CN116262198A - Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas - Google Patents
Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas Download PDFInfo
- Publication number
- CN116262198A CN116262198A CN202210234575.4A CN202210234575A CN116262198A CN 116262198 A CN116262198 A CN 116262198A CN 202210234575 A CN202210234575 A CN 202210234575A CN 116262198 A CN116262198 A CN 116262198A
- Authority
- CN
- China
- Prior art keywords
- type dust
- bag
- flue gas
- deacidification
- dust collector
- 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
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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- 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
- B01D46/0002—Casings; Housings; Frame constructions
- B01D46/0012—In-line filters
-
- 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
- B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
-
- 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
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/06—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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
- B01D53/685—Halogens or halogen compounds by treating the gases with solids
-
- 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
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- 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
- B01D2258/0291—Flue gases from waste incineration plants
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas, which comprises a slaked lime storage injection system, a primary bag-type dust remover, a baking soda storage injection system, an activated carbon storage injection system, a reaction tower, a secondary bag-type dust remover, a compressed air system and an ash conveying system; the invention adopts a two-stage dry desulfurization deacidification dust removal technology, and one-stage dry desulfurization deacidification dust removal technologySpraying slaked lime powder into the inlet of the primary bag-type dust collector for a slaked lime desulfurization deacidification dust removal system; the second level is a baking soda desulfurization deacidification dust removal system, and baking soda powder (NaHCO) is sprayed in front of the reaction tower 3 ) The whole process has high desulfurization and deacidification dust removal efficiency and low emission concentration, can overcome the problem of low efficiency of the traditional dry desulfurization and deacidification, and can realize SO 2 HCl and dust are discharged in ultralow, the heat loss of the smoke is low, the smoke heating cost of a subsequent low-temperature SCR denitration system can be reduced, the dry desulfurization moisture content is low, the smoke is dissipated after being discharged, and white smoke is not generated.
Description
Technical Field
The invention relates to the technical field of flue gas purification systems, in particular to a two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas.
Background
Garbage incineration is an important technology for treating domestic garbage in China, and is used as a treatment technology with the most thorough harmless treatment, the most obvious volume reduction and the highest recycling degree. The refuse incineration can produce toxic and harmful gases such as SO 2 How to control the emission concentration of pollutants in incineration flue gas, such as HCl, HF, dioxin, etc., has been widely paid attention to, and in order to avoid secondary pollution, the waste incineration flue gas must be subjected to purification treatment.
Experiments prove that the higher the smoke temperature is, the easier the smoke temperature is diffused, the more humid the smoke is, the more difficult the smoke is diffused, and the haze is formed. With the gradual strict environmental protection requirements, the white smoke plume is required to be treated, which is commonly called as 'white smoke elimination'. Both wet desulfurization and semi-dry desulfurization can spray water or slurry into the flue gas, so that the humidity of the flue gas is saturated and the temperature of the flue gas is low. The saturated flue gas is reduced in temperature in the process of mixing and diffusing with the atmosphere, water in the flue gas is separated out, and white fog is formed around a chimney, so that the saturated flue gas is a main reason for forming common white smoke plumes.
In general, the content of HCl in acid gas of waste incineration flue gas is highest, HF and SO 2 Relatively low, they can cause corrosion to incinerators and boilers in addition to the pollution environment, and their treatment processes are classified into dry, semi-dry and wet methods. The dry method is to spray slaked lime or sodium bicarbonate directly into the flue and assist a subsequent high-efficiency dust remover. The process comprisesThe process is simple, the maintenance is convenient, but the deacidification effect is poor, and the national standard GB 1885-2014 emission requirement is not met. The semi-dry method is to spray Ca (OH) 2 slurry through a deacidification tower, atomize the slurry into fine mist droplets in the deacidification tower to react with acidic substances, so as to achieve the removal purpose, but the semi-dry method can only meet the current national standard emission, and cannot meet the further ultra-low emission requirement. The wet method adopts a washing tower for washing, and utilizes alkaline absorbent such as NaOH and the like to absorb acid gas in the washing tower. The wet method has high removal rate, although the wet method can meet the requirements of HCl and SO 2 The ultra-low emission requirement, however, the complex flow and the treatment process can reduce the temperature of the flue gas, the white flue gas needs to be eliminated by reheating before the flue gas is discharged from the chimney, the sewage which generates a large amount of high-concentration chloride salt and heavy metal needs to be treated, and the treatment cost is high.
