CN110711470A - Desulfurization and denitrification purification process for incineration flue gas of biomass boiler - Google Patents

Desulfurization and denitrification purification process for incineration flue gas of biomass boiler Download PDF

Info

Publication number
CN110711470A
CN110711470A CN201910898013.8A CN201910898013A CN110711470A CN 110711470 A CN110711470 A CN 110711470A CN 201910898013 A CN201910898013 A CN 201910898013A CN 110711470 A CN110711470 A CN 110711470A
Authority
CN
China
Prior art keywords
flue gas
denitration
desulfurization
biomass boiler
denitrification
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.)
Pending
Application number
CN201910898013.8A
Other languages
Chinese (zh)
Inventor
施小东
傅远峰
翁林钢
叶青
戚科技
张帅
刘洪昌
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.)
Zhejiang Doway Advanced Technology Co Ltd
Original Assignee
Zhejiang Doway Advanced Technology 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 Zhejiang Doway Advanced Technology Co Ltd filed Critical Zhejiang Doway Advanced Technology Co Ltd
Priority to CN201910898013.8A priority Critical patent/CN110711470A/en
Publication of CN110711470A publication Critical patent/CN110711470A/en
Pending legal-status Critical Current

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/32—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by electrical effects other than those provided for in group B01D61/00
    • B01D53/323—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by electrical effects other than those provided for in group B01D61/00 by electrostatic effects or by high-voltage electric fields
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/76—Gas phase processes, e.g. by using aerosols
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2067—Urea
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/101—Baghouse type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/102—Intercepting solids by filters electrostatic
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers
    • Y—GENERAL 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/30—Technologies for a more efficient combustion or heat usage

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Health & Medical Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Dispersion Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention provides a desulfurization, denitrification and purification process for incineration flue gas of a biomass boiler. And (4) performing cloth bag dust removal on the cooled flue gas, and collecting the smoke dust in the flue gas in a fly ash collecting system. The flue gas after the bag dust removal enters a plasma reaction device or an ozone generator to convert NO in the flue gas into NO2、N2O5And HNO3Part of SO2Conversion to H2SO4. The flue gas after the oxidation gets into the absorption tower, absorbs the acidic material in the flue gas through spraying alkali lye, lets in the denitration additive simultaneously or adopts wet flue gas desulfurization system thick liquid to absorb nitrogen oxide, realizes the denitration in coordination. Denitration reaction is respectively carried out on the flue gas before and after cloth bag dust removal, so that the denitration efficiency is improved; still reduce the flue gas temperature to suitable scope through waste heat recovery to do benefit to follow-up deacidification denitration process, and realize heat recovery, avoid the waste of the energy.

