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 PDF

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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
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flue gas
deacidification
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bag filter
desulfurization
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陈明华
余维豪
秦艳梅
王爱武
傅嘉宾
喻宏伟
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Ningbo Yibu Technology Co ltd
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    • 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
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    • 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
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • 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
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
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    • B01D2251/30—Alkali metal compounds
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D—SEPARATION
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    • B01D2251/606—Carbonates
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    • 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
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Abstract

本发明公开了一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，包括消石灰储存喷射系统、一级布袋除尘器、小苏打储存喷射系统、活性炭储存喷射系统、反应塔、二级布袋除尘器、压缩空气系统和输灰系统；本发明采用两级干法脱硫脱酸除尘技术，一级为消石灰脱硫脱酸除尘系统，在一级布袋除尘器入口喷入消石灰粉；二级为小苏打脱硫脱酸除尘系统，在反应塔前喷入小苏打粉（NaHCO3），整个工艺脱硫脱酸除尘效率高，排放浓度低，能够克服传统干法脱硫脱酸效率低的问题，可实现SO2、HCl、粉尘超低排放，且对烟气的热量损耗低，能够降低后续低温SCR脱硝系统烟气加热成本，且干法脱硫水分含量低，有利于烟气排放后消散，无白烟产生。

Figure 202210234575

The invention discloses a two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas. device, compressed air system and ash conveying system; the present invention adopts two-stage dry desulfurization, deacidification and dust removal technology, the first stage is slaked lime desulfurization, deacidification and dust removal system, and slaked lime powder is sprayed into the inlet of the bag filter; the second stage is baking soda The desulfurization, deacidification and dust removal system sprays baking soda powder (NaHCO 3 ) in front of the reaction tower. The whole process has high desulfurization, deacidification and dust removal efficiency and low emission concentration, which can overcome the problem of low efficiency of traditional dry desulfurization and deacidification, and can realize SO 2 , HCl, and dust are ultra-low emissions, and the heat loss to the flue gas is low, which can reduce the flue gas heating cost of the subsequent low-temperature SCR denitrification system, and the dry desulfurization has a low moisture content, which is conducive to the dissipation of the flue gas after emission, and no white smoke is produced.

Figure 202210234575

Description

Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas
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)

