the desulfurized ash and the flue gas dust are collected separately through an independent ash discharging system, and the secondary utilization value of the desulfurized ash is improved; the treatment efficiency of the system is effectively improved.
Description
Technical Field
The utility model relates to the field of industrial flue gas pollution control, in particular to a semi-dry desulfurization and multi-pollution co-treatment system for high-dust industrial flue gas.
Background
CFB (circulating fluidized bed) semi-dry desulfurization technology is widely applied to flue gas SO at present 2 Treatment technology with SO 2 High removal efficiency and stable operation. The conventional CFB circulating fluidized bed process mainly comprises a desulfurization reaction tower, a bag-type dust collector and a material circulating system, wherein after the mixed reaction of the desulfurizing agent and the flue gas, the desulfurizing agent is collected through the bag-type dust collector and returns to the desulfurization tower through the material circulation for continuous reaction, and in the process, dust in the flue gas also participates in circulation along with the desulfurizing agent, but as the dust in the flue gas and fly ash have no desulfurization effect, the desulfurization effect of the circulating fluidized bed can be seriously affected by the dust with an excessively high proportion. Meanwhile, dust with high proportion content can be generated in the by-product desulfurization ash, so that the purity of the desulfurization ash is greatly reduced, and great difficulty is caused to the disposal and secondary utilization of the desulfurization ash.
The common particle size of dust (fly ash) in the flue gas of the industrial furnace is 10-100 um, and the existing circulating fluidized bed desulfurization process applied to engineering needs to newly build a flue gas pre-dedusting device (usually an electric dust removing device or a gravity dust removing device) at an inlet for desulfurization treatment of high-dust flue gas, so that investment and occupied area are increased, and the pre-dedusting device has no gain effect on bag dust removal of semi-dry desulfurization (because the flue gas is mixed and reacted with a desulfurizing agent in the desulfurization process, and the dust content is increased again). Therefore, the applicability of conventional circulating fluidized bed desulfurization processes to the disposal of high dust fumes remains a great problem, both from the standpoint of investment, occupation of land, and process rationality.
In the circulating fluidization dry flue gas desulfurization method adopting layered feed back disclosed in patent CN 1225304C, two-stage particle separation and recirculation are adopted for feed back in the external particle recirculation process of the desulfurizing tower from the perspective of reducing the lower part adhesion and blockage of the desulfurizing reactor and the burden of a single dust collector. However, since the particle size of the conventional desulfurizing agent is overlapped with that of dust in the flue gas, effective separation of the desulfurizing agent from the dust (fly ash) cannot be realized; and the materials after two-stage separation return to the desulfurization system, and the desulfurization system is a conventional circulating fluidized bed process, so that the problem of influence of dust accumulation on desulfurization reaction under the condition of high-dust flue gas can not be solved.
In addition, with the gradual increase of environmental protection requirements, the pollutant treatment of industrial flue gas is not limited to SO 2 The standard emission of NOx and dust also puts forward higher requirements on dioxin and heavy metals existing in the flue gas, and the cooperative treatment of multiple pollutants becomes the direction of environmental protection development. Usually, the removal of dioxin and heavy metals adopts an adsorption principle, and the reacted adsorbent is collected together through a dust removal system. However, in the conventional circulating fluidized bed desulfurization process, only the adsorbent is injected into the inlet of the desulfurization tower and the adsorption reaction is completed in the tower because the concentration of the desulfurizing agent in the fluidized bed in the tower is high (800-1000 g/Nm) 3 ) The dosage of the adsorbent is greatly higher than that of the adsorbent, so that the adsorbent is wrapped by the high-concentration desulfurizing agent, and the removing effect on dioxin and heavy metals is limited.
Disclosure of Invention
Aiming at the problems, the utility model aims to provide a system and a method for semidry desulfurization and multi-pollution co-treatment of high-dust industrial flue gas, which are practical in improving the purity and the secondary utilization value of desulfurization ash and realizing multi-pollutant co-treatment.