Description

Desulfurization and denitrification purification process for incineration flue gas of biomass boiler
Technical Field
The invention relates to the technical field of flue gas purification, in particular to a desulfurization and denitrification purification process for incineration flue gas of a biomass boiler.
Background
Electric energy is energy on which human beings live, but the electric energy is not directly obtained from the nature, but is converted from other energy sources. The data of '2018 Chinese power production type proportion' issued by the statistical bureau shows that the thermal power generation is still the main power of power supplyMilitary, 73.32% of the annual energy production of 2018. Thermal power generation supplies electric energy and is accompanied by environmental pollution. No matter the traditional coal-fired power generation, the emerging garbage combustion power generation, the biomass combustion power generation and the like can generate NOX、SO2And heavy metals, fly ash and other atmospheric pollutants bring great harm to the production and life of human beings.
Although the traditional flue gas treatment process meets the requirement of pollutant emission limit in the emission standard of atmospheric pollutants of thermal power plants (GB13223-2011), the traditional flue gas treatment process also has the problems of instability, high operation cost, low denitration and desulfurization efficiency and the like in the operation process. In recent years, with the improvement of environmental protection requirements, many thermal power plants try to replace coal, sludge and the like with biomass and the like as boiler fuels, so that the problem of environmental pollution caused by open-air stacking and incineration of biomass is solved, and the use of coal can be saved. However, in a flue gas treatment system of a thermal power plant using biomass as fuel, it is found that fly ash generated after biomass combustion contains a plurality of heavy metals and inorganic salts thereof, and has low porosity and high viscosity and strength. If the denitration is performed by adopting the traditional honeycomb or plate type SCR denitration device before the bag-type dust collector, the fly ash containing the alkaline metal can contact with the catalyst during the process operation, so that the catalyst is inactivated, the denitration efficiency is further reduced, and the long-term stable operation of a denitration system is influenced. If the SCR denitration device is arranged behind the bag type dust collector, an imported medium-low temperature catalyst is mostly adopted, the denitration needs to be carried out at about 230 ℃, the denitration efficiency is not high, and the cost is high. Therefore, it is necessary to provide a practical and effective desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler in a thermal power plant using biomass and the like as fuel.
Disclosure of Invention
The invention aims to provide a desulfurization, denitrification and purification process for incineration flue gas of a biomass boiler, and solves the problems that the denitration efficiency is not high and the cost is high in the existing process no matter before dust removal or after dust removal.
In order to solve the problems, the invention provides a desulfurization, denitrification and purification process for incineration flue gas of a biomass boiler, which comprises the following steps:
a primary denitration step: spraying a denitration agent into the biomass boiler, so that the flue gas generated after the fuel is combusted in the hearth of the biomass boiler and the denitration agent are subjected to SNCR denitration reaction;
a waste heat recovery step: enabling the outlet flue gas of the biomass boiler to enter a waste heat recovery device to recover waste heat in the flue gas, and reducing the temperature of the flue gas;
a bag dust removal step: the flue gas from the waste heat recovery device enters a bag-type dust collector for dust removal, and the smoke dust in the flue gas is collected by the bag-type dust collector and collected in a fly ash collection system as fly ash;
an oxidation reaction step: the flue gas after the bag dust removal enters a plasma reaction device or an ozone generator for oxidation reaction, and NO in the flue gas is converted into NO2、N2O5And HNO3Part of SO in the flue gas2Is also converted into H2SO4；
An absorption step: enabling the flue gas after the oxidation reaction to enter an absorption tower, spraying alkali liquor into the absorption tower through a spraying device, enabling acid substances in the flue gas to be absorbed by the sprayed alkali liquor, and simultaneously introducing a denitration additive into the absorption tower or absorbing nitrogen oxide by adopting a wet desulphurization system slurry to realize synergistic denitration;
electric precipitation: and (4) allowing the flue gas treated in the absorption step to enter an electric dust remover for dust removal, and discharging the clean flue gas after dust removal.
According to an embodiment of the invention, in the burning and denitration step, a denitration agent is sprayed into the biomass boiler through an SNCR denitration device, wherein the spraying position of the SNCR denitration device for spraying the denitration agent is positioned at the upper part of a hearth of the biomass boiler or at the inlet of a cyclone separator.
According to an embodiment of the invention, in the burning and denitration step, the injected denitration agent is urea or ammonia water, and the injection amount of the denitration agent is 1.0-1.4 times of the theoretical value of the molar weight of the nitrogen oxides in the flue gas.
According to an embodiment of the present invention, in the waste heat recovery step, the waste heat recovery device uses an air waste heat device, and the temperature of the flue gas is reduced to 150 ℃ after the waste heat is recovered.
According to an embodiment of the invention, in the bag-type dust removing step, the bag-type dust remover is made of PPS plastic with heat resistance and chemical resistance.
According to an embodiment of the invention, in the oxidation reaction step, the flue gas subjected to cloth bag dust removal is introduced into a low-temperature plasma reaction device through a draught fan for plasma discharge treatment, and the low-temperature plasma reaction device generates high-energy electrons and oxygen radicals serving as active particles required by desulfurization and denitrification to convert NO in the flue gas into NO2、N2O5And HNO3。
