WO2022210389A1 - Système de traitement de polluants et procédé de traitement de polluants - Google Patents

Système de traitement de polluants et procédé de traitement de polluants Download PDF

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Publication number
WO2022210389A1
WO2022210389A1 PCT/JP2022/014537 JP2022014537W WO2022210389A1 WO 2022210389 A1 WO2022210389 A1 WO 2022210389A1 JP 2022014537 W JP2022014537 W JP 2022014537W WO 2022210389 A1 WO2022210389 A1 WO 2022210389A1
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Prior art keywords
exhaust gas
liquid water
recovery device
water
pollutant treatment
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PCT/JP2022/014537
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English (en)
Japanese (ja)
Inventor
達生 山本
浩之 河野
佑介 赤松
直樹 芳賀
義祐 仁平
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前田建設工業株式会社
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Priority to JP2023511183A priority Critical patent/JPWO2022210389A1/ja
Publication of WO2022210389A1 publication Critical patent/WO2022210389A1/fr

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    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/40—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by heating to effect chemical change, e.g. pyrolysis
    • 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
    • B01D53/14—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 absorption
    • 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
    • B01D53/14—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 absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/06—Recovery or working-up of waste materials of polymers without chemical reactions
    • C08J11/08—Recovery or working-up of waste materials of polymers without chemical reactions using selective solvents for polymer components
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D2101/00—Harmful chemical substances made harmless, or less harmful, by effecting chemical change
    • A62D2101/20—Organic substances
    • A62D2101/22—Organic substances containing halogen
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D2101/00—Harmful chemical substances made harmless, or less harmful, by effecting chemical change
    • A62D2101/20—Organic substances
    • A62D2101/28—Organic substances containing oxygen, sulfur, selenium or tellurium, i.e. chalcogen

Definitions

  • the present invention relates to a pollutant treatment system and a pollutant treatment method.
  • Some pollutants that require disposal are toxic when released into the environment, and pyrolysis using high temperatures such as incineration is sometimes adopted as a treatment method for detoxifying these pollutants. .
  • pyrolysis using high temperatures such as incineration is sometimes adopted as a treatment method for detoxifying these pollutants.
  • the process of pyrolysis may chemically decompose the pollutants themselves, the exhaust from the process may still contain by-products that should not be released into the environment as such.
  • Such by-products include dust, nitrogen oxides (NOx), sulfur oxides (SOx), hydrogen fluoride gas (HF), dioxins (polychlorinated benzoparadioxin, polychlorinated dibenzofuran, dioxin polychlorinated biphenyl) and the like.
  • NOx nitrogen oxides
  • SOx sulfur oxides
  • HF hydrogen fluoride gas
  • dioxins polychlorinated benzoparadioxin, polychlorinated dibenzofuran, dioxin polychlorinated biphenyl
  • Persistent organic fluorine compounds have been pointed out to have an effect on the human body, and because they are extremely chemically stable, they are known to cause environmental pollution over a long period of time without being naturally decomposed when released into the environment. there is Therefore, in order to safely decompose pollutants including the same substances released into the environment, they are thermally decomposed by heating them to a high temperature using a furnace.
  • Typical examples of such persistent organic fluorine compounds include PFOS (perfluorooctane sulfonic acid) and PFOA (perfluorooctanoic acid). These persistent organic fluorine compounds are contained in various chemicals such as fire extinguishing agents and cleaning agents, and must be disposed of safely without being released into the environment.
  • Fig. 1 is a diagram showing an overview of equipment that is currently used as a decomposition treatment facility for such persistent organic fluorine compounds.
  • contaminants containing persistent organic fluorine compounds are put into an incinerator (rotary kiln/secondary combustion furnace) 100 and thermally decomposed.
  • Exhaust gas from the incinerator 100 is heat-recovered by the boiler 101 and the temperature is lowered, then the temperature is further reduced to about 200 degrees Celsius or less by the quenching tower 102, and the dust is removed by the bag filter 103.
  • the need to cool the exhaust is to prevent thermal damage to the bag filter 103 .
  • the exhaust gas is further desulfurized and denitrified by the desulfurization and denitrification equipment 104 and released into the atmosphere from the chimney 105 .
  • Non-Patent Document 1 reports that de novo synthesis of dioxins occurs when the exhaust gas temperature peaks at 400 degrees Celsius (see FIG. 5 in particular).
  • hydrogen fluoride gas exhibits strong corrosiveness to metals at temperatures below about 500 degrees Celsius. Therefore, in the equipment shown in FIG. 1, deterioration of the subsequent flue, various equipment, and the chimney 105 progresses due to metal corrosion due to hydrogen fluoride gas contained in the exhaust gas whose temperature has been reduced by the boiler 101 and the quench tower 102. Therefore, there is a problem of shortening the equipment life.
  • the wet recovery device mechanically agitates the high-temperature exhaust gas and the liquid water.
  • the pollutant treatment system has a circulation device that circulates and supplies the liquid water to the wet recovery device and removes by-products from the circulating liquid water. .
  • the contaminant contains a persistent organic fluorine compound, and upon thermal decomposition of the contaminant, a reactive agent that reacts with fluorine to produce a harmless substance.
  • a contaminant treatment system comprising an inlet for introducing the
  • a pollutant treatment system according to any one of (1) to (5), further comprising an auxiliary recovery device for aerating the exhaust air that has passed through the wet recovery device into water.