With the increasingly strict emission of flue gas, the emission standard of national Tianjin, hebei and other provincial garbage flue gas places is gradually required to be ultra-low, and the ultra-low emission standard is that the dust is less than or equal to 10 mg/Nm 3 、HCl：10mg/Nm 3 、SO 2 ：20mg/Nm 3 、NOx:80 mg/Nm 3 . To meet NOx emissions of less than 80 mg/Nm 3 The low-temperature SCR denitration system is required to be additionally arranged behind the flue gas purification system. The wet desulfurization exhaust temperature is 50 ℃, the semi-dry desulfurization exhaust temperature is 150 ℃, the low-temperature SCR denitration reaction temperature is 220-230 ℃, a large amount of steam is consumed for flue gas temperature rise, and the operation cost is too high.
Disclosure of Invention
The invention aims to provide a two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas, which can solve the problem of low desulfurization efficiency of the traditional dry/semi-dry desulfurization technology and avoid the problems of wet desulfurization white flue gas, waste water and the like.
In order to achieve the above purpose, the present invention provides the following technical solutions:
a two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas comprises a slaked lime storage injection system, a primary bag-type dust remover, a baking soda storage injection system, an active carbon storage injection system, a reaction tower, a secondary bag-type dust remover, a compressed air system and an ash conveying system; the specific process steps are as follows:
s1: boiler tail gas enters a primary desulfurization and deacidification system: an inlet flue is arranged on the primary bag-type dust collector, slaked lime powder is sprayed into the inlet flue of the primary bag-type dust collector through a slaked lime storage and spraying system to perform pre-desulfurization and deacidification, the filtering wind speed is less than or equal to 0.7 m/min, and the reaction process is as follows:
Ca(OH) 2 + SO 2 + 1/2O 2 → CaSO 4 + H 2 O；
Ca(OH) 2 + 2HCl → CaCl 2 + 2H 2 O；
s2: the flue gas enters a secondary desulfurization deacidification system after being filtered by a primary bag-type dust collector, firstly enters a reaction tower, and sodium bicarbonate powder and active carbon powder are respectively sprayed into a flue at the lower part of the reaction tower through a sodium bicarbonate storage injection system and an active carbon storage injection system, and are fully mixed with the flue gas in the reaction tower;
s3: after passing through the reaction tower, sodium bicarbonate and active carbon enter a secondary bag-type dust collector, a filter cake layer on the surface of a filter bag of the secondary bag-type dust collector continuously reacts with acid gas, and the filtering wind speed is less than or equal to 0.7 m/min to carry out long-time stay reaction;
s4: the flue gas after reaction purification is sent into a chimney through the action of an induced draft fan to be discharged into the atmosphere, and desulfurization products are discharged to an ash conveying system through an ash hopper at the bottom of the secondary bag-type dust collector and are conveyed to a plant fly ash curing system through the ash conveying system.
Further, the primary bag-type dust remover is connected with a boiler tail gas conveying pipeline, and the boiler tail gas conveying pipeline is in butt joint with an injection port of the slaked lime storage injection system; the flue gas outlet of the primary bag-type dust collector is connected with the reaction tower through a pipeline, and the flue gas inlet at the bottom of the reaction tower is respectively in butt joint with the injection ports of the baking soda storage injection system and the active carbon storage injection system; the outlet end of the reaction tower is connected with a secondary bag-type dust remover through a pipeline, and a draught fan is arranged at the smoke outlet of the secondary bag-type dust remover; the compressed air system is respectively connected with the primary bag-type dust collector and the secondary bag-type dust collector in a control way through a pipe valve structure, and air bags with back blowing structures are arranged on filter bags of the primary bag-type dust collector and the secondary bag-type dust collector; and ash hoppers at the bottoms of the primary bag-type dust collector and the secondary bag-type dust collector are connected with an ash conveying system through pipelines.