According to an embodiment of the invention, in the absorbing step, the denitration additive is Na2S、Na2SO3、(NH4)2SO3One or more of (a).
According to an embodiment of the present invention, in the absorption step, the wet desulphurization system slurry is used to absorb nitrogen oxides, the absorption tower has an absorption tower main body, a first slurry tank is arranged at the bottom of the absorption tower main body, the wet desulphurization system slurry tank is communicated with the first slurry tank of the absorption tower, and the absorption of SO in the wet desulphurization system slurry tank is utilized2SO not oxidized later3 2-And absorbing the nitrogen oxide treated by the oxidation reaction by ions.
According to an embodiment of the present invention, in the absorption step, a second slurry pool installation and oxidation device is disposed outside the absorption tower main body, and the slurry after absorbing the nitrogen oxides enters the second slurry pool outside the tower to be oxidized, crystallized and discharged.
According to an embodiment of the invention, in the absorption step, the alkali liquor sprayed into the absorption tower is fed into the spraying device again for cyclic spraying.
Compared with the prior art, the technical scheme has the following advantages:
the invention carries out primary denitration on the flue gas generated after the combustion in the biomass boiler before the bag-type dust removal step,and then recovering heat energy in the flue gas after the primary denitration through a waste heat recovery step, so that the temperature of the flue gas is reduced. The flue gas is subjected to bag-type dust removal and oxidation reaction, so that NO which is difficult to absorb in the flue gas is converted into NO which is easy to absorb2、N2O5And HNO3Part of SO2Is also converted into H2SO4. And (3) the oxidized flue gas is subjected to absorption action of an absorption tower to realize desulfurization and deacidification, and finally, the smoke dust is removed through an electric dust removal step to obtain clean flue gas and the clean flue gas is discharged. In the scheme of the invention, the flue gas is subjected to preliminary denitration reaction before the cloth bag dust removal process, and nitrogen oxides in the flue gas after the cloth bag dust removal are oxidized and denitrated in a coordinated manner in the deacidification process, so that deacidification and multiple denitration are realized, and the denitration efficiency is improved; in addition, waste heat recovery is carried out after primary denitration, so that on one hand, the temperature of the flue gas can be reduced to a proper range, the subsequent deacidification and denitration process is facilitated, on the other hand, heat energy can be recovered, and the energy waste is avoided.
Drawings
FIG. 1 is a flow chart of a desulfurization, denitrification and purification process for incineration flue gas of a biomass boiler provided by the invention;
FIG. 2 is a schematic structural diagram of a desulfurization and denitrification purification system for incineration flue gas of a biomass boiler for implementing the process of the invention.
Detailed Description
The following description is only for the purpose of disclosing the invention so as to enable a person skilled in the art to practice the invention. The embodiments in the following description are given by way of example only, and other obvious variations will occur to those skilled in the art. The principles of the invention, as defined in the following description, may be applied to other embodiments, variations, modifications, equivalents, and other arrangements without departing from the spirit and scope of the invention.
As shown in fig. 1, the invention provides a desulfurization, denitrification and purification process for incineration flue gas of a biomass boiler, which can perform preliminary denitrification reaction on the flue gas after the combustion of the biomass boiler before the cloth bag dust removal process, oxidize nitrogen oxides in the flue gas after the cloth bag dust removal and perform synergistic denitrification in the deacidification process, i.e. perform multiple denitrification, thereby improving the denitrification efficiency; in addition, waste heat recovery is carried out after primary denitration, so that on one hand, the temperature of the flue gas can be reduced to a proper range, the subsequent deacidification and denitration process is facilitated, on the other hand, heat energy can be recovered, and the energy waste is avoided. The desulfurization, denitrification and purification process for incineration flue gas of the biomass boiler comprises the following steps:
a primary denitration step: spraying a denitration agent into the biomass boiler 300, so that the flue gas and the denitration agent generated after the fuel is combusted in the hearth of the biomass boiler 300 are subjected to SNCR denitration reaction;
a waste heat recovery step: the outlet flue gas of the biomass boiler 300 enters the waste heat recovery device 20 to recover the waste heat in the flue gas, and the temperature of the flue gas is reduced;
a bag dust removal step: the flue gas from the waste heat recovery device 20 enters a bag-type dust collector 30 for dust collection, and the smoke dust in the flue gas is collected by the bag-type dust collector 30 and collected in a fly ash collection system 70 as fly ash;
an oxidation reaction step: the flue gas after the bag-type dust removal enters an oxidation reaction device 40 (such as a plasma reaction device or an ozone generator) for oxidation reaction, and NO in the flue gas is converted into NO2、N2O5And HNO3Part of SO in the flue gas2Is also converted into H2SO4；
An absorption step: enabling the flue gas after the oxidation reaction to enter an absorption tower 50, spraying alkali liquor into the absorption tower 50 through a spraying device 51, enabling acid substances in the flue gas to be absorbed by the sprayed alkali liquor, and meanwhile introducing a denitration additive into the absorption tower 50 or absorbing nitrogen oxide by adopting a wet desulphurization system slurry to realize synergistic denitration;