  • the heating furnace includes a secondary combustion furnace, and the secondary combustion furnace is configured such that the volume can be changed by joining a plurality of shells so that they can be disassembled.
  • a contaminant treatment system consisting of:
  • thermally decomposing pollutants bringing high temperature exhaust gas of 500 degrees Celsius or higher containing by-products generated by the thermal decomposition into contact with liquid water, recovering the by-products in the liquid water;
  • the contaminant contains a persistent organic fluorine compound, and upon thermal decomposition of the contaminant, a reactive agent that reacts with fluorine to produce a harmless substance.
  • a contaminant treatment method comprising adding
  • the amount of the reactant to be added is determined in advance from the properties of the contaminant or the results of trial operation of the contaminant treatment method using the contaminant.
  • the pollutants include chlorides, and the toxicity equivalent of dioxins in the high-temperature exhaust cooled to 300 degrees Celsius or less is 0.1 ng.
  • FIG. 1 is a diagram showing an outline of equipment currently used as decomposition treatment equipment for persistent organic fluorine compounds.
  • 1 is a configuration diagram of a pollutant treatment system according to a preferred embodiment of the present invention
  • FIG. 1 is a schematic diagram of a portion of a pollutant treatment system with a supplemental hydrogen fluoride recovery device in the middle of the flue
  • FIG. 1 is an external side view of a wet recovery device used in a pollutant treatment system according to this embodiment
  • FIG. It is a figure which shows the internal structure of a wet collection
  • FIG. 1 is a flowchart of a method for treating contaminants containing persistent organic fluorine compounds by the contaminant treatment system according to the present embodiment
  • FIG. 4 is a graph showing measured values of exhaust temperature before and after wet recovery device values in the pollutant treatment system according to the example.
  • FIG. 4 is a graph showing measured temperatures of circulated liquid water in the pollutant treatment system according to the same embodiment;
  • 4 is a table showing the measured values and the removal rate of each by-product from the exhaust.
  • 10 is a table showing the results of measurement of dioxin concentration contained in exhaust gas after passing through a wet recovery device and dioxin concentration in circulating water used in the wet recovery device under conditions 7 and 8.
  • FIG. 4 is a graph showing measured values of exhaust temperature before and after wet recovery device values in the pollutant
  • FIG. 2 is a configuration diagram of a pollutant treatment system 1 according to a preferred embodiment of the present invention.
  • the contaminant treatment system 1 has a configuration in which a heating furnace 2, a desuperheater 3, a wet recovery device 4, a dehydrator 5 and a chimney 6 are connected in this order by flues 8b to 8e. Also, in this example, a wet recovery device 4, a dehydrator 5 and a circulation device 7 connected to a chimney 6 are installed.
  • the heating furnace 2 is a furnace in which contaminants are charged and thermally decomposed by heating the contaminants at a high temperature.
  • the type of heating furnace 2 is not particularly limited.
  • a surface melting furnace 2a and a secondary combustion furnace 2b are connected by a flue 8a. or an electric furnace such as an arc type or a plasma type, and the secondary combustion furnace 2b may be installed as required, and is not essential.
  • the type and configuration of the heating furnace 2 may be selected and designed according to the properties of the contaminants to be treated. If the contaminant contains a persistent compound, the temperature and reaction time required for decomposition of such compound should be ensured. For example, when the contaminant contains PFOS or PFOA, which are persistent organic fluorine compounds, the decomposition requires 850 degrees Celsius or more and a residence time of 2 seconds or more. Therefore, in this example, the surface melting furnace 2a is selected as a type that can sufficiently heat the persistent organic fluorine compound, and the secondary combustion furnace 2b is installed to ensure a sufficient residence time. .
  • V (V/Q) x 3600 Therefore, V should be determined so that ⁇ >2.
  • the secondary combustion furnace 2b may be configured by joining a plurality of shells so that they can be disassembled so that the volume of the secondary combustion furnace 2b can be changed according to the operating conditions of the pollutant treatment system 1.
  • the secondary combustion furnace 2b can be separated into a lower shell 2b-1, an intermediate shell 2b-2, and an upper shell 2b-3, and these can be flanged, for example, to form a secondary combustion furnace. 2b is assembled.
  • the volume of the secondary combustion furnace 2b can be changed by using or not using the intermediate shell 2b-2.
  • intermediate shells 2b-2 of different sizes (heights) or by stacking a plurality of intermediate shells 2b-2, the volume of the secondary combustion furnace 2b can be flexibly changed as required. be.
  • the molten slag generated in the surface melting furnace 2a is collected as cinders, detoxified as necessary, and reused as appropriate disposal or construction materials.
  • High-temperature exhaust discharged from the heating furnace 2 is introduced into the heat exchanger 3 through the flue 8b.
  • the desuperheater 3 is equipment that reduces the temperature of the exhaust to approximately 500 degrees Celsius.
  • the exhaust gas from the heating furnace 2 has a high temperature, reaching approximately 900 to 1600 degrees Celsius depending on the operating conditions.
  • the temperature reducer 3 adjusts the temperature of such high-temperature exhaust gas to a temperature that is easy to handle in downstream processes.
  • the temperature of the exhaust after the temperature reduction by the temperature reducer 3 is assumed to be 500 degrees Celsius or higher.
  • the exhaust gas contains hydrogen fluoride gas. Since a film is formed, corrosion by hydrogen fluoride is suppressed.
