CN218846146U - Hazardous waste incineration disposal system - Google Patents
Hazardous waste incineration disposal system Download PDFInfo
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- CN218846146U CN218846146U CN202222671581.4U CN202222671581U CN218846146U CN 218846146 U CN218846146 U CN 218846146U CN 202222671581 U CN202222671581 U CN 202222671581U CN 218846146 U CN218846146 U CN 218846146U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
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Abstract
The application relates to a hazardous waste incineration treatment system, which comprises an incineration system and a flue gas treatment system; the burning system is formed by sequentially connecting a rotary kiln and a secondary combustion chamber, namely a smoke outlet of the rotary kiln is connected with a feed inlet of the secondary combustion chamber; flue gas processing system exhaust-heat boiler, quench tower, circulating fluidized bed, sack cleaner and caustic wash tower, exhaust-heat boiler air inlet pass through the pipeline and are connected with second combustion chamber exhanst gas outlet, and exhaust-heat boiler exhanst gas outlet is connected the air inlet with the quench tower and is connected, and the quench tower discharge gate is connected with the circulating fluidized bed feed inlet, and the circulating fluidized bed discharge gate is connected with the caustic wash tower through sack cleaner, draught fan, and the caustic wash tower tail gas passes through the chimney evacuation. The application realizes the good incineration of the hazardous waste incineration, has low operation cost, and the reaction product is non-toxic and pollution-free and has no byproduct emission.
Description
Technical Field
The application relates to hazardous waste innocent treatment technical field especially relates to a hazardous waste incineration disposal system.
Background
The global warming, ozone layer destruction and acid rain are three environmental problems of global concern, sulfur dioxide and nitrogen oxide are main precursor substances of acid rain, nitrogen oxide causing atmospheric pollution is mainly nitric oxide and nitrogen dioxide, the nitric oxide can act with hemoglobin to reduce the oxygen therapy function of blood, the nitrogen dioxide has strong stimulation to respiratory organs and can cause acute asthma, the nitrogen oxide can also harm plants, is corrosive to materials and has a destructive effect on the ozone layer. The government pays attention to the control work of the nitrogen oxide, environmental protection regulations become stricter day by day, and the emission reduction index of the nitrogen oxide is further determined.
Because the components of the hazardous waste are complex and often mixed, at present, the hazardous waste is mixed according to a certain proportion (organic and inorganic are mixed) and then is incinerated, the incinerated residue is treated by other methods, and the flue gas is treated by a tail gas treatment system. There is a problem that if the incineration effect is poor or the treatment of the exhaust gas is incomplete, polluting gases such as nitric oxide and nitrogen dioxide, dust, and the like are easily generated. Therefore, how to realize good incineration of hazardous waste incineration is a technical problem which needs to be solved urgently at present.
SUMMERY OF THE UTILITY MODEL
The main object of this application is to provide a hazardous waste incineration processing system, can realize the good burning that hazardous waste burns.
The specific technical scheme is as follows: a hazardous waste incineration disposal system comprises an incineration system and a flue gas treatment system; the burning system is formed by sequentially connecting a rotary kiln and a secondary combustion chamber, namely a smoke outlet of the rotary kiln is connected with a feed inlet of the secondary combustion chamber; flue gas processing system exhaust-heat boiler, quench tower, circulating fluidized bed, sack cleaner and caustic wash tower, exhaust-heat boiler air inlet pass through the pipeline and are connected with second combustion chamber exhanst gas outlet, and exhaust-heat boiler exhanst gas outlet is connected the air inlet with the quench tower and is connected, and the quench tower discharge gate is connected with the circulating fluidized bed feed inlet, and the circulating fluidized bed discharge gate is connected with the caustic wash tower through sack cleaner, draught fan, and the caustic wash tower tail gas passes through the chimney evacuation.
And furthermore, the two alkaline washing towers comprise a first alkaline washing tower and a second alkaline washing tower which are respectively connected in sequence, namely, an outlet of the induced draft fan is connected with a feed inlet of the first alkaline washing tower, a discharge hole of the first alkaline washing tower is connected with a feed inlet of the second alkaline washing tower, and a discharge hole of the second alkaline washing tower is connected with a chimney.