electric precipitation: the flue gas treated in the absorption step enters an electric dust collector 60 for dust removal, and the clean flue gas after dust removal is discharged.
Specifically, in the preliminary denitration step, a denitration agent is injected into the biomass boiler 300 through the SNCR denitration device 10, wherein the injection position of the SNCR denitration device 10 into which the denitration agent is injected is located at the upper part of the furnace of the biomass boiler 300 or the inlet of the cyclone.The sprayed denitrifier is urea or ammonia water, and the sprayed amount of the denitrifier is nitric oxide NO in the flue gasXIs 1.0 to 1.4 times the theoretical molar weight of (A). Thus, the fuel is combusted in the hearth of the biomass boiler 300, and the generated flue gas flows upwards to the upper part of the hearth or the inlet of the cyclone separator reacts with the injected denitrating agent to carry out SNCR primary denitration. Wherein the fuel is biomass and the like.
In the waste heat recovery step, the waste heat recovery device 20 adopts an air waste heat device, the flue gas at the outlet of the biomass boiler 300 enters an air preheater for waste heat recovery, and the temperature of the flue gas is reduced to 150 ℃ after the waste heat is recovered.
In the bag-type dust removing step, the bag-type dust remover 30 is made of heat-resistant and chemical-resistant PPS plastic (i.e., polyphenylene sulfide). The exhaust gas from the waste heat recovery device, such as the air preheater, enters the bag-type dust collector 30 for dust removal, the smoke dust in the exhaust gas is collected by the bag, and the collected ash is collected into the fly ash collection system 70 as fly ash.
In the oxidation reaction step, in an embodiment, the flue gas after being subjected to the bag-type dust removal is introduced into a low-temperature plasma reaction device through an induced draft fan 80 for plasma discharge treatment, and the low-temperature plasma reaction device generates high-energy electrons and oxygen radicals serving as active particles required by desulfurization and denitrification to convert NO in the flue gas into NO2、N2O5And HNO3。
In another embodiment, an ozone generator is used to replace a low-temperature plasma reaction device, and after the flue gas subjected to cloth bag dust removal enters the ozone generator, the ozone generator generates oxygen radicals required by deacidification and denitration to convert NO in the flue gas into NO2、N2O5And HNO3。
In the absorption step, the flue gas after the oxidation reaction further flows into the absorption tower 50, and the absorption tower 50 includes an absorption tower main body 51, a spray device 52, and a coordinated denitration device 53. Acidic substances in the flue gas enter an absorption tower main body 51 of the absorption tower 50 and are absorbed by alkali liquor sprayed by a spraying device 52. In order to improve the efficiency of absorbing acid substances by the alkali liquor, a circulating spraying device is adopted, the alkali liquor sprayed into the absorption tower main body 51 of the absorption tower 50 is sent into the spraying device 52 again for circulating spraying, and the reutilization is realized. Meanwhile, a denitration additive is introduced into the absorption tower main body 51 of the absorption tower 50 through the cooperative denitration device 53 or the slurry of the wet desulfurization system is adopted to absorb nitrogen oxide, so that cooperative denitration is realized in the wet absorption tower.
In an embodiment, while spraying the alkali solution into the absorption tower main body 51 of the absorption tower 50, the denitration additive is introduced into the absorption tower main body 51 of the absorption tower 50, and the denitration additive is Na2S、Na2SO3、(NH4)2SO3One or more of (a).
In another embodiment, the slurry of the wet desulfurization system is used to replace the denitration additive to absorb the nitrogen oxide, the bottom of the absorption tower main body 51 is provided with a first slurry tank, the slurry tank of the wet desulfurization system is communicated with the first slurry tank, and the slurry tank of the wet desulfurization system is used to absorb the SO2SO not oxidized later3 2-And absorbing the nitrogen oxide treated by the oxidation reaction by ions. A second slurry pool is additionally arranged outside the absorption tower main body 51 of the absorption tower 50, an oxidation device is arranged, the oxidation device in the first slurry pool is eliminated, and the slurry absorbing the nitrogen oxides enters the second slurry pool outside the tower to be oxidized, crystallized and discharged.
In the electric dust removal step, the flue gas deacidified by the absorption tower 50 enters an electric dust remover 60 for dust removal, the electric dust remover 60 is a wet-type electric dust remover, and the clean flue gas after electric dust removal is discharged from a chimney 400.
FIG. 2 is a desulfurization and denitrification purification system for incineration flue gas of a biomass boiler, which implements the process of the invention. As shown in fig. 2, the biomass boiler incineration flue gas desulfurization and denitration purification system includes an SNCR denitration device 10, a waste heat recovery device 20, a bag-type dust remover 30, an oxidation reaction device 40, an absorption tower 50, and an electric dust remover 60.
The SNCR denitration device 10 is a device that performs a denitration reaction on flue gas by using a selective non-catalytic reduction method (SNCR). The selective non-catalytic reduction (SNCR) method is characterized in that a reducing agent is sprayed into a temperature window suitable for denitration reaction to reduce nitrogen oxides in flue gas into harmless nitrogen and water; the technology generally adopts ammonia, urea or hydroammonic acid sprayed in a furnace as a reducing agent to reduce nitrogen oxides, and the reducing agent only reacts with the nitrogen oxides in the flue gas and does not generally react with oxygen; this technique does not employ a catalyst, so this method is called selective non-catalytic reduction (SNCR). The SNCR denitration device 10 comprises a denitration agent preparation storage mechanism 11 and a denitration agent atomization injection mechanism 12, wherein the denitration agent preparation storage mechanism 11 is communicated with the denitration agent atomization injection mechanism 12. The denitration agent atomization and injection mechanism 12 injects the denitration agent into the biomass boiler 300, so that the flue gas generated by burning the fuel in the hearth of the biomass boiler 300 and the denitration agent are subjected to SNCR denitration reaction, and preliminary denitration is realized. The spraying position of the denitration agent atomizing and spraying mechanism 12 of the SNCR denitration device 10 is located at the upper part of the furnace of the biomass boiler 300.