Further, the slaked lime powder in S1 is stored in a slaked lime bin, is sprayed into a flue through a spraying system, enters a first-stage bag-type dust collector and is attached to a filter bag to form a filter cake layer, the filter cake layer is contacted with flue gas for a long time, after the filter cake layer reaches a certain thickness, a bag differential pressure signal starts a compressed air system to blow back the filter bag, and ash hoppers of which filter cakes fall to the bottom of the first-stage bag-type dust collector are sent to an ash conveying system to start the next purification period.
Further, S3 sodium bicarbonate and residual SO in the flue gas 2 Reacting with HCl acid gas, and adsorbing dioxin and heavy metal pollutants in the flue gas by using activated carbon; at the smoke temperature of 190-200 ℃ and NaHCO 3 With SO 2 There are two reaction pathways for HCl:
(1) the direct reaction:
2NaHCO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + 2CO 2 + H 2 O
NaHCO 3 + HCl → NaCl + CO 2 + H 2 O
② NaHCO 3 and (3) performing post-pyrolysis reaction:
2NaHCO 3 + (Heat) → Na 2 CO 3 + CO 2 + H 2 O
Na 2 CO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + CO 2
Na 2 CO 3 + 2HCl → 2NaCl + CO 2 + H 2 O。
further, the slaked lime storage injection system and the primary bag-type dust remover form a primary desulfurization and deacidification system.
Further, the baking soda storage and injection system, the activated carbon storage and injection system, the reaction tower and the secondary bag-type dust remover form a secondary desulfurization and deacidification system.
Furthermore, the primary bag-type dust remover, the reaction tower and the secondary bag-type dust remover are provided with a plurality of groups in a matching way, and single-channel operation or double-channel parallel operation can be realized according to the flue gas quantity.
Compared with the prior art, the invention has the beneficial effects that:
1. the two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention can be flexibly used according to single-channel operation or double-channel parallel operation of the flue gas quantity.
2. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention has the advantages of large flue gas treatment amount, simple system, small occupied area, stable operation and less maintenance workload.
3. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention has the advantages of high reaction efficiency, high utilization rate of deacidification agent, saving of deacidification agent compared with the traditional dry desulfurization, and low operation cost.
4. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention has the advantages that no high-salt wastewater is generated, and a wastewater treatment system is not needed.
5. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention has very high desulfurization deacidification dust removal efficiency, and the emission index can reach the ultralow emission standard.
6. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention has the advantages that white smoke is not generated, the flue gas can be discharged without whitening, the increasingly strict flue gas whitening requirement is met, and the investment is saved.
7. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas provided by the invention has the advantages that the discharged flue gas is high, the steam consumption of the subsequent low-temperature SCR system flue gas temperature rise can be saved, and the construction cost and the operation cost of the SCR system are reduced.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
FIG. 2 is a process flow diagram of the present invention;
FIG. 3 is a diagram of a two-channel parallel two-stage dry desulfurization and deacidification dust removal structure of the invention.
