CN112797429A - Double-dry deacidification method and system for hazardous waste incineration flue gas - Google Patents
Double-dry deacidification method and system for hazardous waste incineration flue gas Download PDFInfo
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- CN112797429A CN112797429A CN202110010245.2A CN202110010245A CN112797429A CN 112797429 A CN112797429 A CN 112797429A CN 202110010245 A CN202110010245 A CN 202110010245A CN 112797429 A CN112797429 A CN 112797429A
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- 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
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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
- 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
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- 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
- B01D53/38—Removing components of undefined structure
- B01D53/40—Acidic components
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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Abstract
A double dry deacidification method and a system for hazardous waste incineration flue gas; the method comprises the steps of quenching and cooling, primary deacidification, primary dedusting, secondary deacidification, secondary dedusting and the like of smoke in sequence; the system comprises a quenching deacidification tower, a primary dry deacidification tower, a primary cloth bag dust remover, a secondary dry deacidification tower and a secondary cloth bag dust remover which are sequentially connected through pipelines, wherein the secondary cloth bag dust remover is connected with an induced draft fan through a pipeline, a primary flue gas online monitoring system and a flue gas electric heater are arranged on a connecting pipeline between the primary cloth bag dust remover and the secondary dry deacidification tower, and a secondary flue gas online monitoring system is arranged on a connecting pipeline between the secondary cloth bag dust remover and the induced draft fan. The method not only can dynamically adjust the adding speed of the deacidification agent and ensure the standard emission of the flue gas, but also avoids the reduction of the temperature of the flue gas to the maximum extent in the whole process, has no deacidification wastewater in the whole process, and greatly reduces the investment and the production running cost of the flue gas purification.
Description
Technical Field
The invention relates to a method and a system for treating flue gas generated in a hazardous waste incineration process, in particular to flue gas treatment based on a double-dry-method deacidification device in a hazardous waste incineration disposal process, and belongs to the technical field of flue gas deacidification treatment.
Background
Hazardous waste generally refers to solid waste that is corrosive, reactive, toxic, flammable, or infectious. Acid gases such as a large amount of hydrogen chloride, sulfur dioxide, hydrogen fluoride and the like can be generated in the incineration disposal process of a traditional hazardous waste rotary kiln, a technical route of 'semi-dry method + wet method' and 'dry method + wet method' is adopted in a flue gas deacidification system, high deacidification efficiency based on wet method deacidification makes the flue gas deacidification system popular in the market, dry method deacidification is generally used for supplement and emergency measures of a wet method deacidification process, quicklime or slaked lime is used as a deacidification agent, and secondary treatment cost of additional water treatment and salt evaporation is increased due to the large amount of discharged deacidification waste water. With the stricter emission limit values of hydrogen chloride, sulfur dioxide and hydrogen fluoride, the stable standard emission of the incineration flue gas is ensured for a long period, and higher requirements are put on the operation management level of hazardous waste operating units and the flue gas purification system.
The dry deacidification device for treating incineration flue gas by using baking soda is proposed in Chinese patent documents CN111359422A, CN109126404A, CN108392976A, CN 3, a dry deacidification system adopting sodium bicarbonate as a reactant and CN108392976A, but the design of the deacidification system is not systematically elucidated, and particularly when acid components in furnace compatible materials are high, the deacidification efficiency of acid gas in flue gas cannot meet the increasingly strict flue gas emission standard, the deacidification efficiency cannot be used as a main deacidification mode for a hazardous waste incineration flue gas purification system, and the environmental protection risk is high.
Therefore, the research on a set of energy-saving and efficient flue gas purification system based on baking soda dry deacidification, which meets the emission standard, and the guarantee of environment-friendly, safe, stable and long-acting operation of a hazardous waste incineration system is a problem to be solved urgently.
Disclosure of Invention
The invention provides a double-dry deacidification method which can dynamically adjust the addition rate of a deacidification agent, ensure that the smoke reaches the standard and is discharged, and no dangerous waste incineration smoke generated by waste water exists in the whole process, and provides a system for realizing the method.