The waste heat recovery device 20 is communicated with the biomass boiler 300, so that the flue gas in the biomass boiler 300 enters the waste heat recovery device 20 to recover the waste heat of the flue gas. Optionally, the heat recovery device 20 is an air preheater.
The bag-type dust collector 30 is communicated with the waste heat recovery device 20, so that the flue gas coming out of the waste heat recovery device 20 enters the bag-type dust collector 30. The bag-type dust collector 30 collects the dust entrained in the flue gas. The bag-type dust collector 30 is made of heat-resistant and chemical-resistant PPS plastic (polyphenylene sulfide). Specifically, the bag-type dust collector 30 includes an inlet flue, an outlet flue, a filter bag, and an ash discharge hopper, and the inlet flue of the bag-type dust collector 30 is communicated with the outlet flue of the waste heat recovery device 20, such as an air preheater. The filter bag of the bag-type dust collector 30 is mainly used for collecting the smoke dust mixed in the smoke.
The biomass boiler incineration flue gas desulfurization and denitration purification system further comprises a fly ash collecting system 70, the fly ash collecting system 70 is communicated with the bag-type dust collector 30, and the smoke dust collected by the bag-type dust collector 30 is attached to the filter bag as fly ash and collected in the fly ash collecting system 70 in a vibration sedimentation mode.
The biomass boiler incineration flue gas desulfurization and denitration purification system further comprises an induced draft fan 80, wherein the induced draft fan 80 is provided with an inlet flue and an outlet flue, and the inlet flue of the induced draft fan 80 is communicated with the outlet flue of the bag-type dust collector 30. The induced draft fan 80 is used for overcoming the resistance generated by the whole system so as to convey the flue gas to the chimney 400.
The oxidation reaction device 40 is communicated with the bag-type dust collector 30 through an induced draft fan 80. That is, the induced draft fan 80 is communicated between the bag-type dust collector 30 and the oxidation reaction device 40 and used for conveying the flue gas. The flue gas dedusted by the bag-type dust remover 30 enters the oxidation reaction device 40 for oxidation reaction under the introduction action of the induced draft fan 80 so as to convert NO in the flue gas into NO2、N2O5And HNO3Part of SO in the flue gas2Is also converted into H2SO4. Alternatively, the oxidation reaction apparatus 40 is a plasma reaction apparatus, and for example, a low-temperature plasma reaction apparatus may be used. The plasma reaction device is internally provided with a plurality of discharge units 41, each discharge unit 41 mainly comprises a high-voltage electrode, a ground level and an air gap channel, and a pulse power supply 90 is adopted as a power supply. The low-temperature plasma reaction device discharges under the action of the pulse power supply 90 and generates high-energy electrons and oxygen radicals which can be used as active particles required by desulfurization and denitrification to convert NO in flue gas into NO2、N2O5And HNO3Part of SO in the flue gas2Is also converted into H2SO4。
The absorption tower 50 includes an absorption tower main body 51, a shower device 52, and a cooperative denitration device 53. The absorption tower main body 51 is communicated with the oxidation reaction device 40, so that the flue gas after the oxidation reaction enters the absorption tower main body 51. The inlet flue section within 2m from the tower wall of the absorption tower main body 51 is made of an alloy anticorrosive material, and the absorption tower main body 51 is made of carbon steel lined with glass flakes. The top of the absorption tower main body 51 is provided with a demisting device to reduce the content of fog drops in the flue gas. The bottom of the absorption tower main body 51 is provided with a first slurry tank.
The spraying device 52 is disposed inside the absorption tower main body 51 and sprays alkali liquor into the absorption tower main body 51, so that acidic substances in the flue gas in the absorption tower main body 51 are absorbed by the sprayed alkali liquor, and residual pollutants in the flue gas are removed. The first slurry tank of the absorption tower main body 51 is communicated with the spraying device 52, and the alkali liquor sprayed out of the spraying device 52 is recovered and stored in the first slurry tank of the absorption tower main body 51 and is sent into the spraying device 52 again for circular spraying.
The cooperative denitration device 53 is communicated with the absorption tower main body 51, and the cooperative denitration device 53 introduces denitration additives or slurry of a wet desulfurization system into the absorption tower main body 51 so as to absorb nitrogen oxides in flue gas, thereby realizing cooperative denitration.
As shown in fig. 2, the flue gas treated by the oxidation reaction device 40 (i.e. the low-temperature plasma reaction device) further flows into the absorption tower 50, and the small-molecule acidic substances in the flue gas enter the absorption tower main body 51 and are absorbed by the alkali liquor circularly sprayed by the spraying device 52. Simultaneously, a denitration additive is introduced into the absorption tower main body 51 through the cooperative denitration device 53 to absorb NO2And the cooperative desulfurization and denitrification in the wet absorption tower are realized. The denitration additive is Na2S、Na2SO3、(NH4)2SO3And the like.