In order to achieve the aim, the utility model relates to a semi-dry desulfurization and multi-pollution co-treatment system for high-dust industrial flue gas, which comprises a desulfurization reaction tower, a particle separation and returning system and a secondary mixing reactor which are connected in sequence; the particle size range of the desulfurizing agent for the desulfurization reaction is 0.5-3 mm; the particle separation efficiency of the particle separation and returning system on particles with the particle size of more than 0.5mm is more than 99 percent;
the desulfurization reaction tower adopts a circulating fluidized bed semi-dry desulfurization reaction tower, and an outlet of the desulfurization reaction tower is connected with an inlet of a particle separation and returning system; the powder discharge port of the particle separation and returning system is connected with the inlet of the desulfurization reaction tower through the returning system, and the flue gas outlet of the particle separation system is connected with the inlet of the secondary mixing reactor.
Further, an outlet on the secondary mixing reactor is connected with a dust removal system; the particle separation system and the dust removal system are provided with independent ash discharging devices.
Furthermore, the desulfurizing agent for the desulfurization reaction is dry powder slaked lime particles.
Further, a reaction material feeding port is arranged on the secondary mixing reactor, the reaction material is one or more of active carbon, fly ash and molecular sieve, and the particle size is smaller than 1mm.
Furthermore, the dust removing system is a cloth bag dust remover, and the collected flue gas and dust and reaction byproducts of the secondary mixing reactor are discharged through an ash discharging device and do not participate in the circulating reaction.
In order to achieve the above purpose, the method for semidry desulfurization and multi-pollution co-treatment of high-dust industrial flue gas of the utility model comprises the following steps: in a system sequentially connected with a desulfurization reaction tower, a particle separation and returning system and a secondary mixing reactor, the particle size range of a desulfurizing agent for desulfurization reaction is 0.5-3 mm; the particle separation efficiency of the particle separation system on particles with the particle size of more than 0.5mm is more than 99 percent;
the outlet of the desulfurization reaction tower is connected with the inlet of the particle separation system; the powder discharge port of the particle separation system is connected with the inlet of the desulfurization reaction tower through the material returning system, and the flue gas outlet of the particle separation system is connected with the inlet of the secondary mixing reactor.
The utility model has the beneficial effects that:
1) The utility model adopts the desulfurizer with larger particle diameter (0.5-3 mm) and effectively separates the flue gas dust (fly ash) by a particle separation system; the desulfurization agent in the materials entering the circulating system is guaranteed to occupy most part, the influence of high-content dust circulation accumulation on the desulfurization effect is avoided, the utilization rate of the desulfurization agent is improved, the ineffective circulation of the materials and the operation cost brought by the ineffective circulation are reduced, and the normal use and desulfurization efficiency of the circulating fluidized bed under the condition of high dust and smoke are guaranteed.
2) The particle separation system provided by the utility model is provided with an independent desulfurization ash discharge device, and the by-product desulfurization ash and dust in the flue gas are collected separately, so that the purity and the secondary utilization value of the desulfurization ash are greatly improved;
3) On the basis of the conventional circulating fluidized bed desulfurization process, the special secondary mixing reactor is added, the synergistic treatment of dioxin and heavy metals in the flue gas is realized, the adsorbent in the secondary reactor is not influenced by the desulfurizing agent of the desulfurization reaction circulation, the use efficiency is high, and the adsorption effect is good.
Drawings
FIG. 1 is a schematic overall flow chart of the present utility model;
in the figure, a circulating fluidized bed desulfurization reaction tower 1, a desulfurizing agent adding port 2, a particle separation system 3, a powder discharging port 4, a circulating system 5, a desulfurized ash discharging port 6, a secondary mixing reactor 7, an adsorbent adding port 8, a bag-type dust remover 9, a dedusting ash discharging port 10, an induced draft fan 11 and a chimney 12.
Detailed Description
Embodiments of the present utility model will be described in detail below with reference to the accompanying drawings.
In the description of the present utility model, it should be understood that the terms "center," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like indicate orientations or positional relationships based on the orientation or positional relationships shown in the drawings, merely to facilitate describing the present utility model and simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
The terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present utility model, unless otherwise indicated, the meaning of "a plurality" is two or more.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
As an embodiment of the present utility model, referring to fig. 1, there is provided a desulfurization reaction tower 1, a particle separation and return system 3, and a secondary mixing reactor 7. The particle separation system can adopt a cyclone dust removal system, a gravity dust removal system and the like, and the dust removal efficiency can be designed according to the particle size of dust; the material returning system can be a pipeline, a chute, a bin pump/pneumatic conveying system and the like. The desulfurization reaction tower 1 adopts a circulating fluidized bed semi-dry desulfurization reaction tower, and an outlet of the desulfurization reaction tower 1 is connected with an inlet of the particle separation system 3; the powder discharge port 4 of the particle separation system 3 is connected with the inlet of the desulfurization reaction tower 1 through a material returning system 5, and the flue gas outlet of the particle separation system 3 is connected with the inlet of the secondary mixing reactor 7; the secondary mixing reactor 7 is provided with a reaction material feeding port 8; the particle separation system 3 has a separate ash discharge device 6, which typically comprises a discharge valve, a silo pump/pneumatic conveyor system, a pneumatic/manual valve block, a pipe.
The particle size of the desulfurizing agent adopted by the utility model is 0.5-3 mm, the desulfurizing agent can be added into the desulfurizing reaction tower 1 through the desulfurizing agent adding port 2, the desulfurizing reaction is completed in the reaction tower with high-dust flue gas to be desulfurized, the desulfurized flue gas enters the particle separating system 3, the particle separating efficiency of the particle separating system 3 for particles with the particle size of more than 0.5mm is more than 99%, the separated large-particle-size desulfurizing agent is conveyed into the desulfurizing reaction tower 1 through the powder discharging port 4 at the lower part of the particle separating system 3 for recycling through the circulating system 5, small-particle-size dust enters the secondary mixing reactor 7 along with the flue gas, and meanwhile, the lower part of the particle separating system 3 is also provided with an independent desulfurized ash discharging device 6, and the desulfurized ash as a reaction byproduct is discharged periodically along with the progress of the desulfurizing reaction.
As a further embodiment of the utility model, referring to FIG. 1, the desulfurization reaction tower 1, a particle separation and return system 3, a secondary mixing reactor 7 and a dust removal system 9 are included. The desulfurization reaction tower 1 adopts a circulating fluidized bed semi-dry desulfurization reaction tower, and an outlet of the desulfurization reaction tower 1 is connected with an inlet of the particle separation system 3; the powder discharge port 4 of the particle separation system 3 is connected with the inlet of the desulfurization reaction tower 1 through a material returning system 5, and the flue gas outlet of the particle separation system 3 is connected with the inlet of the secondary mixing reactor 7; the secondary mixing reactor 7 is provided with a reaction material feeding port 8, and the outlet is connected with a dust removal system 9; the particle separating system 3 and the dust removal system 9 have separate dust discharging means 6 and 10.
The particle size of the desulfurizing agent adopted in the embodiment is 1-2mm, the desulfurizing agent is added into the desulfurizing reaction tower 1 through the desulfurizing agent adding port 2, the desulfurizing reaction is completed in the reaction tower with high-dust flue gas to be desulfurized, the desulfurized flue gas enters the particle separating system 3, the particle separating efficiency of the particle separating system 3 for particles with the particle size of more than 0.5mm is more than 99%, the separated large-particle-size desulfurizing agent passes through the powder discharging port 4 at the lower part of the particle separating system 3 and is conveyed into the desulfurizing reaction tower 1 through the circulating system 5 for recycling, small-particle-size dust enters the secondary mixing reactor 7 along with the flue gas, and meanwhile, the lower part of the particle separating system 3 is also provided with an independent desulfurized ash discharging device 6, and the desulfurized ash serving as a reaction byproduct is discharged periodically along with the progress of the desulfurizing reaction.