The invention relates to a double-dry deacidification method for hazardous waste incineration flue gas, which is to carry out rapid cooling, primary deacidification, primary dedusting, secondary deacidification and secondary dedusting on the flue gas in sequence, and specifically comprises the following steps:
(1) quenching and cooling: cooling the incineration flue gas of the hazardous waste to below 200 ℃ by quenching, and maintaining the temperature at 180-200 ℃;
(2) primary deacidification: spraying a deacidification agent into the flue gas subjected to the quenching and cooling treatment to perform primary deacidification treatment;
(3) primary dust removal: performing dust removal treatment on the flue gas subjected to the primary deacidification treatment; the dust removal mode is cloth bag dust removal;
(4) secondary deacidification: making the temperature of the flue gas after primary dedusting not lower than 160 ℃, spraying deacidification agent and activated carbon powder into the flue gas, and performing secondary deacidification treatment;
(5) secondary dust removal: performing dust removal treatment on the flue gas subjected to the secondary deacidification treatment; the dust removal mode is cloth bag dust removal.
And (2) in the step (1), the flow velocity of the gas flow is maintained at 10-20m/s in the operation process of quenching and cooling, primary deacidification, primary dedusting, secondary deacidification and secondary dedusting.
The step (1) of quenching and cooling refers to that the temperature of the flue gas is reduced from 500-550 ℃ to 180-200 ℃ within 1 second.
The quenching liquid (clear water or alkaline substance solution) is sprayed into the flue gas, and the alkaline substance solution with the mass concentration not higher than 10% is preferred.
The injection rate of the deacidification agent in the step (2) and the step (4) in the smoke is not higher than 15 kg/min. The deacidification agent is alkaline material powder, wherein the volume of particles with the particle size of less than 20um is not less than 90%.
The contact time of the deacidification agent in the step (2) and the deacidification agent in the step (4) with the smoke is not less than 1.5 seconds.
The adding amount of the activated carbon in the step (3) is controlled to be 0.5-1kg per ton of dangerous waste feeding amount.
And (3) and (5) removing dust under the pressure difference of not less than 1000Pa so as to ensure that a sufficient amount of deacidification agent is attached to the surface of the dust removing cloth bag.
And (4) controlling the injection rate of the deacidification agent in the step (4) by monitoring the data of the flue gas after primary dedusting, wherein the monitoring indexes at least comprise the concentrations of hydrogen chloride, hydrogen fluoride and sulfur dioxide in the flue gas, and when the indexes of the flue gas after primary dedusting reach the standard, suspending the injection of the deacidification agent in secondary deacidification, otherwise increasing the injection amount.
The double-dry deacidification system for the hazardous waste incineration flue gas for realizing the method adopts the following technical scheme:
the system comprises a quenching deacidification tower, a first-stage dry deacidification tower, a first-stage bag-type dust remover, a second-stage dry deacidification tower and a second-stage bag-type dust remover, wherein the quenching deacidification tower is sequentially connected through a pipeline, the first-stage dry deacidification tower is connected with a draught fan through a pipeline, a first-stage flue gas online monitoring system and a flue gas electric heater are arranged on a connecting pipeline between the first-stage bag-type dust remover and the second-stage dry deacidification tower, a second-stage flue gas online monitoring system is arranged on a connecting pipeline between the second-stage bag-type dust remover and the draught fan, a quenching liquid spray gun is arranged at the top of the quenching deacidification tower, a first-stage deacidification agent spray.
The feed inlets of the first-stage dry acid removal tower and the second-stage dry acid removal tower are connected with a pneumatic conveying device, the pneumatic conveying device is connected with a deacidification agent storage tank, and a metering weighing feeder is arranged on the connecting pipeline.
The bag-type dust collector at least comprises 4 independent chambers, the upper box body is provided with steam heat tracing, and each chamber is provided with an independent pulse back-blowing pipeline.
The flue gas after heat exchange of the waste heat boiler is cooled and then is in contact reaction with the dilute alkali liquor sprayed by the quenching liquid spray gun in the quenching deacidification tower, and the temperature of the flue gas is reduced to 180-200 ℃. The deacidification agent (alkaline material) sprayed in the first-stage dry-method deacidification tower neutralizes and reacts the acid gas in the flue gas, and the unreacted deacidification agent is attached to the surface of the bag-type dust collector along with the flue gas and further contacts and reacts with the acid gas. The real-time data of the flue gas monitored by the primary flue gas on-line monitoring system controls the injection rate of the deacidification agent in the secondary dry-method deacidification tower and adjusts the feeding amount of compatible hazardous waste materials, and the flue gas temperature is not lower than 160 ℃ through a flue gas electric heater. Activated carbon powder is sprayed into the secondary dry deacidification tower to adsorb heavy metals and dioxin in the flue gas, and the flue gas is dedusted and deacidified by a secondary bag-type dust remover and then discharged by a draught fan.
The invention has simple structure, simple and convenient operation, economy, high efficiency, energy conservation and environmental protection, can dynamically adjust the addition rate of the deacidification agent, ensures the deacidification efficiency of the hydrogen chloride, the sulfur dioxide and the hydrogen fluoride to be more than 90 percent, and ensures the standard emission of the flue gas. The method is different from wet deacidification, no deacidification wastewater is generated in the whole process, the reduction of the flue gas temperature is avoided to the maximum extent in the whole process, and the secondary treatment cost of the wastewater and the flue gas heating cost of a wet deacidification tower are greatly saved. By designing the primary CEMS on-line monitoring system, the parameter adjustment of the secondary dry deacidification agent injection can be optimized, the deacidification performance is fully exerted, the deacidification efficiency of the acid gas and the use rate of the deacidification agent are improved, the standard emission of the flue gas is ensured, and the use amount of the deacidification agent is reduced. The whole system is designed with the concept of energy conservation and environmental protection fully considered, and the investment and production running cost of the flue gas purification system are greatly reduced.
Drawings
FIG. 1 is a schematic flow diagram of a double dry deacidification method for hazardous waste incineration flue gas in the invention.
FIG. 2 is a schematic diagram of the structural principle of the double dry deacidification system for hazardous waste incineration flue gas in the invention.
In the figure: 1. the system comprises a quenching deacidification tower, 2a primary dry deacidification tower, 3 a primary bag-type dust remover, 4a primary flue gas online monitoring system (primary CEMS), 5 a flue gas electric heater, 6a secondary dry deacidification tower, 7 a secondary bag-type dust remover, 8 a draught fan, 9 a secondary flue gas online monitoring system (secondary CEMS), 10 a chimney, 11 a quenching liquid spray gun, 12 a primary deacidification agent spray pipe, 13 a secondary deacidification agent and an activated carbon spray pipe.
Detailed Description
The double-dry deacidification method for hazardous waste incineration flue gas disclosed by the invention has the process flow as shown in figure 1, and adopts a process route of 'quenching and cooling, primary deacidification, primary bag-type dust removal, secondary deacidification tower and secondary bag-type dust remover'. The flue gas runs in turn at each stage at a flow rate of 10-20m/s, and the specific process is as follows:
(1) the temperature of the flue gas generated by burning the hazardous waste is rapidly cooled to below 200 ℃, and can be reduced from 500-550 ℃ to 180-200 ℃ within 1 second, and maintained at 180-200 ℃, and the rapid cooling liquid is injected into the flue gas. The quenching liquid can be clear water or an alkaline material solution, the alkaline material solution can simultaneously have the dual functions of quenching and cooling the flue gas and deacidifying, and the concentration of the alkaline material solution is adjusted between 0 percent and 10 percent according to the operating condition.
(2) Spraying alkaline material powder (such as one or more of sodium hydroxide, sodium carbonate, sodium bicarbonate and calcium hydroxide) into the desulfurized flue gas to perform primary deacidification treatment. The volume of the particles with the particle size smaller than 20um in the alkaline material powder is not less than 90%, and the injection rate of the alkaline material powder is 0-15 kg/min.
(3) And performing cloth bag dust removal on the flue gas subjected to the primary deacidification treatment.
(4) Heating the pipeline to make the temperature of the flue gas after primary dedusting not lower than 160 ℃, spraying alkaline material powder and activated carbon powder into the flue gas, and performing secondary deacidification treatment. The injection rate of the alkaline material powder and the activated carbon powder in the flue gas is 0-15 kg/min.
(5) And performing cloth bag dust removal treatment on the flue gas subjected to the secondary deacidification treatment.
The double-dry deacidification system for hazardous waste incineration flue gas for realizing the method is shown in fig. 2 and comprises a quenching deacidification tower 1, a primary dry deacidification tower 2, a primary cloth bag dust remover 3, a secondary dry deacidification tower 6 and a secondary cloth bag dust remover 7 which are sequentially connected through pipelines. The secondary bag-type dust collector 6 is connected with an induced draft fan 8 through a pipeline, and the working condition full pressure of the induced draft fan 8 preferably meets at least 5000Pa so as to maintain the flow velocity of the flue gas between the devices at 10-20 m/s. The air outlet of the induced draft fan 8 is connected with a chimney 10. A primary flue gas online monitoring system 4 and a flue gas electric heater 5 are arranged on a connecting pipeline between the primary bag-type dust collector 3 and the secondary dry-method deacidification tower 6, and a secondary flue gas online monitoring system 9 is arranged on a connecting pipeline between the secondary bag-type dust collector 7 and an induced draft fan 8 or in a chimney 10.
The top of the rapid cooling deacidification tower 1 is provided with a flue gas inlet and a rapid cooling liquid spray gun 11, the rapid cooling liquid spray gun 11 is connected with a rapid cooling pump station (prior art), the rapid cooling pump station is connected with a rapid cooling liquid tank, rapid cooling liquid such as clear water or alkaline material solution (such as NaOH dilute solution) is stored in the rapid cooling liquid tank, and the rapid cooling liquid tank is connected with the rapid cooling pump station. The alkaline material solution can simultaneously have the dual functions of flue gas quenching and cooling and deacidification, the concentration of the alkaline material solution is adjusted according to the monitoring value of an online concentration meter arranged between a quenching liquid tank and a quenching pump station, and the concentration of the alkaline material solution is adjusted between 0 percent and 10 percent according to the operating condition. The flue gas after heat exchange of the waste heat boiler enters the rapid cooling deacidification tower 1 from a flue gas inlet, and the rapid cooling liquid is sprayed into the flue gas in the rapid cooling deacidification tower 1 through a rapid cooling liquid spray gun 11. The lower smoke outlet of the quenching deacidification tower 1 is connected with the smoke inlet of the first-stage dry deacidification tower 2. The quench deacidification tower 1 is used for supplementing a dry deacidification system. The quenching pump station cools the flue gas by conveying quenching liquid, automatically controls the flow of dilute alkali liquid sprayed by the quenching liquid spray gun 11 according to the temperature monitored by a temperature sensor arranged in the quenching deacidification tower 1, and maintains the temperature of the cooled flue gas at 180-200 ℃. The quenching deacidification tower 1 and the first-stage dry deacidification tower 2 share an ash outlet bin.
A primary deacidification agent spray pipe 12 is arranged above the smoke inlet on the primary deacidification tower 2, and a secondary deacidification agent and activated carbon spray pipe 13 is arranged above the smoke inlet on the secondary deacidification tower 6. The deacidification agent used in the first-stage dry-method deacidification tower 2 and the second-stage dry-method deacidification tower 6 adopts alkaline material (such as one or more of sodium hydroxide, sodium carbonate, sodium bicarbonate and calcium hydroxide) powder, the alkaline material powder is prepared by a grinding machine, the requirement that the particle size of 90% volume in the powder is less than 20 mu m is met, and the ground alkaline material powder is sprayed into the first-stage dry-method deacidification tower 2 and the second-stage dry-method deacidification tower 6 from two independent pipelines through positive pressure pneumatic conveying equipment. A metering weighing feeder is arranged between the grinder and the pneumatic conveying equipment, and can accurately meter and feed alkaline material powder. As the alkaline material powder is easy to absorb moisture and agglomerate, the discharge force of the grinding machine is dynamically adjusted in real time according to the injection amount, the alkaline material powder is ensured to be timely injected into a flue after being ground and is not stored for a long time, and the injection rate of the alkaline material powder can be adjusted between 0 and 15 kg/min. The activated carbon powder can be sprayed into the secondary dry deacidification tower 6 through the secondary deacidification agent and the activated carbon spray pipe 13. The activated carbon powder is sprayed to remove heavy metals and dioxin in the flue gas.
The primary flue gas online monitoring system 4 and the secondary flue gas online monitoring system 9 are in the prior art, the monitoring indexes at least comprise the concentrations of hydrogen chloride, hydrogen fluoride and sulfur dioxide in flue gas, and monitoring data can be transmitted with the control system in real time. The monitoring data of the primary flue gas on-line monitoring system 4 is used for guiding and adjusting the operation parameters of alkaline material powder injection in the secondary dry-method deacidification tower 6, and the flue gas data monitored by the follow-up secondary flue gas on-line monitoring system 9 is guaranteed to reach the standard.
The flue gas electric heater 4 is arranged on a pipeline between the primary flue gas on-line monitoring system 4 and the secondary deacidification tower 6, and can be automatically controlled through a temperature sensor to ensure that the temperature of flue gas flowing through is above 160 ℃, so that alkaline material powder in the secondary dry deacidification tower 6 can efficiently react with acid gas in the optimal temperature range after being sprayed in, and the utilization rate and the deacidification efficiency are improved.
Dispose steam heat tracing in the last box of one-level sack cleaner 3 and second grade sack cleaner 7, can be through regularly or regularly hinder the automatic pulse blowback deashing of two kinds of modes, every sack cleaner should include 4 independent bins at least, and every bin is provided with solitary pulse blowback pipeline, and the sack cleaner should be able to bear 1500 Pa's pressure drag at least.
The operation of the above system is as follows.
The temperature of the flue gas after heat exchange of the waste heat boiler is reduced from 1100 ℃ to 500-550 ℃, then the flue gas is in full contact with and fast reacts with the dilute alkali solution fog drops (the particle size is less than 20 mu m) sprayed by the quenching liquid spray gun 11 in the quenching deacidification tower 1, and the temperature of the flue gas is reduced to 180-200 ℃. The alkaline material powder sprayed into the primary dry deacidification tower 2 is decomposed, a large number of microporous structures similar to activated carbon are formed in the newly generated substances, the specific surface area is obviously improved, the reaction activity is extremely strong, the acidic gas in the flue gas can be neutralized and reacted quickly and efficiently, and the unreacted alkaline material powder is attached to the surface of the bag-type dust collector along with the flue gas and further contacts and reacts with the acidic gas. In order to prolong the reaction time and increase the turbulence of the flue gas, the flue of the primary dry deacidification tower 2 adopts a sleeve type structure design, so that the contact time of alkaline material powder and the flue gas is ensured to be more than 1.5 s.
Controlling the injection rate of alkaline material powder in the secondary dry-method deacidification tower 6 and adjusting the feeding amount of compatible hazardous waste materials through real-time data of the smoke components monitored by the primary smoke online monitoring system 4; when the monitoring index of the primary flue gas online monitoring system 4 reaches the standard, the injection of alkaline material powder in the secondary dry-method deacidification tower 6 is suspended; otherwise, the injection amount of the alkaline material powder in the secondary dry deacidification tower 6 is increased. When the temperature of the flue gas at the outlet of the primary flue gas online monitoring system 4 is lower than 160 ℃, the flue gas electric heater 5 is started to heat the flue, so that the temperature of the flue gas is higher than 160 ℃. Besides alkaline material powder, active carbon powder is sprayed in the secondary dry-method deacidification tower 6 at the same time for adsorbing heavy metal and dioxin in flue gas. In order to prolong the contact time of the deacidification agent and the high-temperature flue gas, the flue of the secondary dry-method deacidification tower 6 is provided with an expansion section and the length of the flue is increased, the adding amount of the activated carbon is controlled to be 0.5-1kg per ton of hazardous waste feeding amount entering a kiln, the injection rate of the alkaline material powder is adjusted within the range of 0-15kg/min, and the pressure difference of a bag-type dust remover is maintained to be more than 1000Pa so as to ensure that the sufficient amount of the alkaline material powder is attached to the surface of a bag.
After the flue gas is dedusted and deacidified by the secondary bag-type dust collector 7, the temperature is still kept above 150 ℃, the flue gas is directly discharged through the draught fan 8 without being heated, and the removal efficiency of hydrogen chloride, sulfur dioxide and hydrogen fluoride reaches above 90%.
The invention can treat low chlorine, low sulfur and low fluorine; the hazardous waste with high chlorine, high sulfur and high fluorine ensures the long-term stable standard emission of the flue gas, improves the use efficiency of the deacidification agent to the maximum extent, does not generate waste water in the whole process, and reduces the investment and the operation cost.
Claims (10)
1. A double-dry deacidification method for hazardous waste incineration flue gas is characterized in that the flue gas is subjected to rapid cooling, primary deacidification, primary dedusting, secondary deacidification and secondary dedusting in sequence, and the method specifically comprises the following steps:
(1) quenching and cooling: cooling the incineration flue gas of the hazardous waste to below 200 ℃ by quenching, and maintaining the temperature at 180-200 ℃;
(2) primary deacidification: spraying a deacidification agent into the flue gas subjected to the quenching and cooling treatment to perform primary deacidification treatment;
(3) primary dust removal: performing dust removal treatment on the flue gas subjected to the primary deacidification treatment;
(4) secondary deacidification: making the temperature of the flue gas after primary dedusting not lower than 160 ℃, spraying deacidification agent and activated carbon powder into the flue gas, and performing secondary deacidification treatment;
(5) secondary dust removal: and (4) performing dust removal treatment on the flue gas subjected to the secondary deacidification treatment.
2. The dual dry deacidification method for hazardous waste incineration flue gas as claimed in claim 1, wherein the flow velocity of the flue gas is maintained at 10-20m/s during the operation processes of quenching temperature reduction, primary deacidification, primary dedusting, secondary deacidification and secondary dedusting in sequence.
3. The dual dry deacidification method for hazardous waste incineration flue gas as claimed in claim 1, wherein the step (1) of quenching and temperature reduction means that the temperature of the flue gas is reduced from 500-550 ℃ to 180-200 ℃ within 1 second.
4. The dual dry deacidification method for hazardous waste incineration flue gas as claimed in claim 1, wherein said quenching cooling is performed by injecting a quenching liquid into the flue gas, wherein said quenching liquid is clear water or alkaline solution with mass concentration not higher than 10%.
5. The dual dry deacidification method for hazardous waste incineration flue gas according to claim 1, wherein the deacidification agent in step (2) and step (4) is alkaline material powder, wherein the volume of the particles with the particle size of less than 20um is not less than 90%, and the spraying rate of the deacidification agent in the flue gas is not more than 15 kg/min.
6. The dual dry deacidification method for hazardous waste incineration flue gas according to claim 1, wherein the contact time of the deacidification agent in the step (2) and the step (4) with the flue gas is not less than 1.5 seconds.
7. The dual dry deacidification method for hazardous waste incineration flue gas according to claim 1, wherein the adding amount of the activated carbon in the step (3) is controlled to be 0.5-1kg per ton of hazardous waste feeding amount.
8. The dual dry deacidification method for hazardous waste incineration flue gas as claimed in claim 1, wherein the injection rate of the deacidification agent in step (4) is controlled by monitoring the flue gas data after primary dedusting, the monitoring indexes at least comprise the concentrations of hydrogen chloride, hydrogen fluoride and sulfur dioxide in the flue gas, when the flue gas indexes after primary dedusting reach the standard, the injection of the deacidification agent in secondary deacidification is suspended, otherwise, the injection amount is increased.
9. The utility model provides a two dry process deacidification systems of hazardous waste incineration flue gas, which is characterized in that, include the rapid cooling deacidification tower that connects gradually through the pipeline, one-level dry process deacidification tower, one-level sack cleaner, second grade dry process deacidification tower and second grade sack cleaner, the second grade sack cleaner passes through the tube coupling draught fan, be provided with one-level flue gas on-line monitoring system and flue gas electric heater on the connecting tube between one-level sack cleaner and the second grade dry process deacidification tower, be provided with second grade flue gas on-line monitoring system on the connecting tube of second grade sack cleaner and draught fan, the top of rapid cooling deacidification tower is provided with the quench liquid spray gun, be provided with one-level deacidification agent spray tube on the one-level dry process deacidification tower, be provided with second.
10. The dual dry deacidification system for hazardous waste incineration flue gas as claimed in claim 1, wherein the feed inlets of the primary dry deacidification tower and the secondary dry deacidification tower are both connected with a pneumatic conveying device, the pneumatic conveying device is connected with a deacidification agent storage tank, and a metering weighing feeder is arranged on the connecting pipeline.
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