The electric dust remover 60 is communicated with the absorption tower 50, and the flue gas enters the electric dust remover 60 from the absorption tower 50 to remove dust. The electrostatic precipitator 60 selects a wet electrostatic precipitator, high-voltage corona discharge is performed in the wet electrostatic precipitator to charge dust, the charged dust reaches the dust collecting plate/pipe under the action of electric field force, and liquid scours the surface of the dust collecting electrode to remove ash, so that fine particles can be effectively collected. The clean flue gas after dust removal is discharged from the chimney 400.
In another embodiment, the flue gas after combustion in the hearth of the biomass boiler 300 is firstly subjected to preliminary denitration by the SNCR denitration device 10, the denitration agent preparing and storing mechanism 11 and the denitration agent atomizing and spraying mechanism 12 of the SNCR denitration device 10 are both arranged on the upper portion of the hearth of the biomass boiler 300, that is, the spraying position of the denitration agent atomizing and spraying mechanism 12 is located on the upper portion of the hearth of the biomass boiler 300. The flue gas after the preliminary denitration enters a waste heat recovery device 20 to recover the flue gas waste heat, and the temperature of the flue gas is reduced to about 150 ℃. The cooled flue gas enters the bag-type dust collector 30 for dust collection, and the flue dust is collected by the bag-type dust collector 30 and is collected into the fly ash collection system 70 as fly ash. Introducing the flue gas subjected to cloth bag dust removal into an oxidation reaction device 40 through an induced draft fan 80, wherein the oxidation reaction device 40 is a low-temperature plasma reaction device; in the pulseThe low-temperature plasma reaction device generates discharge reaction and generates a large amount of high-energy electrons under the action of the charging source, the high-energy electrons attack active components such as oxygen, water molecules and the like carried in the smoke to generate active particles such as oxygen free radicals, hydroxyl free radicals and the like, and the active particles convert NO which is not easily absorbed in the smoke into NO which is easily absorbed by alkali liquor2、N2O5And HNO3Part of SO2Is also converted into H2SO4. The flue gas treated by the oxidation reaction device 40 (i.e. the low-temperature plasma reaction device) is introduced into the absorption tower 50, and the residual small molecular acid in the flue gas is absorbed by the sprayed alkali liquor in the absorption tower main body 51 of the absorption tower 50. While Na is added to the first slurry tank of the absorption tower main body 51 through the cooperative denitrification device 532S、Na2SO3、(NH4)2SO3One or more denitration additives for absorbing NO in the flue gas2And the like. The flue gas after deacidification and denitration is discharged from the chimney 400 to the outside after fog drops are removed by the demister at the top of the absorption tower main body 51 and then enters the electric dust collector 60 to further remove residual dust.
In yet another embodiment, the flue gas after combustion in the hearth of the biomass boiler 300 is first subjected to preliminary denitration by the SNCR denitration device 10, wherein the denitration agent preparing and storing mechanism 11 and the denitration agent atomizing and spraying mechanism 12 of the SNCR denitration device 10 are provided with cyclone inlets, i.e. the spraying position of the denitration agent atomizing and spraying mechanism 12 is located at the cyclone inlets. The flue gas after the preliminary denitration enters a waste heat recovery device 20 to recover the flue gas waste heat, and the temperature of the flue gas is reduced to about 150 ℃. The cooled flue gas enters the bag-type dust collector 30 for dust collection, and the flue dust is collected by the bag-type dust collector 30 and is collected into the fly ash collection system 70 as fly ash. The flue gas after the bag-type dust removal is introduced into the absorption tower 50 through the induced draft fan 80. A branch pipe is arranged in a flue communicated between the bag-type dust collector 30 and the absorption tower 50 and is connected with an ozone generator to be used as an oxidation reaction device 40. The oxidation reaction device 40, i.e. the ozone generator, generates ozone which reacts with the circulating flue gas in the flue and oxidizes NO which is not easily absorbed into NO2、N2O5And HNO3Partial SO2Is also converted into H2SO4. In the absorption tower 50, the oxidized residual substances in the flue gas are absorbed by the alkali liquor sprayed by the spraying device 52. The cooperative denitration device 53 is a slurry tank of the wet desulfurization system and is communicated with the first slurry tank of the absorption tower main body 51. The rest of the slurry in the slurry pool of the wet desulphurization system is introduced into the absorption tower main body 51 of the absorption tower 50 while being sprayed, and a large amount of SO in the slurry of the wet desulphurization system is utilized3 2-Ion absorption of NO2The purpose of absorbing nitrogen oxide is realized. The absorption tower 50 further comprises a second slurry tank arranged outside the absorption tower main body 51, an oxidation device is arranged inside the second slurry tank, and slurry after the coordinated denitration reaction enters the second slurry tank and is discharged outside after being oxidized and crystallized by the oxidation device in the second slurry tank. And the flue gas after desulfurization and denitrification enters the electric dust collector 60 after fog drops are removed by the demister at the top of the absorption tower main body 51 so as to further remove residual dust. The clean flue gas after electric precipitation is discharged from the chimney 400.
It will be appreciated by persons skilled in the art that the embodiments of the invention described above and shown in the drawings are given by way of example only and are not limiting of the invention. The objects of the invention have been fully and effectively accomplished. The functional and structural principles of the present invention have been shown and described in the examples, and the embodiments of the present invention may be subject to any changes or modifications without departing from the principles.