  • the type of the desuperheater 3 is also not particularly limited.
  • the desuperheater 3 is an air-cooled heat exchanger, which reduces the temperature of the exhaust gas through heat exchange between the gases by passing high-temperature exhaust gas through the inside of the perforated pipe and supplying outside air to the outside thereof. is.
  • the outside air heated by heat exchange is supplied as heated air to the heating furnace 2 and used for combustion assistance.
  • water-cooled heat exchangers i.e., those that use water instead of outside air as a cooling medium
  • cooling towers i.e., those that reduce the exhaust temperature by mixing cold outside air into the exhaust. etc.
  • the exhaust gas whose temperature has been reduced by the desuperheater 3 is introduced into the wet recovery device 4 through the flue 8c.
  • the wet recovery device 4 is a facility that brings high-temperature exhaust gas of 500 degrees Celsius or higher containing by-products into contact with liquid water to recover the by-products in the liquid water.
  • the by-products include dust, sulfur oxides, and hydrogen fluoride gas.
  • hydrogen fluoride easily dissolves in liquid water and becomes hydrofluoric acid, resulting in high-temperature exhaust gas. Almost all of the hydrogen fluoride in the exhaust gas is recovered in the liquid water by sufficiently contacting the liquid water with the exhaust gas without evaporating the liquid water exposed to the exhaust gas.
  • the wet recovery device 4 has a configuration for mixing a large amount of liquid water and exhaust gas. By contacting and mixing a large amount of liquid water with the exhaust gas, part of the water evaporated due to the high temperature of the exhaust gas is reintroduced into the liquid water. .
  • the exhaust gas passing through the flue 8c before being introduced into the wet recovery device 4 may contain hydrogen fluoride, the temperature of the exhaust gas is 500 degrees Celsius or higher. are almost never corroded and damaged.
  • the exhaust gas that has passed through the wet recovery device 4 is reduced in temperature as a result of contact with a large amount of liquid water, but this exhaust gas contains almost no hydrogen fluoride and corrodes downstream equipment such as the flue 8d. will not be damaged by
  • a specific configuration of the wet recovery device 4 in this embodiment will be described later. Also, in the wet recovery device 4, almost all of the by-products such as dust and sulfur oxides contained in the exhaust gas are recovered in the liquid water.
  • the exhaust gas from the surface melting furnace 2a used in the pollutant treatment system 1 according to the present embodiment contains almost no dust, but even a small amount of dust may be captured in the liquid water in the wet recovery device 4.
  • the exhaust from the wet recovery system 4 is virtually free of particulates because it is collected by the wet recovery system.
  • the exhaust that has passed through the wet recovery device 4 is introduced into the dehydrator 5 through the flue 8d.
  • This exhaust gas contains droplets of liquid water generated by the wet recovery device 4 and droplets of condensed water vapor, and the dehydrator 5 is a device that separates and removes the liquid water contained in such exhaust gas.
  • the configuration of the dehydrator 5 is not particularly limited, a cyclone separator is used in this example.
  • the exhaust air that has passed through the dehydrator 5 has been cleaned by removing by-products. Such exhaust is led to the chimney 6 through the flue 8e and released into the atmosphere.
  • liquid water containing hydrofluoric acid is generated from the wet recovery device 4 and recovered by the dehydrator 5, or steam accompanying cooling of the exhaust gas in the chimney 6.
  • the liquid water generated by the aggregation of is collected and introduced into the circulation device 7, subjected to appropriate treatment, sent to the wet recovery device 4, and used when recovering the by-products in the exhaust. recycled as liquid water.
  • the details of the treatment in the circulation device 7 will be described later.
  • the contaminant treatment system 1 can thermally decompose and treat contaminants while suppressing the release of dioxins into the environment.
  • the pollutant contains a persistent organic fluorine compound
  • thermally decompose the persistent organic fluorine compound recover almost all of the generated hydrogen fluoride, and release it into the environment. Because it can be suppressed, contaminants containing persistent organic fluorine compounds can be safely disposed of. Since the contaminant treatment system 1 is almost unaffected by metal corrosion caused by hydrogen fluoride caused by thermal decomposition of the persistent organic fluorine compounds, it has a long equipment life and is capable of producing persistent organic fluorine compounds at low cost. Disposal of contaminants containing
  • the contaminant contains a persistent organic fluorine compound
  • almost all of the hydrogen fluoride contained in the exhaust gas discharged from the heating furnace 2 and passing through the flue 8b is It is planned to be recovered in liquid water in
  • the contaminants charged into the heating furnace 2 contain a large amount of persistent organic fluorine compounds and thus generate a large amount of hydrogen fluoride gas
  • the concentration of hydrogen fluoride in the exhaust gas is extremely high, There is concern that the wet recovery device 4 may not be able to completely remove the particles.
  • the pollutant treatment system 1 can have an additional configuration that sufficiently removes the hydrogen fluoride gas to clean the exhaust gas even when the concentration of hydrogen fluoride contained in the exhaust gas is high.
  • additional configurations are described below.
  • a first additional configuration is a configuration in which an introduction portion 11 is provided for introducing a reactant that reacts with fluorine to generate a harmless substance.
  • a reactant that reacts with fluorine to generate a harmless substance.
  • the fluorine generated by the decomposition of the contaminants is to form harmless substances, for example stable fluorine compounds such as metal fluoride salts, which are fixed and safely removed as ash.
  • stable fluorine compounds such as metal fluoride salts
  • an introduction part 11 for introducing a reactant is provided in the combustion chamber of the surface combustion furnace 2a.
  • the reactant is mixed with the pollutants being burned in the surface combustion furnace 2a or the exhaust gas generated by the pollutants, and fixes the fluorine contained therein to produce harmless substances.
  • the reactant may be a metal compound or metal powder or small pieces.
  • a piece of iron can be used.
  • the metal compound is not limited to an inorganic compound, and may be an organic compound.
  • natural materials containing these substances such as shells and limestone, may be used as reactants.
  • the position of the introduction part 11 for introducing the reactant is not limited to the combustion chamber of the surface combustion furnace 2a shown in the above example. Besides this, or in addition to this, on the path between the surface combustion furnace 2a and the secondary combustion furnace 2b such as the flue 8a, the combustion chamber of the secondary combustion furnace 2b, the secondary combustion such as the flue 8b
  • the introduction part 11 may be provided at any or a plurality of positions on the route between the furnace 2b and the desuperheater 3 and on the route between the desuperheater 3 and the wet recovery device 4 such as the flue 8c. Further, a predetermined reactant may be mixed in advance with the contaminant to be introduced into the heating furnace 2 .
  • the arrangement and structure of the introduction part 11 may be appropriately determined according to the properties of the contaminants and reactants to be introduced, the equipment to be provided with the introduction part 11 and its position.
  • the introduction part 11 may mix the reactant powder into the heated air blown into the surface combustion furnace 2a or the secondary combustion furnace 2b, or the contaminants introduced into the surface combustion furnace 2a may be mixed in advance. It may be added and mixed, or it may contain both.
  • the structure of the introduction part 11 may be a powder sprayer or an auto hopper depending on the shape of the reactant.
  • the heating furnace 2 is charged with It is necessary to use an appropriate amount of reactant according to the persistent organic fluorine compound to be used.
  • the amount of reactant to be introduced should be determined in advance based on the properties of the contaminants and the results of the test run. For example, if the contaminants to be treated are known substances such as liquid detergents, and the type and concentration of persistent organic fluorine compounds such as PFOS/PFOA contained in the contaminants are known, The amount of reactant required per volume of contaminant to be treated can be readily determined. If the contaminant is a mixture of multiple substances or the nature of the contaminant is not necessarily clear, a small amount of the contaminant is treated experimentally using the contaminant treatment system 1, and By analyzing the concentration of hydrogen fluoride contained in the , it is possible to estimate the amount of hydrogen fluoride generated in the treatment of the contaminants and thus determine the amount of reactant required.
  • the amount of contaminants used is small so that the amount of hydrogen fluoride generated can be sufficiently recovered by the wet recovery device 4, and the exhaust before being introduced into the wet recovery device 4 may be sampled from, for example, the flue 8c for analysis.
  • the amount of reactant to be introduced may be adjusted at predetermined intervals. For example, a portion of the exhaust before being introduced into the wet recovery device 4 may be sampled and analyzed every day, every week, etc., and the amount of reactant may be adjusted. Alternatively, the amount of reactant may be similarly adjusted each time the weight or volume of contaminants introduced into the contaminant treatment system 1 reaches a predetermined amount. For example, if weight is used, it should be every 1 t, and if volume is used, it should be every 1 m 3 .
  • the amount of reactant to be introduced should have a predetermined safety margin so that the concentration of hydrogen fluoride in the exhaust gas can be sufficiently reduced even in the event of an unintended event such as a sudden change in the properties of pollutants. It is good to consider and set a little more.
  • the concentration of hydrogen fluoride contained in the exhaust may be determined not by sampling and analyzing the exhaust directly, but by an indirect method.
  • the concentration of hydrogen fluoride in the exhaust gas may be estimated by measuring the concentration of hydrofluoric acid in the water to be treated recirculated from the wet recovery device 4 to the circulation device 7 .
  • a sensor that detects the concentration of hydrogen fluoride contained in the exhaust gas can be used at any position on the exhaust path of the pollutant treatment system 1, preferably before the wet recovery device 4 (e.g. Any position of the flue 8c) is provided, and the amount of the reactant introduced from the introduction part 11 is also adjusted in real time according to the concentration of hydrogen fluoride in the exhaust gas detected in real time. can be If the amount of reactant to be introduced is controlled in real time, the amount of excess reactant to be introduced can be reduced, which is economical.
  • the second additional configuration is a configuration in which an auxiliary recovery device 9 is provided for almost completely removing hydrogen fluoride in the exhaust that has not been recovered by the wet recovery device 4 .
  • the additional auxiliary recovery device 9 is installed after the wet recovery device 4 , preferably on the route between the wet recovery device 4 and the dehydrator 5 .
  • Fig. 3 is a schematic diagram showing a part of the pollutant treatment system 1 in which the auxiliary recovery device 9 is provided in the middle of the flue 8d.
  • the auxiliary recovery device 9 is a device for recovering hydrogen fluoride remaining in the exhaust gas by aerating the exhaust gas from the wet recovery device 4 into a large amount of water, and in the example shown in FIG. It is composed of an aeration tank 9b.
  • the blower 9a is connected to a flue 8d-1 that is connected to the wet recovery device 4 on the upstream side of the flue 8d, sucks the exhaust gas from the wet recovery device 4, and is placed in the aeration tank 9b. It is forcibly sent to the aerated aeration pump (aerator) 9c.
  • a sufficient amount of water is stored in the aeration tank 9b, and the aeration pump 9c is fixed in the water inside.
  • the blower 9a and the aeration pump 9c are connected by a flue 9d, and exhaust air from the wet recovery system 4 is sent to the aeration pump 9c.
  • the aeration pump 9c mixes the exhaust gas sent from the blower 9a with the water in the aeration tank 9b, and may be designed exclusively for the pollutant treatment system 1. You may use the commercial thing used for water quality improvement, such as.
  • the structure and operation of the one shown in FIG. 3 will be described as an example of the aeration pump 9c.
  • the aeration pump 9c includes a submersible motor 9e, an impeller 9f fixed to the shaft of the submersible motor 9e, and a case 9g that houses the impeller 9f.
  • the impeller 9f rotates, and functions as a centrifugal pump that sucks fluid around its rotation axis and discharges it in the centrifugal direction.
  • the case 9g opens to the flue 9d above the rotation axis of the impeller 9f and opens to the aeration tank 9b below the rotation axis. Furthermore, it is open to the aeration tank 9b over the entire periphery in the centrifugal direction of the impeller 9f.
  • the exhaust is sucked into the case 9g from above as indicated by a in FIG.
  • the water in 9b is sucked into the case 9g from below, mixed by the impeller 9f, and discharged from the side of the case 9g as water mixed with fine bubbles, as indicated by c in the figure.
  • the exhaust gas is sufficiently mixed with the water in the aeration tank 9b, and hydrogen fluoride remaining in the exhaust gas is dissolved in the water in the aeration tank 9b and recovered.
  • the structure of the aeration pump 9c shown here is just an example, and an aeration pump with another structure may be used. Further, if the aeration pump 9c itself has sufficient suction performance for exhaust, the blower 9a may be omitted.
  • the exhaust gas from which hydrogen fluoride has been sufficiently removed is sent from the upper part of the aeration tank 9b to the dehydrator 5 through the flue 8d-2 connected to the dehydrator 5 on the downstream side of the flue 8d. be done.
  • the concentration of hydrogen fluoride in the water in the aeration tank 9b gradually increases. Therefore, a certain amount of water in the aeration tank 9b is periodically or continuously sent to the circulation device 7 as the water to be treated, and the reduced amount of clean water is replenished from the circulation device 7.
  • the amount of water in the aeration tank 9b is kept constant, and the concentration of hydrogen fluoride in the water in the aeration tank 9b is kept below a certain value.
  • the temperature of the exhaust gas that has passed through the wet recovery device 4 is reduced. If this exhaust gas contains hydrogen fluoride that could not be recovered by the wet recovery device 4, it is considered that the exhaust gas is corrosive to metals for the reason described above. Therefore, in the configuration using the auxiliary hydrogen fluoride recovery device 9, the flue 8d-1, the blower 9a, the flue 9d and the case 9g are exposed to a corrosive environment.
  • the concentration of hydrogen fluoride in the exhaust gas passing through such members is considerably reduced by passing through the wet recovery device 4. .
  • the rate of progress of corrosion is by no means rapid because it is not in the range of 200 degrees Celsius to 500 degrees Celsius where metal corrosion by hydrogen fluoride progresses most. do not have. Therefore, the period until these members deteriorate is long, and the replacement frequency thereof can be kept low. Therefore, when the pollutant contains a persistent organic fluorine compound and the auxiliary recovery device 9 is used, it is desirable to select operating conditions such that the temperature of the exhaust gas that has passed through the wet recovery device 4 is 200 degrees Celsius or less. .
  • a corrosion-preventive lining for example, to form a fluororesin film on the inner surfaces of these members that come into contact with the exhaust. This is because if the temperature of the exhaust gas passing through these members is lowered to 200 degrees Celsius or less, the anti-corrosion coating will not be thermally damaged.
  • PTFE polytetrafluoroethylene
  • the auxiliary recovery device 9 not only removes hydrogen fluoride gas that may remain in the exhaust gas, but also removes other by-products that could not be completely removed by the wet recovery device 4 in the aeration tank 9b. Since it is thought to capture and recover in the water inside, it is also effective for contaminants that do not necessarily contain persistent organic fluorine compounds.
  • the pollutant treatment system 1 appropriately monitors the properties of the exhaust gas during the treatment process in order to stably treat the pollutants, and provides feedback to the process conditions. may be performed.
  • the position of monitoring the properties of the exhaust gas and the parameters to be monitored may be appropriate, but for example, the monitoring of the temperature will be explained.
  • various parameters such as sulfur oxide concentration, chloride ion concentration, dioxin concentration, amount of dust contained, etc. are measured, and the operating conditions of the pollutant treatment system 1 are changed according to the results. you can
  • a temperature sensor 10a is provided in the flue 8b and a temperature sensor 10b is provided in the flue 8c to measure the temperature of the exhaust before and after passing through the desuperheater 3.
  • the sensors 10a and 10b are not necessarily composed of a single device, and may be considered as an assembly of a plurality of detection devices. Further, in addition to the sensors shown in FIG.
  • the sensors 10a and 10b monitor the temperature of the exhaust before and after passing through the desuperheater 3. As a result, the operating conditions of the desuperheater 3 are adjusted so that the temperature of the exhaust gas passing through the flue 8c and introduced into the wet recovery device 4 does not drop below 500 degrees Celsius, and overheating is prevented. control to prevent
  • the temperature of the exhaust gas passing through the flue 8b and flowing into the desuperheater 3 may be used to adjust the desuperheating capacity of the desuperheater 3 and the operating conditions of the heating furnace 2.
  • the adjustment of the cooling capacity of the desuperheater 3 can be performed by increasing or decreasing the supply amount of the desuperheating medium such as outside air or water when the desuperheater 3 is a heat exchanger, or by adjusting the desuperheater 3 as a desuperheater. In some cases, it can be done by increasing or decreasing the amount of outside air to be introduced.
  • the desuperheating medium such as outside air or water when the desuperheater 3 is a heat exchanger
  • FIG. 4 is an external side view of the wet recovery device 4 used in this example.
  • the wet recovery device 4 includes a case 13 and an electric motor 14 installed on a pedestal 12 .
  • the case 13 has a hollow flat columnar shape with a central axis facing in the horizontal direction, and has a flue 8c for introducing the exhaust from the desuperheater 3 and the exhaust from the wet recovery device 4 to the dehydrator 5.
  • a flue 8d is connected. Therefore, the exhaust gas that has passed through the flue 8c is introduced into the case 13 of the wet recovery device 4 and then discharged from the flue 8d.
  • a shaft 15 is rotatably supported on the central axis of the case 13 through the case 13 .
  • the shaft 15 is connected to an electric motor 14 by a belt 16, and by rotating the electric motor 14, power is applied to the shaft 15 to rotate it.
  • the use of the electric motor 14 and the belt 16 is an example of a mechanism for applying rotational power to the shaft 15, and does not mean that the mechanism of the wet recovery device 4 is limited to this mechanism.
  • the power transmission mechanism between the electric motor 14 and the shaft 15 may be a mechanism other than the belt 16, and the output shaft of the electric motor 14 and the shaft 15 may be directly connected.
  • the power source of the rotational power need not be the electric motor 14, and any power may be used.
  • a water injection pipe 17 is attached to the upper part of the case 13 so that liquid water from the circulation device 8 is injected into the case 13 .
  • a drain pipe 18 is attached to the lower portion of the flue 8 d to discharge the liquid water flowing out of the case 13 and into the flue 8 d and circulate it to the circulation device 7 .
  • the specific attachment position of the drain pipe 18 does not necessarily have to be part of the flue 8 d , and it may be attached directly to the lower portion of the case 13 .
  • flues 8c and 8d are designed to be air-tight and liquid-tight, and consideration is given to prevent leakage of exhaust air and liquid water to the outside.
  • FIG. 5 is a diagram showing the internal structure of the wet recovery device 4, showing the inside of the case 13.
  • FIG. A rotating disk 19 fixed to a shaft 15 is accommodated inside the case 13 , and the rotating disk 19 rotates as the shaft 15 rotates. It is desirable that a plurality of rotary discs 19 be provided at appropriate intervals in the axial direction of the shaft 15 . Note that the rotation direction of the rotating disk 19 is counterclockwise in FIG. 5 in this example.
  • a large number of plate-shaped blades 20 are erected on the surface of the rotating disk 19 .
  • the blades 20 are preferably fixed along the radial direction of the rotating disc 19 so that when the rotating disc 19 rotates, a large amount of shear is applied to the fluid inside the case 13 .
  • the rotating disk 19 and the blades 20 are for stirring the liquid water inside the case 13 and the exhaust gas, and bringing the exhaust gas into sufficient contact with the liquid water.
  • the shape of the blades 20 and the mounting angle with respect to the rotary disk 19 may be changed as appropriate.
  • a large number of through holes 21 are provided in the rotary disk 19 as required.
  • the through-holes 21 are provided to reduce the weight of the rotating disk 19, reduce the fluid pressure difference between both surfaces of the rotating disk 19, and obtain a uniform stirring state of the liquid water and the exhaust gas inside the case 13. It is.
  • the material of the wet recovery device 4 is not particularly limited, but it is desirable to use a metal material with excellent corrosion resistance, heat resistance, weather resistance and mechanical properties, and stainless steel is used in this example.
  • the exhaust gas introduced into the wet recovery unit 4 has a high temperature of 500 degrees Celsius or more. 19 is rarely attacked by corrosion.
  • the high-temperature exhaust gas introduced into the case 13 is stirred and brought into contact with the liquid water to be cooled down to 200 degrees Celsius or lower, in this example, 100 degrees Celsius or lower. Since it is wholly or largely removed, it also exhibits little or no corrosiveness to metals.
  • the liquid water containing hydrogen fluoride and containing hydrofluoric acid naturally exhibits corrosiveness to metals, but the hydrofluoric acid is removed during the process of circulation through the circulation device 7. , the concentration of which is kept low enough that corrosiveness to metals is not a problem.
  • the exhaust gas introduced into the wet recovery device 4 at a high temperature of 500 degrees Celsius or less is rapidly reduced in temperature by contact with the liquid water in the wet recovery device 4, and is reduced to 300 degrees Celsius or less, or 100 degrees Celsius or less in this example. Therefore, even if the exhaust gas contains chlorine gas, almost no dioxins are generated by de novo synthesis.