1.一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于，包括消石灰储存喷射系统（1）、一级布袋除尘器（2）、小苏打储存喷射系统（3）、活性炭储存喷射系统（4）、反应塔（5）、二级布袋除尘器（6）、压缩空气系统（7）和输灰系统（8）；具体工艺步骤如下：1. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas, characterized in that it includes a slaked lime storage injection system (1), a first-stage bag filter (2), a baking soda storage injection system (3), activated carbon Storage injection system (4), reaction tower (5), secondary bag filter (6), compressed air system (7) and ash conveying system (8); the specific process steps are as follows: S1：锅炉尾气进入一级脱硫脱酸系统：一级布袋除尘器（2）上设有入口烟道（10），在一级布袋除尘器（2）的入口烟道（10）通过消石灰储存喷射系统（1）喷入消石灰粉进行预脱硫脱酸，过滤风速≤0.7 m/min，反应过程如下：S1: Boiler tail gas enters the first-stage desulfurization and deacidification system: the first-stage bag filter (2) is provided with an inlet flue (10), and the inlet flue (10) of the first-stage bag filter (2) is sprayed through slaked lime storage System (1) is sprayed with slaked lime powder for pre-desulfurization and deacidification, and the filtration wind speed is ≤0.7 m/min. The reaction process is as follows: Ca(OH)2 + SO2 + 1/2O2 → CaSO4 + H2O；Ca(OH) 2 + SO 2 + 1/2O 2 → CaSO 4 + H 2 O; Ca(OH)2 + 2HCl → CaCl2 + 2H2O；Ca(OH) 2 + 2HCl → CaCl 2 + 2H 2 O; S2：烟气经一级布袋除尘器（2）过滤后进入二级脱硫脱酸系统，首先进入反应塔（5），在反应塔（5）下部烟道内通过小苏打储存喷射系统（3）和活性炭储存喷射系统（4）分别喷入小苏打粉和活性炭粉，小苏打粉和活性炭粉在反应塔（5）内与烟气充分混合；S2: The flue gas is filtered by the first-stage bag filter (2) and enters the second-stage desulfurization and deacidification system. It first enters the reaction tower (5), and passes through the baking soda storage injection system (3) and the lower flue of the reaction tower (5). The activated carbon storage injection system (4) sprays baking soda powder and activated carbon powder respectively, and the baking soda powder and activated carbon powder are fully mixed with the flue gas in the reaction tower (5); S3：经过反应塔（5）后，小苏打和活性炭进入二级布袋除尘器（6），在二级布袋除尘器（6）的滤袋表面滤饼层继续与酸性气体反应，过滤风速≤0.7 m/min，进行长时间停留反应；S3: After passing through the reaction tower (5), baking soda and activated carbon enter the secondary bag filter (6), and the filter cake layer on the surface of the filter bag of the secondary bag filter (6) continues to react with acid gas, and the filtering wind speed is ≤0.7 m/min, for long-term residence reaction; S4：经反应净化后的烟气通过引风机（9）的作用送入烟囱排入大气中，脱硫产物由二级布袋除尘器（6）底部的灰斗排至输灰系统（8），由输灰系统（8）输送至厂区飞灰固化系统。S4: The flue gas after reaction and purification is sent into the chimney and discharged into the atmosphere through the action of the induced draft fan (9), and the desulfurization product is discharged from the ash hopper at the bottom of the secondary bag filter (6) to the ash conveying system (8), and then The ash conveying system (8) conveys to the fly ash solidification system in the factory area. 2.如权利要求1所述的一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于：所述一级布袋除尘器（2）上连接锅炉尾气输送管道，锅炉尾气输送管道上与消石灰储存喷射系统（1）的喷射口对接；所述一级布袋除尘器（2）的烟气出口通过管道与反应塔（5）连接，反应塔（5）底部的烟气入口处分别与小苏打储存喷射系统（3）、活性炭储存喷射系统（4）的喷射口对接；所述反应塔（5）的出口端通过管道与二级布袋除尘器（6）连接，二级布袋除尘器（6）的烟气出口处安装引风机（9）；所述压缩空气系统（7）通过管阀结构分别与一级布袋除尘器（2）、二级布袋除尘器（6）控制连接，在一级布袋除尘器（2）和二级布袋除尘器（6）的滤袋上设有反吹结构的气包；所述一级布袋除尘器（2）和二级布袋除尘器（6）底部的灰斗通过管道与输灰系统（8）连接。2. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas as claimed in claim 1, characterized in that: the first-stage bag filter (2) is connected to the boiler tail gas transmission pipeline, and the boiler tail gas transmission pipeline The upper part is docked with the injection port of the slaked lime storage injection system (1); the flue gas outlet of the first-stage bag filter (2) is connected to the reaction tower (5) through a pipe, and the flue gas inlet at the bottom of the reaction tower (5) is respectively It is docked with the injection port of the baking soda storage injection system (3) and the activated carbon storage injection system (4); the outlet end of the reaction tower (5) is connected to the secondary bag filter (6) through a pipeline, and the secondary bag filter (6) An induced draft fan (9) is installed at the flue gas outlet of The filter bags of the first-level bag filter (2) and the second-level bag filter (6) are equipped with air bags with a back-blowing structure; the bottom of the first-level bag filter (2) and the second-level bag filter (6) The ash hopper is connected to the ash conveying system (8) through pipelines. 