Claims (10)

1. A desulfurization and denitrification purification process for incineration flue gas of a biomass boiler is characterized by comprising the following steps of:
a primary denitration step: spraying a denitration agent into the biomass boiler, so that the flue gas generated after the fuel is combusted in the hearth of the biomass boiler and the denitration agent are subjected to SNCR denitration reaction;
a waste heat recovery step: enabling the outlet flue gas of the biomass boiler to enter a waste heat recovery device to recover waste heat in the flue gas, and reducing the temperature of the flue gas;
a bag dust removal step: the flue gas from the waste heat recovery device enters a bag-type dust collector for dust removal, and the smoke dust in the flue gas is collected by the bag-type dust collector and collected in a fly ash collection system as fly ash;
an oxidation reaction step: the flue gas after the bag dust removal enters a plasma reaction device or an ozone generator for oxidation reaction, and NO in the flue gas is converted into NO2、N2O5And HNO3Part of SO in the flue gas2Is also converted into H2SO4；
An absorption step: enabling the flue gas after the oxidation reaction to enter an absorption tower, spraying alkali liquor into the absorption tower through a spraying device, enabling acid substances in the flue gas to be absorbed by the sprayed alkali liquor, and simultaneously introducing a denitration additive into the absorption tower or absorbing nitrogen oxide by adopting a wet desulphurization system slurry to realize synergistic denitration;
electric precipitation: and (4) allowing the flue gas treated in the absorption step to enter an electric dust remover for dust removal, and discharging the clean flue gas after dust removal.
2. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler as recited in claim 1, wherein in the step of combustion and denitrification, a denitration agent is injected into the biomass boiler through an SNCR denitration device, wherein the injection position of the SNCR denitration device for injecting the denitration agent is located at the upper part of the furnace chamber of the biomass boiler or at the inlet of the cyclone separator.
3. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler as recited in claim 1 or 2, wherein in the step of combustion and denitrification, the injected denitrifying agent is urea or ammonia water, and the injection amount of the denitrifying agent is 1.0-1.4 times of the theoretical value of the molar weight of the nitrogen oxides in the flue gas.
4. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler as recited in claim 1, wherein in the waste heat recovery step, an air waste heat device is adopted as the waste heat recovery device, and the temperature of the flue gas is reduced to 150 ℃ after the waste heat is recovered.
5. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler as recited in claim 1, wherein in the bag-type dust removal step, the bag-type dust remover is made of PPS plastic with heat resistance and chemical resistance.
6. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler as recited in claim 1, wherein in the oxidation reaction step, the flue gas subjected to the bag-type dust removal is introduced into a low-temperature plasma reaction device through a draught fan for plasma discharge treatment, and the low-temperature plasma reaction device generates high-energy electrons and oxygen radicals serving as active particles required for desulfurization and denitrification to convert NO in the flue gas into NO2、N2O5And HNO3。
7. The desulfurization, denitrification and purification process for incineration flue gas of biomass boiler according to claim 1, wherein in the absorption step, the denitrification additive is Na2S、Na2SO3、(NH4)2SO3One or more of (a).
8. The desulfurization, denitrification and purification process for incineration flue gas of a biomass boiler as recited in claim 1, wherein in the absorption step, the nitrogen oxides are absorbed by using a wet desulfurization system slurry, the absorption tower has an absorption tower main body, a first slurry tank is arranged at the bottom of the absorption tower main body, the wet desulfurization system slurry tank is communicated with the first slurry tank of the absorption tower, and the absorption of SO in the wet desulfurization system slurry tank is utilized2SO not oxidized later3 2-And absorbing the nitrogen oxide treated by the oxidation reaction by ions.
9. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler according to claim 8, wherein in the absorption step, a second slurry tank is arranged outside the absorption tower main body, an oxidation device is installed, and the slurry after absorbing the nitrogen oxides enters the second slurry tank outside the tower to be oxidized, crystallized and discharged.
10. The desulfurization, denitrification and purification process for the incineration flue gas of the biomass boiler as recited in claims 7 to 9, wherein in the absorption step, the alkali liquor sprayed into the absorption tower is fed into the spray device again for circulating spray.
CN201910898013.8A 2019-09-23 2019-09-23 Desulfurization and denitrification purification process for incineration flue gas of biomass boiler Pending CN110711470A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201910898013.8A CN110711470A (en) 2019-09-23 2019-09-23 Desulfurization and denitrification purification process for incineration flue gas of biomass boiler