In the figure: 1. a slaked lime storage injection system; 2. a primary bag-type dust collector; 3. a baking soda storage injection system; 4. an activated carbon storage injection system; 5. a reaction tower; 6. a secondary bag-type dust collector; 7. a compressed air system; 8. an ash conveying system; 9. an induced draft fan; 10. and an inlet flue.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Referring to fig. 1, the embodiment of the invention provides a two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas, which comprises a slaked lime storage injection system 1, a primary bag-type dust remover 2, a baking soda storage injection system 3, an activated carbon storage injection system 4, a reaction tower 5, a secondary bag-type dust remover 6, a compressed air system 7 and an ash conveying system 8; the specific process steps are as follows:
s1: boiler tail gas enters a primary desulfurization and deacidification system: an inlet flue 10 is arranged on the primary bag-type dust collector 2, slaked lime powder is sprayed into the inlet flue 10 of the primary bag-type dust collector 2 through a slaked lime storage and spraying system 1 to perform pre-desulfurization and deacidification, and the filtering wind speed is less than or equal to 0.7 m/min and SO 2 The removal efficiency is 40-50%, and the HCl removal efficiency is 60-70%; wherein, the reaction process of lime hydrate desulfurization and deacidification is as follows:
Ca(OH) 2 + SO 2 + 1/2O 2 → CaSO 4 + H 2 O；
Ca(OH) 2 + 2HCl → CaCl 2 + 2H 2 O；
the slaked lime powder is stored in a slaked lime bin, is sprayed into a flue through a spraying system, enters a primary bag-type dust remover 2, is attached to a filter bag, forms a filter cake layer, has long contact time with flue gas, and has good desulfurization and deacidification efficiency; after the filter cake layer reaches a certain thickness, the compressed air is started to reversely blow the filter bag by a cloth bag differential pressure signal, the filter cake falls into an ash bucket to start the next purification period, the concentration of acid gas is reduced after the flue gas is filtered by the primary cloth bag dust collector 2, and the dust concentration is less than 20 mg/Nm 3 。
S2: the flue gas enters a secondary desulfurization deacidification system after being filtered by a primary bag-type dust collector 2, firstly enters a reaction tower 5, and sodium bicarbonate powder and activated carbon powder are respectively sprayed into a flue at the lower part of the reaction tower 5 through a sodium bicarbonate storage spraying system 3 and an activated carbon storage spraying system 4, and are fully mixed with the flue gas in the reaction tower 5; turbulent flow is formed through the special structure in the interior, the particles are rubbed with each other, the specific surface area is fully improved, the absorbent concentration is high, and the deacidification speed is high.
S3: after passing through the reaction tower 5, the baking soda and the activated carbon enter a secondary bag-type dust collector 6, the filter cake layer on the surface of a filter bag of the secondary bag-type dust collector 6 continuously reacts with the acid gas, the filtering wind speed is less than or equal to 0.7 m/min, and the reaction is carried out for a long time, so that the reaction is more complete, and the dust in the flue gas is removed, the contact area of the deacidification agent and the flue gas is larger, the reaction is more complete, and the reaction efficiency is high; wherein, the baking soda and the residual SO in the flue gas 2 Carrying out HCl reaction, and adsorbing pollutants such as dioxin, heavy metals and the like in the flue gas by using activated carbon;
at the smoke temperature of 190-200 ℃ and NaHCO 3 With SO 2 There are two reaction pathways for HCl:
(1) the direct reaction:
2NaHCO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + 2CO 2 + H 2 O
NaHCO 3 + HCl → NaCl + CO 2 + H 2 O
② NaHCO 3 and (3) performing post-pyrolysis reaction:
2NaHCO 3 + (Heat) → Na 2 CO 3 + CO 2 + H 2 O
Na 2 CO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + CO 2
Na 2 CO 3 + 2HCl → 2NaCl + CO 2 + H 2 O
active NaHCO 3 The powder is quickly pyrolyzed and converted into CO after being contacted with hot flue gas 2 And Na (Na) 2 CO 3 Extremely largeImprove NaHCO 3 Porosity and specific surface area of the particles, while renewing the Na that survived 2 CO 3 Thereby promoting SO 2 Contact of acid gases such as HCl and the like with a base desulfurizing agent to improve SO 2 And HCl removal rate.
S4: after the flue gas is subjected to two-stage dry desulfurization, deacidification, dust removal and purification, SO (SO) 2 The removal rate is more than 95 percent (600-20 mg/Nm) 3 ) The HCl removal rate is more than 99 percent (1200-10 mg/Nm) 3 ) The dust removal rate is more than 99.8 percent (5000-8 mg/Nm) 3 ) Can realize ultra-low emission of pollutants: SO (SO) 2 ≤20 mg/Nm 3 ，HCl≤10 mg/Nm 3 Dust is less than or equal to 10 mg/Nm 3 The purified flue gas is sent into a chimney through the action of a draught fan 9 to be discharged into the atmosphere, and the desulfurization product is discharged to an ash conveying system 8 through an ash hopper of a bag-type dust collector and is conveyed to a plant fly ash curing system through the ash conveying system 8.
Referring to fig. 2, in the embodiment of the present invention, a first-stage bag-type dust collector 2 is connected to a boiler tail gas delivery pipe, and the boiler tail gas delivery pipe is in butt joint with an injection port of a slaked lime storage injection system 1; the flue gas outlet of the primary bag-type dust collector 2 is connected with a reaction tower 5 through a pipeline, and the flue gas inlet at the bottom of the reaction tower 5 is respectively in butt joint with the jet ports of the baking soda storage jet system 3 and the active carbon storage jet system 4; the outlet end of the reaction tower 5 is connected with a secondary bag-type dust remover 6 through a pipeline, and a draught fan 9 is arranged at the smoke outlet of the secondary bag-type dust remover 6; the compressed air system 7 is respectively connected with the primary bag-type dust collector 2 and the secondary bag-type dust collector 6 in a control way through a pipe valve structure, and air bags with back blowing structures are arranged on filter bags of the primary bag-type dust collector 2 and the secondary bag-type dust collector 6; the ash hoppers at the bottoms of the primary bag-type dust collector 2 and the secondary bag-type dust collector 6 are connected with an ash conveying system 8 through pipelines; wherein, the slaked lime storage injection system 1 and the primary bag-type dust remover 2 form a primary desulfurization and deacidification system; the baking soda storage and injection system 3, the active carbon storage and injection system 4, the reaction tower 5 and the secondary bag-type dust remover 6 form a secondary desulfurization and deacidification system.
Referring to fig. 3, in the embodiment of the present invention, a plurality of groups of primary bag-type dust collectors 2, reaction towers 5 and secondary bag-type dust collectors 6 are provided in a matching manner, so that single-channel operation or dual-channel parallel operation can be realized according to the flue gas amount.
To sum up: the invention provides a two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas, which is mainly used for tail gas SO of a waste incineration power plant 2 Removing HCl and dust, wherein a two-stage dry desulfurization and deacidification dust removal technology is adopted, a primary stage is a slaked lime desulfurization and deacidification dust removal system, and slaked lime powder is sprayed into an inlet of a primary bag-type dust remover 2; the second level is a baking soda desulfurization deacidification dust removal system, baking soda powder (NaHCO) is sprayed in front of the reaction tower 5 3 ) The whole process has high desulfurization and deacidification dust removal efficiency and low emission concentration, can overcome the problem of low efficiency of the traditional dry desulfurization and deacidification, and can realize SO 2 HCl and dust are discharged in ultralow, the heat loss of the smoke is low, the smoke heating cost of a subsequent low-temperature SCR denitration system can be reduced, the dry desulfurization moisture content is low, the smoke is dissipated after being discharged, and white smoke is not generated.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should be covered by the protection scope of the present invention by making equivalents and modifications to the technical solution and the inventive concept thereof.
Claims (7)
1. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas is characterized by comprising a slaked lime storage injection system (1), a primary bag-type dust remover (2), a baking soda storage injection system (3), an activated carbon storage injection system (4), a reaction tower (5), a secondary bag-type dust remover (6), a compressed air system (7) and an ash conveying system (8); the specific process steps are as follows:
s1: boiler tail gas enters a primary desulfurization and deacidification system: an inlet flue (10) is arranged on the primary bag-type dust collector (2), slaked lime powder is sprayed into the inlet flue (10) of the primary bag-type dust collector (2) through a slaked lime storage spraying system (1) for pre-desulfurization and deacidification, the filtering wind speed is less than or equal to 0.7 m/min, and the reaction process is as follows:
Ca(OH) 2 + SO 2 + 1/2O 2 → CaSO 4 + H 2 O；
Ca(OH) 2 + 2HCl → CaCl 2 + 2H 2 O；
s2: the flue gas is filtered by a first-stage bag-type dust collector (2) and then enters a second-stage desulfurization and deacidification system, firstly enters a reaction tower (5), and sodium bicarbonate powder and activated carbon powder are respectively sprayed into a flue at the lower part of the reaction tower (5) through a sodium bicarbonate storage injection system (3) and an activated carbon storage injection system (4), and are fully mixed with the flue gas in the reaction tower (5);
s3: after passing through the reaction tower (5), sodium bicarbonate and active carbon enter a secondary bag-type dust collector (6), a filter cake layer on the surface of a filter bag of the secondary bag-type dust collector (6) continuously reacts with acid gas, and the filtering wind speed is less than or equal to 0.7 m/min, so that long-time stay reaction is carried out;
s4: the flue gas after reaction purification is sent into a chimney through the action of an induced draft fan (9) to be discharged into the atmosphere, and desulfurization products are discharged to an ash conveying system (8) through an ash hopper at the bottom of a secondary bag-type dust remover (6) and are conveyed to a plant area fly ash curing system through the ash conveying system (8).
2. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas according to claim 1, which is characterized in that: the primary bag-type dust collector (2) is connected with a boiler tail gas conveying pipeline which is in butt joint with the jet orifice of the slaked lime storage jet system (1); the flue gas outlet of the primary bag-type dust collector (2) is connected with the reaction tower (5) through a pipeline, and the flue gas inlet at the bottom of the reaction tower (5) is respectively in butt joint with the injection ports of the baking soda storage injection system (3) and the active carbon storage injection system (4); the outlet end of the reaction tower (5) is connected with a secondary bag-type dust remover (6) through a pipeline, and a draught fan (9) is arranged at the smoke outlet of the secondary bag-type dust remover (6); the compressed air system (7) is respectively connected with the primary bag-type dust collector (2) and the secondary bag-type dust collector (6) in a control way through a pipe valve structure, and air bags with back blowing structures are arranged on filter bags of the primary bag-type dust collector (2) and the secondary bag-type dust collector (6); the ash hoppers at the bottoms of the primary bag-type dust collector (2) and the secondary bag-type dust collector (6) are connected with an ash conveying system (8) through pipelines.
3. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas according to claim 1, which is characterized in that: and S1, storing slaked lime powder in a slaked lime bin, spraying the slaked lime powder into a flue through a spraying system, enabling the slaked lime powder to enter a first-stage bag-type dust collector (2) and then attaching the slaked lime powder to a filter bag to form a filter cake layer, enabling the filter cake layer to be in long-time contact with flue gas, enabling a compressed air system (7) to blow back the filter bag through a bag differential pressure signal after the filter cake layer reaches a certain thickness, enabling a filter cake to fall into an ash hopper at the bottom of the first-stage bag-type dust collector (2), and sending the filter cake to an ash conveying system (8), and starting the next purification period.
4. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas according to claim 1, which is characterized in that: s3, sodium bicarbonate and residual SO in flue gas 2 Reacting with HCl acid gas, and adsorbing dioxin and heavy metal pollutants in the flue gas by using activated carbon; at the smoke temperature of 190-200 ℃ and NaHCO 3 With SO 2 There are two reaction pathways for HCl:
(1) the direct reaction:
2NaHCO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + 2CO 2 + H 2 O
NaHCO 3 + HCl → NaCl + CO 2 + H 2 O
② NaHCO 3 and (3) performing post-pyrolysis reaction:
2NaHCO 3 + (Heat) → Na 2 CO 3 + CO 2 + H 2 O
Na 2 CO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + CO 2
Na 2 CO 3 + 2HCl → 2NaCl + CO 2 + H 2 O。
5. the two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas is characterized in that the slaked lime storage injection system (1) and the primary bag-type dust remover (2) form a primary desulfurization deacidification system.
6. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas according to claim 1, wherein the baking soda storage injection system (3), the activated carbon storage injection system (4), the reaction tower (5) and the two-stage bag-type dust remover (6) form a two-stage desulfurization deacidification system.