  • high-temperature exhaust gas is introduced into the liquid water from the side of the device, and by-products are removed from the side of the device as well.
  • the discharged exhaust is discharged outside the device. That is, the flue 8c through which the high-temperature exhaust passes and the flue 8d through which the exhaust after removal of the by-product passes are connected to the side of the apparatus.
  • the "side surface of the apparatus” means excluding the upper and lower surfaces of the wet recovery apparatus 4. That is, in general understanding, the flues 8c and 8d are connected to the side of the wet recovery device 4 rather than above or below, so that the exhaust gas is introduced from the side and discharged from the side. With such a configuration, the height of the entire wet recovery device 4 in the installed state can be kept low and the size can be reduced, so that the wet recovery device 4 can be easily transported, installed, and dismantled.
  • the wet recovery device 4 since the height of the wet recovery device 4 itself is low, the wet recovery device 4 can be mounted on a transportation vehicle without being disassembled. It is only necessary to connect the flues 8c and 8d, the water injection pipe 17, the drain pipe 18, and the like. .
  • the "side surface of the device” here should be a position where the height of the wet recovery device 4 when installed does not increase significantly due to the connection of the flues 8c and 8d. If the shape of the wet recovery device 4 makes it difficult to distinguish between the upper surface, the lower surface, and the side surface, as shown in FIG. If the exhaust outlets 23 for the removed exhaust are non-overlapping, the flues 8c, 8d are connected to the side of the device and the hot exhaust is introduced from the side of the device to remove the hydrogen fluoride. It can be said that the exhaust gas is discharged from the side of the device. Also, the vertical center line C is conceptualized as a vertical line passing through the power center of the wet recovery device 4 and the geometric center of the reaction chamber, here the space inside the case 13 .
  • the specific configuration of the wet recovery device 4 shown in this example is an example.
  • the structure is not necessarily limited to that shown in FIGS. 4 and 5 as long as the structure can mechanically agitate high-temperature exhaust gas and liquid water.
  • a structure that does not necessarily involve mechanical stirring may be used as the wet recovery device 4 as long as it is a mechanism that allows the high-temperature exhaust gas and liquid water to sufficiently contact each other.
  • the liquid water recovered from the drain pipe 18 of the wet recovery device 4 and the liquid recovered from the exhaust gas by the dehydrator 5 contain hydrofluoric acid and sulfur oxides contained in the exhaust gas from the heating furnace 2.
  • Environmental pollutants such as dust and soot caused by combustion can be included.
  • This liquid water may be treated as it is as a waste liquid and disposed of, and clean water may be constantly supplied from the water injection pipe 17 of the wet recovery device 4, but in that case, a large amount of water to be treated is generated, and a large amount of clean water is also required.
  • the collected liquid water is returned to the circulation device 7 to be cleaned, and supplied to the wet recovery device 4 for circulating use. It reduces the amount of water required.
  • Liquid water is also refluxed in the circulation device 7, in addition to the liquid water recovered from the wet recovery device 4 and the liquid water recovered from the dehydrator 5, as the water to be treated.
  • the temperature of the water vapor contained in the exhaust gas is reduced and condenses into liquid water. Since the exhaust air discharged from the chimney 6 is sufficiently purified, the liquid water generated in the chimney 6 is basically clean water, so it is considered that there is no problem in discharging this as it is. In this example, from the viewpoint of reducing the amount of water used in the pollutant treatment system 1 as a whole, it is collected and recycled.
  • FIG. 6 is a schematic diagram showing an example of the internal configuration of the circulation device 7.
  • the circulation device 7 includes a first receiving tank 24, a reactor 25, a second receiving tank 26, a separator 27, a suspended solid recovery tank 28, and a water storage tank 29. After entering the first water receiving tank 24 as shown in , it is returned to the wet recovery apparatus 4 as clean water through the reactor 25, the second water receiving tank 26, the separator 27 and the water tank 29.
  • the first receiving tank 24 is a tank that temporarily stores water to be treated that is returned from the wet recovery device 4, the dehydrator 5, the chimney 6, and the auxiliary hydrogen fluoride recovery device 9 if provided. When the amount of water to be treated in the first water receiving tank 24 reaches a certain level or more, the water to be treated is transferred to the reactor 25 using an appropriate pump or the like.
  • the reactor 25 is a device that uses a chemical reaction to remove fluorine and other chemical substances contained in the water to be treated.
  • the specific structure and mechanism of the reactor 25 may be arbitrary. or mechanically agitated to fix fluorine in the granular treatment agent, or an ion exchange resin or an ion exchange membrane to remove fluorine from the water to be treated. Further, these granular processing agents, ion exchange resins, or ion exchange membranes may simultaneously remove chemical substances other than fluorine contained in the water to be treated, such as sulfate ions and nitrate ions.
  • the reactor 25 or the processing agent in the reactor 25 should be replaced because removing more than a certain amount of fluorine and other chemical substances reduces the removal performance. Replacement may be performed when the amount of water to be treated reaches a certain amount, or the concentration of chemical substances such as hydrogen fluoride contained in the liquid water flowing out of the reactor 25 may be monitored. It may be performed when the concentration exceeds a threshold.
  • the liquid water that has passed through the reactor 25 is transferred to the second water receiving tank 26 using an appropriate pump or the like.
  • the second water receiving tank 26 is a water tank for temporarily storing water requiring treatment from which chemical substances such as fluorine have been removed. to transfer the water to be treated to the separator 27 .