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201910898013.8A CN110711470A (en) 2019-09-23 2019-09-23 Desulfurization and denitrification purification process for incineration flue gas of biomass boiler

Publications (1)

Publication Number Publication Date
CN110711470A true CN110711470A (en) 2020-01-21

Family

ID=69210740

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201910898013.8A Pending CN110711470A (en) 2019-09-23 2019-09-23 Desulfurization and denitrification purification process for incineration flue gas of biomass boiler

Country Status (1)

Country Link
CN (1) CN110711470A (en)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111450683A (en) * 2020-05-08 2020-07-28 北京金大万翔环保科技有限公司 Biomass boiler flue gas ozone oxidation denitration process and equipment
CN111905565A (en) * 2020-07-14 2020-11-10 杭州中荷环保科技有限公司 Plasma co-processing device and processing method for waste gas of kerosene engine
CN112588030A (en) * 2020-12-27 2021-04-02 太仓市兴益机电设备制造有限公司 Flue gas multistage purification and waste heat utilization system for biomass burner
CN113634104A (en) * 2021-08-25 2021-11-12 北京嘉博文生物科技有限公司 Treatment process of waste gas generated in kitchen waste treatment process
RU2818476C1 (en) * 2023-03-09 2024-05-02 Пекин Чжун Син Хуэй Жун Энерджи Сейвинг Текнолоджи Ко., Лтд. Ash collection system

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111450683A (en) * 2020-05-08 2020-07-28 北京金大万翔环保科技有限公司 Biomass boiler flue gas ozone oxidation denitration process and equipment
CN111905565A (en) * 2020-07-14 2020-11-10 杭州中荷环保科技有限公司 Plasma co-processing device and processing method for waste gas of kerosene engine
CN112588030A (en) * 2020-12-27 2021-04-02 太仓市兴益机电设备制造有限公司 Flue gas multistage purification and waste heat utilization system for biomass burner
CN113634104A (en) * 2021-08-25 2021-11-12 北京嘉博文生物科技有限公司 Treatment process of waste gas generated in kitchen waste treatment process
RU2818476C1 (en) * 2023-03-09 2024-05-02 Пекин Чжун Син Хуэй Жун Энерджи Сейвинг Текнолоджи Ко., Лтд. Ash collection system

Similar Documents

Publication Publication Date Title
CN110711470A (en) Desulfurization and denitrification purification process for incineration flue gas of biomass boiler
CN110860196B (en) Desulfurization and denitrification system for cement flue gas
CN101485957B (en) Device and method of simultaneous desulfuration and denitration for flue gas using ozone oxygenation combined with double-tower washing
CN211302635U (en) Biomass boiler burns flue gas desulfurization denitration clean system
CN210107409U (en) Hazardous waste burns flue gas clean system
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
CN101810993B (en) Method for achieving high effective mercury removal through modifying electrostatic precipitator
MXPA04006507A (en) Exhaust gas treatment system.
CN106524205B (en) Ultra-low emission purification equipment for flue gas of coal-fired industrial furnace
CN212188526U (en) Flue gas treatment system after sludge treatment
CN110787630A (en) Flue gas treatment device and process for semi-dry desulfurization and low-temperature SCR denitration of carbide slag
KR101567746B1 (en) Apparatus for treating exhaust gas
CN105169943A (en) Integrated system for coke oven flue gas desulfurization and denitrification and waste heat recovery
CN102371113A (en) Flue gas purifying treatment method and system
CN205127750U (en) Desulphurization of exhaust gas denitration of coke oven flue and waste heat recovery's integrated system
CN204582930U (en) A kind of low cost coal-fired flue-gas multiple pollutant minimum discharge system
CN113776061A (en) Hazardous waste incineration flue gas purification and waste heat recovery device and method thereof
CN105251325A (en) Sintering flue gas circulating fluidized bed desulfurization and denitrification system and method
CN205102149U (en) Multiple gas cleaning is demercuration device in coordination
CN106178877A (en) A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique
CN106076106A (en) A kind of semi-dry desulfurization and denitrification system and method based on biomass ash
CN109260919A (en) The integration desulfurization denitration device and its desulfurization denitration method of ozone combination urea
CN105222143A (en) Mercury removal device and method are worked in coordination with in one kind of multiple gas cleanings
CN107952296A (en) A kind of agglomerates of sintered pellets flue gas multiple pollutant cooperated purification system based on bag-type dusting
CN218741209U (en) Useless active carbon pyrolysis regeneration gas cleaning system of danger

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination