CN110986053A - Method for treating high-halogen hazardous waste - Google Patents

Method for treating high-halogen hazardous waste Download PDF

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Publication number
CN110986053A
CN110986053A CN201911123883.4A CN201911123883A CN110986053A CN 110986053 A CN110986053 A CN 110986053A CN 201911123883 A CN201911123883 A CN 201911123883A CN 110986053 A CN110986053 A CN 110986053A
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China
Prior art keywords
flue gas
denitration
halogen
temperature
feeding
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Application number
CN201911123883.4A
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Chinese (zh)
Inventor
樊俊
周强
朱耀祖
盛骁
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Jiangsu Zhongding Environment Engineering Share Co ltd
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Jiangsu Zhongding Environment Engineering Share Co ltd
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Priority to CN201911123883.4A priority Critical patent/CN110986053A/en
Publication of CN110986053A publication Critical patent/CN110986053A/en
Withdrawn legal-status Critical Current

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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44Details; Accessories
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J1/00Removing ash, clinker, or slag from combustion chambers
    • F23J1/06Mechanically-operated devices, e.g. clinker pushers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/02Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/02Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025Arrangements 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/06Arrangements of devices for treating smoke or fumes of coolers
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/08Arrangements of devices for treating smoke or fumes of heaters
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00Combustion technologies with mitigation potential
    • Y02E20/30Technologies for a more efficient combustion or heat usage

Abstract

The invention relates to a method for treating hazardous waste, in particular to a method for treating high-halogen hazardous waste. The high-halogen hazardous waste is sent into a rotary kiln through a feeding mechanism to be incinerated, then enters a secondary combustion chamber from the rotary kiln to be incinerated for the second time to obtain high-acid flue gas with thoroughly decomposed dioxin, and then the high-acid flue gas sequentially undergoes denitration, waste heat recovery, quenching, desulfurization, dust removal, precooling, deacidification and heating to reach the emission standard, so that the high-halogen hazardous waste is treated. The method can save energy and water resources, does not corrode subsequent equipment, and does not cause the problem of the dioxin discharge exceeding the standard.

Description

Method for treating high-halogen hazardous waste
Technical Field
The invention relates to a method for treating hazardous waste, in particular to a method for treating high-halogen hazardous waste.
Background
In recent years, the hazardous waste industry has been rapidly developed. Along with the increase of government environmental management, the structure of the hazardous waste is changed, the components are more and more complex, the disposal difficulty is more and more high, and the content of halogen such as chlorine, sulfur, fluorine and the like in the hazardous waste is higher and higher from the industries such as pesticide, chemical engineering and the like.
At present, the traditional hazardous waste treatment method comprises the following steps: the method comprises the following steps of primary incineration, secondary incineration, waste heat recovery, quenching, dry reaction, dust removal, deacidification and temperature rise, and the tail gas emission standard can be met. The flue gas generated by burning the high-halogen hazardous waste has high acidity and is easy to corrode a waste heat boiler, so that when the high-halogen hazardous waste is treated by adopting the traditional hazardous waste treatment method, the waste heat recovery step needs to be changed into a water cooling step, the waste heat boiler cannot be used for waste heat utilization, and energy and water resources are wasted. Meanwhile, the incineration of the high-halogen hazardous waste can generate a large amount of hydrogen chloride and sulfur dioxide to increase the corrosion of subsequent equipment. Moreover, high-halogen hazardous waste incineration can generate a large amount of hydrogen chloride and chloride ions, the probability of generating dioxin by adopting a traditional hazardous waste treatment method is very high, and the problem of exceeding the standard of dioxin is easy to occur during tail gas emission.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a method for treating high-halogen hazardous waste, which can save energy and water resources, does not corrode subsequent equipment, and does not cause the problem of overproof dioxin emission.
In order to solve the problems, the following technical scheme is provided:
the method for treating the high-halogen dangerous waste is characterized by comprising the following steps of:
first, primary incineration
And (3) feeding the high-halogen hazardous waste into a rotary kiln through a feeding mechanism to be incinerated to 800-1000 ℃, feeding flue gas and slag generated by incineration into a secondary combustion chamber, and discharging the slag from a slag extractor at the bottom of the secondary combustion chamber.
Second, secondary incineration
And (3) continuously and fully incinerating the flue gas entering the secondary combustion chamber to 1100-1150 ℃, and staying in the secondary combustion chamber for more than 2s to obtain the high-acid flue gas.
Thirdly, denitration
And (3) feeding the flue gas after incineration in the secondary combustion chamber into a cooling denitration tower, cooling the flue gas to 930-970 ℃ through alkali liquor in the cooling denitration tower, and then carrying out denitration treatment on the cooled flue gas.
Fourthly, recovering waste heat
And (4) feeding the denitrated flue gas into a waste heat boiler for waste heat recovery, so that the temperature of the flue gas at the outlet of the boiler is reduced to 500-550 ℃.
Fifth, quench cooling
And (3) sending the flue gas after waste heat recovery into a quenching tower, and quenching the flue gas to be below 200 ℃ within 1S, so as to avoid the regeneration of dioxin at 280-320 ℃.
Sixth step, deacidifying by dry method
And (3) sending the quenched flue gas into a dry reaction device to remove dioxin, heavy metals and acid gases in the flue gas.
Seventh, removing dust
And (4) feeding the deacidified flue gas into a dust remover so as to remove dust in the flue gas.
Eighth step, precooling
And (3) feeding the dedusted flue gas into a precooler, so that the temperature of the flue gas is reduced to 65-75 ℃.
Ninth step, deacidifying
And deacidifying the pre-cooled smoke through a deacidification tower.
The tenth step of heating
The deacidified flue gas is heated to a temperature of more than 130 ℃ by a reheater, and the emission standard can be met.
The cooling denitration tower in the denitration step comprises an SNCR cooling denitration tower arranged in front of the waste heat boiler, and the denitration treatment mode is that urea or ammonia water is sprayed into the cooling denitration tower for denitration in a temperature range of 930-970 ℃.
The invention further improves the scheme that the cooling and denitration tower also comprises an SCR denitration tower, and the SCR denitration tower is connected in series between the SNCR cooling and denitration tower and the waste heat boiler. Such an improvement has the advantage that the denitration effect can be further improved.
The invention is further improved in that the feeding mechanism in the primary incineration step is an SMP system or a double-stage screw conveyor. The improved advantages can ensure the uniformity of material mixing, and make the smoke components generated by the burning system relatively uniform and have good stability.
And the desulfurization step comprises the steps of spraying activated carbon and sodium bicarbonate ground into fine powder into the dry-type reaction device through a Roots blower, adsorbing dioxin and heavy metals by using the activated carbon, and removing acid gas in the flue gas by using the sodium bicarbonate.
The dust remover in the dust removing cloth is a cloth bag dust remover, and in the dust removing process, activated carbon and baking soda contained in the smoke can be adsorbed on the surface of a filter bag of the cloth bag dust remover so as to continuously react with the smoke and further remove dioxin, heavy metals and acid gases in the smoke.
The number of deacidification towers in the deacidification step is two, and the flue gas passes through the two deacidification towers in sequence to carry out secondary deacidification.
By adopting the scheme, the method has the following advantages:
the high-halogen dangerous waste is sent into the rotary kiln to be burnt through the feeding mechanism, then enters the secondary combustion chamber from the rotary kiln to be burnt for the second time to obtain the high-acid flue gas with thoroughly decomposed dioxin, and then the high-acid flue gas sequentially undergoes denitration, waste heat recovery, rapid cooling, desulfurization, dust removal, precooling, deacidification and heating to reach the emission standard. In the cooling and denitration step of the treatment method, the flue gas is cooled by using the alkali liquor, and then the flue gas is subjected to denitration treatment. Therefore, the step of waste heat recovery still exists, so that energy and water resources are saved, and the service life of subsequent equipment is prolonged. In addition, after the flue gas is cooled and denitrated, hydrogen chloride and chloride ions in the flue gas are reduced, and dioxin is not easily regenerated in the subsequent treatment steps, so that the problem that the emission of the dioxin exceeds the standard is avoided.
Detailed Description
Example one
The method for treating the high-halogen dangerous waste comprises the following steps:
first, primary incineration
And (3) sending the high-halogen hazardous waste into a rotary kiln through an SMP system to be incinerated to 800 ℃, introducing smoke and slag generated by incineration into a secondary combustion chamber, and discharging the slag from a slag extractor at the bottom of the secondary combustion chamber.
Second, secondary incineration
And (4) continuously and fully incinerating the flue gas entering the secondary combustion chamber to 1100 ℃, and staying in the secondary combustion chamber for 2s to obtain the high-acid flue gas.
Thirdly, denitration
And (2) feeding the flue gas burned in the secondary combustion chamber into an SNCR (selective non-catalytic reduction) cooling and denitration tower arranged in front of a waste heat boiler, cooling the flue gas to 930 ℃ by the cooling and denitration tower through alkali liquor, and spraying urea into the cooling and denitration tower to denitrate in a temperature interval of 930 ℃.
Fourthly, recovering waste heat
And (4) feeding the denitrated flue gas into a waste heat boiler for waste heat recovery, so that the temperature of the flue gas at the outlet of the boiler is reduced to 500 ℃.
Fifth, quench cooling
And (3) sending the flue gas after waste heat recovery into a quenching tower, and quenching the temperature of the flue gas to 150 ℃ in 1S, thereby avoiding the regeneration of dioxin at 280 ℃.
Sixth step, deacidifying by dry method
And (3) feeding the quenched flue gas into a dry reaction device, spraying activated carbon and sodium bicarbonate ground into the dry reaction device through a Roots blower, adsorbing dioxin and heavy metals by using the activated carbon, and removing acid gas in the flue gas by using the sodium bicarbonate.
Seventh, removing dust
And (4) feeding the deacidified flue gas into a bag-type dust remover so as to remove dust in the flue gas. In the dust removal process, activated carbon and baking soda contained in the flue gas can be adsorbed on the surface of a filter bag of the bag-type dust remover, so that the activated carbon and the baking soda can continuously react with the flue gas, and dioxin, heavy metals and acid gases in the flue gas are further removed.
Eighth step, precooling
And (3) sending the dedusted flue gas into a precooler, so that the temperature of the flue gas is reduced to 65 ℃.
Ninth step, deacidifying
And sequentially passing the pre-cooled flue gas through two deacidification towers for secondary deacidification.
The tenth step of heating
The deacidified flue gas is heated to 130 ℃ by a reheater, and the emission standard can be met.
The tenth step, discharge
And (4) sending the tail gas into a chimney through an exhaust fan, and discharging the tail gas into the atmosphere to finish the treatment of the high-halogen dangerous waste.
Example two
The method for treating the high-halogen dangerous waste comprises the following steps:
first, primary incineration
And (3) feeding the high-halogen dangerous waste into a rotary kiln through a double-stage screw conveyor to be incinerated to 1000 ℃, feeding flue gas and slag generated by incineration into a secondary combustion chamber, and discharging the slag from a slag extractor at the bottom of the secondary combustion chamber.
Second, secondary incineration
And (3) continuously and fully incinerating the flue gas entering the secondary combustion chamber to 1150 ℃, and staying in the secondary combustion chamber for 3s to obtain the high-acid flue gas.
Thirdly, denitration
And (3) feeding the flue gas burned in the secondary combustion chamber into an SNCR (selective non-catalytic reduction) cooling and denitration tower arranged in front of a waste heat boiler, cooling the flue gas to 970 ℃ by the cooling and denitration tower through alkali liquor, and spraying ammonia water into the cooling and denitration tower to denitrate in a 970 ℃ temperature interval.
Fourthly, recovering waste heat
And (4) sending the denitrated flue gas into a waste heat boiler for waste heat recovery, so that the temperature of the flue gas at the outlet of the boiler is reduced to 550 ℃.
Fifth, quench cooling
And (3) sending the flue gas after waste heat recovery into a quenching tower, and quenching the temperature of the flue gas to 200 ℃ at 0.5S, thereby avoiding the regeneration of dioxin at 320 ℃.
Sixth step, deacidifying by dry method
And (3) feeding the quenched flue gas into a dry reaction device, spraying activated carbon and sodium bicarbonate ground into the dry reaction device through a Roots blower, adsorbing dioxin and heavy metals by using the activated carbon, and removing acid gas in the flue gas by using the sodium bicarbonate.
Seventh, removing dust
And (4) feeding the deacidified flue gas into a bag-type dust remover so as to remove dust in the flue gas. In the dust removal process, activated carbon and baking soda contained in the flue gas can be adsorbed on the surface of a filter bag of the bag-type dust remover, so that the activated carbon and the baking soda can continuously react with the flue gas, and dioxin, heavy metals and acid gases in the flue gas are further removed.
Eighth step, precooling
And (3) sending the dedusted flue gas into a precooler, so that the temperature of the flue gas is reduced to 75 ℃.
Ninth step, deacidifying
And sequentially passing the pre-cooled flue gas through two deacidification towers for secondary deacidification.
The tenth step of heating
The deacidified flue gas is heated to 150 ℃ by a reheater, so that the emission standard can be met,
the tenth step, discharge
And (4) sending the tail gas into a chimney through an exhaust fan, and discharging the tail gas into the atmosphere to finish the treatment of the high-halogen dangerous waste.
EXAMPLE III
The method for treating the high-halogen dangerous waste comprises the following steps:
first, primary incineration
And (3) feeding the high-halogen dangerous waste into a rotary kiln through a double-stage screw conveyor to be incinerated to 900 ℃, feeding flue gas and slag generated by incineration into a secondary combustion chamber, and discharging the slag from a slag extractor at the bottom of the secondary combustion chamber.
Second, secondary incineration
And (4) continuously and fully incinerating the flue gas entering the secondary combustion chamber to 1100 ℃, and staying in the secondary combustion chamber for 2s to obtain the high-acid flue gas.
Thirdly, denitration
Firstly, feeding the flue gas burned in the secondary combustion chamber into an SNCR (selective non-catalytic reduction) cooling and denitration tower arranged in front of a waste heat boiler, cooling the flue gas to 950 ℃ by the SNCR cooling and denitration tower through alkali liquor, and then spraying urea into the SNCR cooling and denitration tower in a temperature interval of 950 ℃ to carry out denitration. And then, feeding the flue gas subjected to denitration in the SNCR cooling denitration tower into an SCR denitration tower for secondary denitration.
Fourthly, recovering waste heat
And (4) conveying the flue gas subjected to secondary denitration into a waste heat boiler for waste heat recovery, so that the temperature of the flue gas at the outlet of the boiler is reduced to 550 ℃.
Fifth, quench cooling
And (3) sending the flue gas after waste heat recovery into a quenching tower, and quenching the flue gas to below 200 ℃ within 1S, so as to avoid the regeneration of dioxin at 300 ℃.
Sixth step, deacidifying by dry method
And (3) feeding the quenched flue gas into a dry reaction device, spraying activated carbon and sodium bicarbonate ground into the dry reaction device through a Roots blower, adsorbing dioxin and heavy metals by using the activated carbon, and removing acid gas in the flue gas by using the sodium bicarbonate.
Seventh, removing dust
And (4) feeding the deacidified flue gas into a bag-type dust remover so as to remove dust in the flue gas. In the dust removal process, activated carbon and baking soda contained in the flue gas can be adsorbed on the surface of a filter bag of the bag-type dust remover, so that the activated carbon and the baking soda can continuously react with the flue gas, and dioxin, heavy metals and acid gases in the flue gas are further removed.
Eighth step, precooling
And (3) sending the dedusted flue gas into a precooler, so that the temperature of the flue gas is reduced to 70 ℃.
Ninth step, deacidifying
And sequentially passing the pre-cooled flue gas through two deacidification towers for secondary deacidification.
The tenth step of heating
Heating the deacidified flue gas to 130 ℃ through a reheater, so that the emission standard can be met, and the treatment of the high-halogen hazardous waste is completed.
The tenth step, discharge
And (4) sending the tail gas into a chimney through an exhaust fan, and discharging the tail gas into the atmosphere to finish the treatment of the high-halogen dangerous waste.