7. The two-stage dry desulfurization deacidification dust removal process for the waste incineration flue gas according to claim 1 is characterized in that a plurality of groups of the primary bag-type dust remover (2), the reaction tower (5) and the secondary bag-type dust remover (6) are arranged in a matched mode, and single-channel operation or double-channel parallel operation can be realized according to the flue gas amount.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210234575.4A CN116262198A (en) | 2022-03-11 | 2022-03-11 | Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210234575.4A CN116262198A (en) | 2022-03-11 | 2022-03-11 | Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116262198A true CN116262198A (en) | 2023-06-16 |
Family
ID=86722794
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210234575.4A Pending CN116262198A (en) | 2022-03-11 | 2022-03-11 | Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116262198A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116651168A (en) * | 2023-07-13 | 2023-08-29 | 北京中科润宇环保科技股份有限公司 | Dry-method multi-pollutant flue gas purification device and method |
| CN117205735A (en) * | 2023-11-09 | 2023-12-12 | 北京中科润宇环保科技股份有限公司 | Deacidifying agent for purifying waste incineration flue gas |
-
2022
- 2022-03-11 CN CN202210234575.4A patent/CN116262198A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116651168A (en) * | 2023-07-13 | 2023-08-29 | 北京中科润宇环保科技股份有限公司 | Dry-method multi-pollutant flue gas purification device and method |
| CN116651168B (en) * | 2023-07-13 | 2024-01-30 | 北京中科润宇环保科技股份有限公司 | Dry-method multi-pollutant flue gas purification device and method |
| CN117205735A (en) * | 2023-11-09 | 2023-12-12 | 北京中科润宇环保科技股份有限公司 | Deacidifying agent for purifying waste incineration flue gas |
| CN117205735B (en) * | 2023-11-09 | 2024-03-05 | 北京中科润宇环保科技股份有限公司 | Deacidifying agent for purifying waste incineration flue gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN206652386U (en) | A kind of minimum discharge purifier of burning city domestic garbage flue gas | |
| CN108636098A (en) | A kind of the minimum discharge purifier and its method of burning city domestic garbage flue gas | |
| CN110917843A (en) | Waste incineration energy-saving flue gas ultralow purification system | |
| WO2021114084A1 (en) | Energy-saving ultralow flue gas purification system for waste incineration | |
| CN110548384A (en) | Ultra-clean emission system and method for hazardous waste incineration flue gas | |
| CN106215563A (en) | Garbage-incineration smoke purifying processing system | |
| CN101822942B (en) | Wet purification method for dioxin and heavy metals in solid waste incineration gas | |
| CN116262198A (en) | Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas | |
| CN112121614A (en) | Stable ultralow emission device and method for solid waste incineration flue gas | |
| CN204320062U (en) | A kind of high effective flue gas cleaning system | |
| CN105169943A (en) | Integrated system for coke oven flue gas desulfurization and denitrification and waste heat recovery | |
| CN205832964U (en) | A kind of semi-dry desulfurization and denitrification system based on biomass ash | |
| CN201899980U (en) | Complete device for treating sludge incineration tail gas in semidry method | |
| CN109140451A (en) | A kind of flue gas purifying technique and equipment of the processing of animal innoxious burning | |
| CN113144862A (en) | Biomass incineration power generation flue gas ultralow emission system and emission method thereof | |
| 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 | |
| CN217220890U (en) | Domestic waste burns flue gas denitration deacidification dust removal integration system of optimization | |
| CN211502852U (en) | Smoke tower integrated waste incineration smoke purification treatment device | |
| CN106076106A (en) | A kind of semi-dry desulfurization and denitrification system and method based on biomass ash | |
| CN106178877A (en) | A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique | |
| CN108499344A (en) | A kind of biomass flue gas dust-removal and desulfurizing denitrating system | |
| CN202823129U (en) | Flue gas cleaning device of spray drying method combined with hydrated lime powder spraying | |
| CN110548387A (en) | integrated treatment device and process for ion denitration, desulfurization and dust removal by semidry method | |
| CN213853843U (en) | Thermal power tail gas treatment equipment |
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 |