As a further improvement of the embodiment, an adsorbent adding port 8 is arranged on the secondary mixing reactor 7, the added reaction materials are one or more of adsorption materials such as activated carbon, fly ash, molecular sieve and the like, the particle size is smaller than 1mm, the adsorption and removal of dioxin and heavy metals in the flue gas are completed in the secondary mixing reactor 7, and the reacted adsorbent byproducts enter a dust removal system 9 along with the flue gas.
The dust removing system 9 adopts a high-efficiency bag-type dust remover, and the collected flue gas and dust and reaction byproducts of the secondary mixing reactor are discharged through an independent ash discharging device 10 and do not participate in the circulating reaction. The purified flue gas is sent to a chimney 12 through a draught fan 11 to reach the standard for emission.
As an embodiment of the method for semi-dry desulfurization and multi-pollution co-treatment of high-dust industrial flue gas, the method comprises the following steps: in a system sequentially connected with a desulfurization reaction tower, a particle separation and returning system and a secondary mixing reactor, an outlet of the desulfurization reaction tower is connected with an inlet of the particle separation system; the powder discharge port of the particle separation system is connected with the inlet of the desulfurization reaction tower through the material returning system, and the flue gas outlet of the particle separation system is connected with the inlet of the secondary mixing reactor.
The particle size range of the desulfurizing agent for the desulfurization reaction is 0.5-3 mm; the particle separation efficiency of the particle separation system on particles with the particle size of more than 0.5mm is more than 99 percent; the separated large-particle-size particles are sent back to the desulfurization reaction tower through the powder discharge port and the returning system to continuously participate in the desulfurization reaction, and the non-separated small-particle-size dust enters the secondary mixing reactor along with the flue gas.
As a further improvement of the embodiment, an adsorbent adding port 8 is arranged on the secondary mixing reactor 7, the added reaction materials are one or more of adsorption materials such as activated carbon, fly ash, molecular sieve and the like, the particle size is smaller than 1mm, the adsorption and removal of dioxin and heavy metals in the flue gas are completed in the secondary mixing reactor 7, and the reacted adsorbent byproducts enter a dust removal system 9 along with the flue gas.
The present utility model has been described in detail with reference to the drawings, but the present utility model is not limited to the above embodiments, and various changes can be made within the knowledge of those skilled in the art without departing from the spirit of the present utility model. Many other changes and modifications may be made without departing from the spirit and scope of the utility model and should be considered as within the scope of the utility model.
In the description of the present specification, a particular feature, structure, material, or characteristic may be combined in any suitable manner in one or more embodiments or examples.
The foregoing is merely illustrative of the present utility model, and the present utility model is not limited thereto, and any person skilled in the art will readily recognize that variations or substitutions are within the scope of the present utility model. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.
Claims (1)
1. A multi-pollution co-disposal system, characterized by: the system at least comprises a desulfurization reaction tower, a particle separation and returning system and a secondary mixing reactor which are connected in sequence; the particle size range of the desulfurizing agent for the desulfurization reaction is 0.5-3 mm; the particle separation efficiency of the particle separation and returning system on particles with the particle size of more than 0.5mm is more than 99 percent;
the desulfurization reaction tower adopts a circulating fluidized bed semi-dry desulfurization reaction tower, and an outlet of the desulfurization reaction tower is connected with an inlet of a particle separation and returning system; the powder discharge port of the particle separation and returning system is connected with the inlet of the desulfurization reaction tower through the returning system, and the flue gas outlet of the particle separation and returning system is connected with the inlet of the secondary mixing reactor.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320330011.0U CN220443550U (en) | 2023-02-28 | 2023-02-28 | Multi-pollution co-treatment system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320330011.0U CN220443550U (en) | 2023-02-28 | 2023-02-28 | Multi-pollution co-treatment system |
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| Publication Number | Publication Date |
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| CN220443550U true CN220443550U (en) | 2024-02-06 |
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| CN202320330011.0U Active CN220443550U (en) | 2023-02-28 | 2023-02-28 | Multi-pollution co-treatment system |
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| CN (1) | CN220443550U (en) |
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