3.如权利要求1所述的一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于：S1中消石灰粉储存于消石灰料仓中，经喷射系统喷入烟道后进入一级布袋除尘器（2）附着在滤袋上，形成滤饼层，与烟气长时间接触，滤饼层到达一定厚度后，由布袋差压信号启动压缩空气系统（7）对滤袋反吹，滤饼掉落至一级布袋除尘器（2）底部的灰斗送入输灰系统（8），开始下一个净化周期。3. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas as claimed in claim 1, characterized in that: the slaked lime powder in S1 is stored in the slaked lime silo, sprayed into the flue by the injection system and then enters a The first-stage bag filter (2) is attached to the filter bag to form a filter cake layer, which is in contact with the flue gas for a long time. After the filter cake layer reaches a certain thickness, the compressed air system (7) is activated by the bag differential pressure signal to blow back the filter bag , the filter cake falls to the ash hopper at the bottom of the first-stage bag filter (2) and is sent to the ash conveying system (8) to start the next purification cycle. 4.如权利要求1所述的一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于：S3中小苏打与烟气中剩余SO2、HCl酸性气体反应，活性炭吸附烟气中的二噁英和重金属污染物；在烟温190-200℃下，NaHCO3与SO2、HCl存在两种反应途径：4. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas as claimed in claim 1, characterized in that: S3 sodium bicarbonate reacts with residual SO 2 and HCl acid gas in the flue gas, and activated carbon absorbs in the flue gas Dioxin and heavy metal pollutants; at a smoke temperature of 190-200°C, there are two reaction pathways between NaHCO 3 and SO 2 , HCl: ① 直接反应：① Direct response: 2NaHCO3 + SO2 + 1/2O2 → Na2SO4 + 2CO2 + H2O2NaHCO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + 2CO 2 + H 2 O NaHCO3 + HCl → NaCl + CO2 + H2ONaHCO 3 + HCl → NaCl + CO 2 + H 2 O ② NaHCO3热解后反应：② Reaction after pyrolysis of NaHCO 3 : 2NaHCO3 + (Heat) → Na2CO3 + CO2 + H2O2NaHCO 3 + (Heat) → Na 2 CO 3 + CO 2 + H 2 O Na2CO3 + SO2+ 1/2O2 → Na2SO4 + CO2 Na 2 CO 3 + SO 2 + 1/2O 2 → Na 2 SO 4 + CO 2 Na2CO3 + 2HCl → 2NaCl + CO2 + H2O。Na 2 CO 3 + 2HCl → 2NaCl + CO 2 + H 2 O. 5.如权利要求1所述的一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于，所述消石灰储存喷射系统（1）和一级布袋除尘器（2）组成一级脱硫脱酸系统。5. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas as claimed in claim 1, characterized in that the slaked lime storage injection system (1) and the first-stage bag filter (2) form a first-stage Desulfurization and deacidification system. 6.如权利要求1所述的一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于，所述小苏打储存喷射系统（3）、活性炭储存喷射系统（4）、反应塔（5）和二级布袋除尘器（6）组成二级脱硫脱酸系统。6. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas according to claim 1, characterized in that the baking soda storage injection system (3), activated carbon storage injection system (4), reaction tower (5) and the secondary bag filter (6) form the secondary desulfurization and deacidification system. 7.如权利要求1所述的一种垃圾焚烧烟气两级干法脱硫脱酸除尘工艺，其特征在于，所述一级布袋除尘器（2）、反应塔（5）以及二级布袋除尘器（6）配套设置有多组，可根据烟气量大小实现单通道运行或双通道并联运行。7. A two-stage dry desulfurization, deacidification and dust removal process for waste incineration flue gas as claimed in claim 1, characterized in that the first-stage bag filter (2), the reaction tower (5) and the second-stage bag filter The device (6) is equipped with multiple sets, which can realize single-channel operation or double-channel parallel operation according to the amount of flue gas.
CN202210234575.4A 2022-03-11 2022-03-11 Two-stage dry desulfurization deacidification dust removal process for waste incineration flue gas Pending CN116262198A (en)

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