Further, a denitration agent feed inlet is formed in the feed inlet of the rotary kiln.
Further, a denitration agent feeding hole is formed in the inlet of the waste heat boiler.
The beneficial effects of this application lie in, realize the good burning that the hazardous waste burns, the running cost is low, the reaction product is nontoxic pollution-free, no accessory substance discharges.
Drawings
FIG. 1 is a device connection diagram of the present invention in which a denitration agent feed port is provided at an inlet of a waste heat boiler;
FIG. 2 is a connection diagram of the equipment of the present invention in which the denitration agent feed port is disposed at the rotary kiln feed port;
wherein, 1, a rotary kiln; 2, a second combustion chamber; 3, a waste heat boiler; 4, a quenching tower; 5 circulating the fluidized bed; 6, a bag-type dust collector; 7 induced draft fan; 8, a first-grade alkaline washing tower; 9, a secondary alkaline washing tower; 10, a chimney; 11, a denitration agent feed inlet a;12 denitration agent feed inlet b.
Detailed Description
Example 1
The hazardous waste incineration disposal system shown in FIG. 1 comprises an incineration system and a flue gas treatment system; the incineration system is formed by sequentially connecting a rotary kiln 1 and a secondary combustion chamber 2, namely a smoke outlet of the rotary kiln 1 is connected with a feed inlet of the secondary combustion chamber 2; flue gas processing system exhaust-heat boiler 3, quench tower 4, circulating fluidized bed 5, sack cleaner 6 and caustic wash tower, 3 air inlets of exhaust-heat boiler pass through pipeline and 2 flue gas exit linkage in second combustion chamber, 3 exhanst gas exits of exhaust-heat boiler are connected the air inlet with quench tower 4 and are connected, 4 discharge gates of quench tower are connected with 5 feed inlets of circulating fluidized bed, 5 discharge gates of circulating fluidized bed are through sack cleaner 6, draught fan 7 is connected with the caustic wash tower, the caustic wash tower tail gas passes through the chimney evacuation, the caustic wash tower is used for the acid gas to absorb.
Further, the two alkaline washing towers comprise a first-level alkaline washing tower 8 and a second-level alkaline washing tower 9, the first-level alkaline washing tower 8 and the second-level alkaline washing tower 9 are sequentially connected, namely, an outlet of the induced draft fan 7 is connected with a feed inlet of the first-level alkaline washing tower 8, a discharge hole of the first-level alkaline washing tower 8 is connected with a feed inlet of the second-level alkaline washing tower 9, and a discharge hole of the second-level alkaline washing tower 9 is connected with a chimney.
Further, a denitration agent feed inlet b11 is arranged at the inlet of the waste heat boiler 3.
Example 2
The hazardous waste incineration disposal system shown in FIG. 2 comprises an incineration system and a flue gas treatment system; the incineration system is formed by sequentially connecting a rotary kiln 1 and a secondary combustion chamber 2, namely a smoke outlet of the rotary kiln 1 is connected with a feed inlet of the secondary combustion chamber 2; flue gas processing system exhaust-heat boiler 3, quench tower 4, circulating fluidized bed 5, sack cleaner 6 and alkaline washing tower, 3 air inlets of exhaust-heat boiler pass through the pipeline and 2 flue gas exit linkage in second combustion chamber, 3 exhanst gas exits of exhaust-heat boiler are connected the air inlet with quench tower 4 and are connected, 4 discharge gates of quench tower are connected with 5 feed inlets of circulating fluidized bed, 5 discharge gates of circulating fluidized bed are through sack cleaner 6, draught fan 7 is connected with the alkaline washing tower, alkaline washing tower tail gas passes through the chimney evacuation, the alkaline washing tower is used for the acid gas to absorb.
Further, the two alkaline washing towers comprise a first-level alkaline washing tower 8 and a second-level alkaline washing tower 9, the first-level alkaline washing tower 8 and the second-level alkaline washing tower 9 are sequentially connected, namely, an outlet of the induced draft fan 7 is connected with a feed inlet of the first-level alkaline washing tower 8, a discharge hole of the first-level alkaline washing tower 8 is connected with a feed inlet of the second-level alkaline washing tower 9, and a discharge hole of the second-level alkaline washing tower 9 is connected with a chimney.
Further, a denitration agent feed port a12 is arranged at the feed port of the rotary kiln 1.
The incineration system consists of a rotary kiln 1 and a secondary combustion chamber 2, various dangerous wastes are pretreated and prepared in a menu and then enter the rotary kiln 1 through different feeding ways, under the continuous rotation of the rotary kiln 1, the wastes are continuously turned, heated, dried, vaporized and combusted in the kiln, residues fall into a residue hopper from the kiln tail and are continuously discharged by a water-sealed slag extractor, flue gas generated by combustion enters the secondary combustion chamber 2 from the kiln tail for high-temperature combustion again, and the dangerous wastes entering the incineration system are fully and thoroughly combusted.
The high-temperature flue gas from the secondary combustion chamber 2 enters a waste heat boiler 3 to recover part of heat energy in the flue gas, and then enters a quench tower 4 to realize rapid cooling of the flue gas. The cooled flue gas is purified by an acid gas through a circulating fluidized bed 5, enters a bag-type dust remover 6 to remove dust, is introduced into a primary alkali washing tower 8 and a secondary alkali washing tower 9 through a draught fan 7 to spray circulating alkali liquor, further removes harmful components in the flue gas, and is discharged into the atmosphere through a chimney after the purified flue gas reaches a hazardous waste incineration pollution control standard GB 18484-2020.
In the high-temperature incineration process of the conventional wastes, NO in the flue gas generated after incineration x Mainly in the form of NO, initially emitted NO x The content of NO in the flue gas is about 95 percent, so the denitration of the flue gas mainly aims at removing NO in the flue gas.
The methylamine water solution, methylamine ethanol solution and methylamine methanol solution have strong irritation and ammonia odor, have the dangerous characteristics of flammability and explosiveness, and belong to dangerous wastes which are relatively difficult to dispose. Methylamine is burnt and decomposed after entering the head of the rotary kiln to generate NH 2 、CO、H 2 In which NH produced by decomposition 2 Reacts with NO in the flue gas to convert NO in the flue gas into pollution-free N 2 Therefore, the aim of denitration is achieved, and the equation is as follows:
NH 2 +NO→N 2 +H 2 O
meanwhile, in the combustion decomposition process of methylamine, oxygen in the surrounding environment is consumed, and a reducing atmosphere in a CO-rich state is rapidly formed at a local position in the flue gas to exciteNO reduction reaction is carried out, so that the denitration efficiency is further improved; the temperature of the kiln tail is controlled to be 900-1000 ℃, the reaction rate of flue gas denitration can be ensured, and relatively high NO can be obtained in a short retention time X And (4) removing efficiency.
For comprehensive hazardous waste disposal enterprises, the calorific value of the collected waste is relatively high, and the heat load in the rotary kiln in unit time is high, so that the yield improvement and efficiency improvement of an incineration system are influenced. Compared with other organic waste liquid, the heat value of the methylamine water solution is in a relatively lower level, so that the methylamine water waste liquid is sprayed and burnt from the kiln head of the rotary kiln, the effect of reducing the heat load of the rotary kiln in unit time can be achieved, and the positive effect on the yield improvement and efficiency improvement of a burning system can be achieved.
The method for denitration by burning hazardous wastes comprises the following steps:
step S1, in the running process of a hazardous waste incineration system, spraying a certain proportion of waste denitration agent into a rotary kiln for incineration through a waste liquid feeding system;
specifically, in the process of normally disposing wastes in a hazardous waste incineration system, nitrogen oxides in flue gas after high-temperature incineration are generally in a high level, a certain proportion of waste denitration agents are sprayed into a rotary kiln for incineration through a waste liquid feeding system, the waste denitration agents comprise one of waste monomethylamine aqueous solution, dimethylamine aqueous solution, trimethylamine aqueous solution, methylamine ethanol solution and methylamine methanol solution, the concentration of the waste denitration agents is generally 10-40%, the waste denitration agents are different from a common denitration method, the feeding position of the waste denitration agents is the rotary kiln head, the calorific value of the waste denitration agents is relatively low, the waste denitration agents are sprayed and burnt from the rotary kiln head, the kiln head temperature is favorably controlled, and the positive effect on the efficiency of incineration and production improvement is achieved.
S2, controlling the feeding amount of the waste denitration agent and the kiln temperature of the rotary kiln;
specifically, due to the difference between the content of nitrogen oxides in flue gas and the concentration of the waste denitration agent, the feeding amount can be adjusted, preferably, the feeding flow rate of the waste denitration agent is 200-400L/h, it is easily understood that, in order to ensure that the reaction of the waste denitration agent and flue gas is in a proper temperature range, preferably, the kiln temperature of the rotary kiln is controlled to be generally 950-1100 ℃.
And S3, removing the content of nitrogen oxide in the flue gas by utilizing the reaction between the flue gas after the waste incineration, and realizing the standard emission of the flue gas.
Preferably, the removal efficiency of nitrogen oxides in the flue gas by using the reaction between the flue gas after waste incineration is 50-65%, and preferably, the flue gas after nitrogen oxides removal reaches the national hazardous waste incineration pollution control standard GB18484-2020 before being discharged.
In this embodiment, through spouting the discarded denitrifier from the rotary kiln hood, control the feeding volume and the rotary kiln temperature of discarded denitrifier, utilize the reaction between the waste incineration back flue gas to get rid of the content of nitrogen oxide in the flue gas, realize that the flue gas is up to standard discharges, finally realize waste comprehensive utilization, the difficult waste of handling obtains effectual processing and disposes, economic benefits is showing, realize the denitration simultaneously in the rotary kiln, reduce the risk of boiler scale deposit, flue blockage, have running cost low, the reaction product is nontoxic pollution-free, advantages such as by-product emission of no side product.
The present invention will be described in detail with reference to the following embodiments in order to make the aforementioned objects, features and advantages of the invention more comprehensible.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention, however, the present invention may be practiced otherwise than as specifically described herein, and it will be appreciated by those skilled in the art that the present invention may be practiced without departing from the spirit and scope of the present invention and that the present invention is not limited by the specific embodiments disclosed below.
In addition, the experimental methods used in the examples described below are all conventional methods unless otherwise specified, the materials and reagents used therein are commercially available unless otherwise specified, and the equipment used in the experiments are well known to those skilled in the art without otherwise specified.
Inventive example 1
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste treatment disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of disposing 3.146% nitrogen content conventional waste by a hazardous waste incineration system, the content of nitrogen oxides in the flue gas is 264-269mg/m as shown by an online monitoring system before treatment, the waste monomethylamine aqueous solution with the concentration of 20% is sprayed into a rotary kiln head through a waste liquid feeding system, the feeding flow of the waste monomethylamine aqueous solution is controlled to be 290-300L/h, the temperature of the rotary kiln is controlled to be 950-960 ℃, and after 3-4min, the online monitoring system shows that the main components of the flue gas after incineration are as follows: oxygen content is 12.1-12.6%, water content is 19.4-19.9%, smoke dust is 1.7-2.2mg/m for thin film fruit growing, carbon monoxide is 1.1-1.6 mg/m for thin film fruit growing, sulfur dioxide is 0.1-0.6mg/m for thin film fruit growing, hydrogen chloride is 0-0.5mg/m for thin film fruit growing, nitrogen oxide is 117-122mg/m for thin film fruit growing, normal feeding of the waste methylamine water solution is continuously kept, and nitrogen oxide content in smoke gas is stabilized at about 117-122mg/m for thin film fruit growing.
Flue gas treatment effect: the denitration efficiency of the flue gas treatment by spraying and burning 20% of waste methylamine water solution through the kiln head of the rotary kiln is 54.6-56.5%, and the treated flue gas is discharged after reaching the national hazardous waste incineration pollution control standard GB 18484-2020); when the method is used for treating the flue gas, the boiler has no obvious scale formation, and is planned to be cleaned once in 1 year; the flue is not obviously blocked, and the flue is planned to be cleaned once in 1 year.
Comparative example 1
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of disposing 3.146% nitrogen content conventional waste in a hazardous waste incineration system, an online monitoring system before treatment shows that the content of nitrogen oxides in flue gas is 264-269mg/m, urea solution with the concentration of 20% is sprayed into a rotary kiln head through a waste liquid feeding system, the feeding flow of the urea solution is controlled to be 290-300L/h, the temperature of the rotary kiln is controlled to be 950-960 ℃, and after 3-4min, the online monitoring system shows that the main components of the flue gas after incineration are as follows: oxygen content is 12.1-12.6%, water content is 19.4-19.9%, smoke dust is 1.7-2.2mg/m for carrying out thin film crop cultivation, carbon monoxide is 1.1-1.6 mg/m for carrying out thin film crop cultivation, sulfur dioxide is 0.1-0.6mg/m for carrying out thin film crop cultivation, hydrogen chloride is 0-0.5mg/m for carrying out thin film crop cultivation, nitrogen oxide is 261-266mg/m for carrying out thin film crop cultivation, normal feeding of urea solution is continuously kept, and nitrogen oxide content in smoke gas is stabilized at about 261-266mg/m for carrying out thin film crop cultivation.
Flue gas treatment effect: the flue gas treatment by spraying and burning 20% urea solution at the kiln head of the rotary kiln has no obvious denitration effect, and the treated flue gas does not reach the national hazardous waste incineration pollution control standard GB 18484-2020.
Comparative example 2
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste treatment disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of disposing 3.146% nitrogen content conventional waste in a hazardous waste incineration system, an online monitoring system before treatment shows that the content of nitrogen oxides in flue gas is 264-269mg/m, urea solution with the concentration of 20% is sprayed into an inlet of a waste heat boiler through a denitration system, the feeding flow of the urea solution is controlled to be 290-300L/h, the kiln temperature of a rotary kiln is controlled to be 950-960 ℃, and after 3-4min, the online monitoring system shows that the main components of the flue gas after incineration are as follows: oxygen content is 12.1-12.6%, water content is 19.4-19.9%, smoke dust is 1.7-2.2mg/m for carrying out thin film crop cultivation, carbon monoxide is 1.1-1.6 mg/m for carrying out thin film crop cultivation, sulfur dioxide is 0.1-0.6mg/m for carrying out thin film crop cultivation, hydrogen chloride is 0-0.5mg/m for carrying out thin film crop cultivation, nitrogen oxide is 151-156mg/m for carrying out thin film crop cultivation, normal feeding of urea solution is continuously kept, and nitrogen oxide content in smoke gas is stabilized at about 151-156mg/m for carrying out thin film crop cultivation.
Flue gas treatment effect: 20% urea solution is sprayed from an inlet of a boiler through a denitration system, the denitration efficiency of the flue gas treatment is 42.0-43.9%, and the treated flue gas is discharged after reaching the national hazardous waste incineration pollution control standard GB 18484-2020; by adopting the method for treatment, the flue gas boiler has obvious scaling, and is planned to be cleaned once in 6 months; the flue is obviously blocked, and the planned cleaning is carried out once in 6 months.
Inventive example 2
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste treatment disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of treating 3.382% nitrogen content conventional waste by a hazardous waste incineration system, an online monitoring system before treatment shows that the content of nitrogen oxides in flue gas is 277-282mg/m, a waste dimethylamine aqueous solution with the concentration of 30% is sprayed into a rotary kiln head through a waste liquid feeding system, the feeding flow of the waste dimethylamine aqueous solution is controlled to be 340-350L/h, the temperature of the rotary kiln is controlled to be 1000-1010 ℃, and after 3-4min, the online monitoring system shows that the main components of the flue gas after incineration are as follows: oxygen content is 13.3-13.8%, water content is 18.6-19.1%, smoke dust is 0.2-0.7mg/m for carrying out thin film crop cultivation, carbon monoxide is 0.4-0.9mg/m for carrying out thin film crop cultivation, sulfur dioxide is 0.4-0.9mg/m for carrying out thin film crop cultivation, hydrogen chloride is 0.3-0.8mg/m for carrying out thin film crop cultivation, nitrogen oxide is 114-119mg/m for carrying out thin film crop cultivation, normal feeding of waste dimethylamine aqueous solution is continuously kept, and nitrogen oxide content in smoke is stable at about 114-119mg/m for carrying out thin film crop cultivation.
Flue gas treatment effect: the denitration efficiency of flue gas treatment by spraying and burning 30% waste dimethylamine aqueous solution at the kiln head of a rotary kiln is 57.8-59.6%, and the treated flue gas is discharged after reaching the national hazardous waste incineration pollution control standard GB 18484-2020; by adopting the method for treatment, the flue gas boiler has no obvious scale formation, and is planned to be cleaned once in 1 year; the flue is not obviously blocked, and is planned to be cleaned once in 1 year.
Inventive example 3
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste treatment disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of treating 3.546% nitrogen content conventional waste by a hazardous waste incineration system, an online monitoring system before treatment shows that the content of nitrogen oxides in flue gas is 299-304mg/m, waste trimethylamine aqueous solution with the concentration of 40% is sprayed into a kiln head of a rotary kiln through a waste liquid feeding system, the feeding flow of the waste trimethylamine aqueous solution is controlled to be 370-380L/h, the temperature of the rotary kiln is controlled to be 1050-1060 ℃, and after 3-4min, the online monitoring system shows that the main components of the incinerated flue gas are as follows: oxygen content is 11.1-11.6%, water content is 18.2-18.7%, smoke dust is 0.3-0.8mg/m for carrying out fruit bearing, carbon monoxide is 0.4-0.9mg/m for carrying out fruit bearing, sulfur dioxide is 0.4-0.9mg/m for carrying out fruit bearing, hydrogen chloride is 0.3-0.8mg/m for carrying out fruit bearing, nitric oxide is 113-118mg/m for carrying out fruit bearing, normal feeding of waste trimethylamine aqueous solution is continuously kept, and nitric oxide content in flue gas is stabilized around 113-118mg/m for carrying out fruit bearing.
Flue gas treatment effect: the denitration efficiency of flue gas treatment is 61.2-62.8% by spraying and burning 40% waste trimethylamine aqueous solution at the kiln head of a rotary kiln, and the treated flue gas is discharged after reaching the national hazardous waste incineration pollution control standard GB 18484-2020; when the method is used for treating the flue gas, the boiler has no obvious scale formation, and is planned to be cleaned once in 1 year; the flue is not obviously blocked, and is planned to be cleaned once in 1 year.
Comparative example 3
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of disposing 3.546% nitrogen content conventional waste by a hazardous waste incineration system, an online monitoring system before treatment shows that the content of nitrogen oxides in flue gas is 299-304mg/m, urea solution with the concentration of 40% is sprayed into an inlet of a waste heat boiler through a denitration system, the feed flow of the urea solution is controlled to be 370-380L/h, the kiln temperature of a rotary kiln is controlled to be 1050-1060 ℃, and after 3-4min, the online monitoring system shows that the main components of the flue gas after incineration are as follows: oxygen content is 11.1-11.6%, water content is 18.2-18.7%, smoke dust is 0.3-0.8mg/m for harvesting folium Brassicae Junceae, carbon monoxide is 0.4-0.9mg/m for harvesting semen Brassicae Junceae, sulfur dioxide is 0.4-0.9mg/m for harvesting semen Brassicae Junceae, hydrogen chloride is 0.3-0.8mg/m for harvesting semen Brassicae Junceae, nitrogen oxide is 158-163mg/m for harvesting semen Brassicae Junceae, normal feeding of urea solution is continuously kept, and nitrogen oxide content in flue gas is stabilized at about 158-163mg/m for harvesting semen Brassicae Junceae.
Flue gas treatment effect: 40% urea solution is sprayed from an inlet of a boiler through a denitration system, the denitration efficiency of the flue gas treatment is 46.4-48.0%, and the treated flue gas is discharged after reaching the national hazardous waste incineration pollution control standard GB 18484-2020; when the method is adopted to treat the flue gas, the boiler has obvious scaling, and is planned to be cleaned once in 6 months; the flue is obviously blocked, and the planned cleaning is carried out once in 6 months.
Inventive example 4
The incineration disposal capacity is designed to be 30t/d by taking a hazardous waste incineration system of a certain hazardous waste treatment disposal center as a disposal object.
The method of the invention is used for treating the flue gas of the hazardous waste incineration system: in the process of disposing 3.472% nitrogen-containing conventional waste in a hazardous waste incineration system, displaying that the content of nitrogen oxides in flue gas is 283-288mg/m by an online monitoring system before treatment, spraying 33% waste methylamine ethanol or methylamine methanol solution into a rotary kiln head through a waste liquid feeding system, controlling the feeding flow of the waste methylamine ethanol or methylamine methanol solution to be 240-250L/h, controlling the temperature of the rotary kiln to be 1090-1100 ℃, and displaying that the main components of the incinerated flue gas are as follows by the online monitoring system after 3-4 min: oxygen content is 12.5-13.0%, water content is 18.4-18.9%, smoke dust is 0.5-1.0mg/m for harvesting folium Brassicae Junceae, carbon monoxide is 0.3-0.8mg/m for harvesting, sulfur dioxide is 0.7-1.2mg/m for harvesting, hydrogen chloride is 0.4-0.9mg/m for harvesting, nitrogen oxide is 135-140mg/m for harvesting, normal feeding of waste methylamine ethanol or methylamine methanol solution is continuously maintained, and nitrogen oxide content in flue gas is stabilized at about 135-140mg/m for harvesting.
Flue gas treatment effect: the denitration efficiency of flue gas treatment by spraying 33% of waste methylamine ethanol or methylamine methanol solution through a rotary kiln head is 51.4-53.1%, and the treated flue gas is discharged after reaching the national hazardous waste incineration pollution control standard GB 18484-2020); the method is adopted to treat the flue gas, the boiler has no obvious scale formation, and the boiler is planned to be cleaned once in 1 year; the flue is not obviously blocked, and is planned to be cleaned once in 1 year.
Claims (4)
1. A hazardous waste incineration disposal system is characterized by comprising an incineration system and a flue gas treatment system;
the incineration system is formed by sequentially connecting a rotary kiln (1) and a secondary combustion chamber (2), namely a smoke outlet of the rotary kiln (1) is connected with a feed inlet of the secondary combustion chamber (2);
flue gas processing system includes exhaust-heat boiler (3), quench tower (4), circulating fluidized bed (5), sack cleaner (6) and alkali wash tower, exhaust-heat boiler (3) air inlet passes through the pipeline and is connected with second combustion chamber (2) exhanst gas outlet, exhaust-heat boiler (3) exhanst gas outlet is connected the air inlet with quench tower (4) and is connected, quench tower (4) discharge gate is connected with circulating fluidized bed (5) feed inlet, circulating fluidized bed (5) discharge gate is through sack cleaner (6), draught fan (7) are connected with the alkali wash tower, the alkali wash tower tail gas passes through the chimney evacuation.
2. The hazardous waste incineration system according to claim 1, wherein the caustic towers comprise two primary caustic towers (8) and two secondary caustic towers (9), the primary caustic tower (8) and the secondary caustic tower (9) are sequentially connected, namely, an outlet of the induced draft fan (7) is connected with a feed inlet of the primary caustic tower (8), a discharge outlet of the primary caustic tower (8) is connected with a feed inlet of the secondary caustic tower (9), and a discharge outlet of the secondary caustic tower (9) is connected with a chimney.
3. A hazardous waste incineration disposal system according to claim 2, wherein the feed inlet of the rotary kiln (1) is provided with a denitrifier feed inlet.
4. The hazardous waste incineration disposal system of claim 2, wherein a denitration agent inlet is provided at an inlet of the exhaust-heat boiler (3).
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