Claims (7)

1. A method for treating high-halogen dangerous waste is characterized by comprising the following steps:
first, primary incineration
Feeding the high-halogen hazardous waste into a rotary kiln through a feeding mechanism to be incinerated to 800-1000 ℃, feeding flue gas and slag generated by incineration into a secondary combustion chamber, and discharging the slag from a slag extractor at the bottom of the secondary combustion chamber;
second, secondary incineration
The flue gas entering the secondary combustion chamber is continuously and fully incinerated to 1100-1150 ℃, and stays in the secondary combustion chamber for more than 2s to obtain high-acid flue gas;
thirdly, denitration
Feeding the flue gas burned in the secondary combustion chamber into a cooling denitration tower, cooling the flue gas to 930-970 ℃ through alkali liquor in the cooling denitration tower, and performing denitration treatment on the cooled flue gas;
fourthly, recovering waste heat
Feeding the denitrated flue gas into a waste heat boiler for waste heat recovery, so that the temperature of the flue gas at the outlet of the boiler is reduced to 500-550 ℃;
fifth, quench cooling
Sending the flue gas after waste heat recovery into a quench tower, and quenching the flue gas to below 200 ℃ within 1S, thereby avoiding the regeneration of dioxin at 280-320 ℃;
sixth step, deacidifying by dry method
Sending the quenched flue gas into a dry-type reaction device to remove dioxin, heavy metals and acid gases in the flue gas;
seventh, removing dust
Feeding the deacidified flue gas into a dust remover so as to remove dust in the flue gas;
eighth step, precooling
Sending the dedusted flue gas into a precooler, so that the temperature of the flue gas is reduced to 65-75 ℃;
ninth step, deacidifying
Deacidifying the pre-cooled smoke through a deacidification tower;
the tenth step of heating
The deacidified flue gas is heated to a temperature of more than 130 ℃ by a reheater, and the emission standard can be met.
2. The method for treating high-halogen hazardous waste as set forth in claim 1, wherein the temperature-reducing denitration tower in the denitration step comprises an SNCR temperature-reducing denitration tower disposed in front of the exhaust-heat boiler, and the denitration treatment is performed by spraying urea or ammonia water into the temperature-reducing denitration tower at a temperature range of 930-970 ℃ to perform denitration.
3. The method according to claim 2, wherein the temperature-reducing denitration tower further comprises an SCR denitration tower, and the SCR denitration tower is connected in series between the SNCR temperature-reducing denitration tower and the exhaust-heat boiler.
4. The method for treating high-halogen hazardous waste according to claim 1, wherein the feeding mechanism in the primary incineration step is an SMP system or a two-stage screw conveyor.
5. The method for treating high-halogen hazardous waste as set forth in claim 1, wherein the desulfurization step is carried out by injecting activated carbon and finely powdered sodium bicarbonate into the dry reaction apparatus through a roots blower, adsorbing dioxin and heavy metals with the activated carbon, and removing acid gases from flue gas with the sodium bicarbonate.
6. The method for treating high-halogen hazardous wastes according to claim 5, wherein the dust collector in the dust collection cloth is a bag-type dust collector, and during the dust collection process, activated carbon and baking soda contained in the flue gas can be adsorbed on the surface of the filter bag of the bag-type dust collector, so as to continue to react with the flue gas, and further remove dioxin, heavy metals and acid gases in the flue gas.
7. The method for treating high-halogen dangerous waste as in any one of claims 1 to 6, wherein the deacidification step comprises two deacidification towers, and the flue gas passes through the two deacidification towers in sequence for secondary deacidification.
CN201911123883.4A 2019-11-19 2019-11-19 Method for treating high-halogen hazardous waste Withdrawn CN110986053A (en)

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CN113124411A (en) * 2021-04-13 2021-07-16 浙江省环保集团有限公司 Fluorine-containing hazardous waste treatment process

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Publication number Priority date Publication date Assignee Title
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113124411A (en) * 2021-04-13 2021-07-16 浙江省环保集团有限公司 Fluorine-containing hazardous waste treatment process

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