  • the separator 27 is a cyclone in this example, and centrifuges and removes suspended solids (SS) in the water to be treated.
  • the separated suspended solids are collected in the suspended solids collection tank 28 and appropriately disposed of.
  • the water that has passed through the separator 27 is clean water from which dissolved chemical substances and suspended substances have been removed, and is stored in the water tank 29 .
  • the specific configuration of the separator 27 does not necessarily have to be a cyclone.
  • it may be a filter using a filter medium such as non-woven fabric or coconut husk mat, or a combination thereof.
  • the water tank 29 is a tank that stores clean water to be sent to the wet recovery device 4 or the auxiliary hydrogen fluoride recovery device 9 if provided.
  • the clean water at a flow rate required by the wet recovery device 4 and the auxiliary hydrogen fluoride recovery device 9 is sent from the water storage tank 29 by an appropriate pump or the like and circulated. Further, water lost due to evaporation or the like during operation of the pollutant treatment system 1 is replenished by replenishing the water tank 29 with raw water, and the amount of water in the water tank 29 is kept constant.
  • a pH adjuster may be added to the clean water in the water tank 29 to control the pH of the clean water to a predetermined value.
  • the use of the pH adjuster can be reduced by using the water as it is without neutralization.
  • the circulation device 7 is a single device integrally including the first water receiving tank 24, the reactor 25, the second water receiving tank 26, the separator 27, the suspended solid recovery tank 28, and the water storage tank 29 described above. may be configured, or may be configured as an assembly of separate devices. Also, filters and additional reactors may be added as needed.
  • the exhaust finally discharged into the atmosphere from the chimney 6 is sufficiently cleaned, and air pollutants such as hydrogen fluoride and sulfur oxides are sufficiently removed. Since it is removed, a large chimney 6 is not necessarily required, and its height, for example, 6 m or less, may be sufficient. A chimney 6 with a height of about 10 m or more may be used depending on the nature of the pollutant to be treated, such as when it contains a large amount of sulfur.
  • the chimney 6 can be loaded on a transportation vehicle without being disassembled during transportation, and a large lifting machine is not required for installation and dismantling of the chimney 6.
  • the height of the wet recovery device 4 used in the pollutant treatment system 1 according to the present embodiment is also kept low, so that it can be loaded on a transportation vehicle without being disassembled, and its installation and installation. Dismantling is also easy.
  • the heating furnace 2 although it depends on its type, the surface melting furnace shown in this example is known to be relatively small, and it is also easy to transport, install and dismantle.
  • the other devices, the desuperheater 3, the dehydrator 5, and the circulation device 7 are also not large-scale devices, so transportation, installation and dismantling thereof are easy.
  • the pollutant treatment system 1 as a whole is easy to transport, install, and dismantle, and construction using a large crane may be unnecessary.
  • the pollutant treatment system 1 can be easily installed by transporting the pollutant treatment system 1 itself to the vicinity of the contaminated area. At the same time, it can be easily dismantled and relocated to another contaminated area after disposal is completed.
  • FIG. 7 is a flow diagram of a pollutant treatment method by the pollutant treatment system 1 according to this embodiment.
  • the contaminants are thermally decomposed by the heating furnace 2 in step S01.
  • a reactive agent that reacts with fluorine to generate a harmless substance may be added to the contaminant and/or its high-temperature exhaust (step S02 ).
  • the amount of this reactant to be added is determined in advance based on the properties of the contaminants and the results of trial operation, or is determined according to the concentration of hydrogen fluoride in the exhaust gas measured or estimated by an appropriate method.
  • the hot exhaust is cooled to a temperature not below 500 degrees Celsius in step S03. Thereafter, the hot exhaust gas of 500 degrees Celsius or higher is brought into contact with liquid water in step S04 to recover the by-products in the liquid water and The temperature is rapidly reduced to 100 degrees or less.
  • This process results in very little de novo synthesis of dioxins, even when the contaminants include chlorides, so the toxicity equivalent of dioxins in the cooled hot exhaust is 0.1 ng-TEQ/ m 3 or less.
  • the hot exhaust and liquid water may be mechanically agitated.
  • an additional step of aerating the exhaust gas into water may be performed to ensure recovery of the hydrogen fluoride in the exhaust gas.
  • step S05 The exhaust after removing the by-products is dehydrated and cleaned in step S05.
  • the clean exhaust is released to the atmosphere in subsequent step S06.
  • the water to be treated collected in steps S04 and S05 is cleaned in step S07 by removing fluorine and other chemical substances, suspended matter including dust, etc., and is used in step S04. It is circulated and supplied as liquid water.
  • the pH of the clean water may be adjusted so as to exhibit alkalinity.
  • FIG. 8 is a graph showing measured values of the exhaust gas temperature before and after the wet recovery device value 4 in the pollutant treatment system 1 .
  • the exhaust before wet collector value 4 is the exhaust through flue 8c
  • the exhaust after wet collector value 4 is the exhaust through flue 8d.
  • the vertical axis indicates the temperature of the exhaust gas [°C]
  • the horizontal axis indicates the elapsed time [hr]. 3 shows the change in temperature of the exhaust after .
  • FIG. 9 is a graph showing measured values of temperatures of liquid water circulated and supplied in the pollutant treatment system 1 according to the same example.
  • the vertical axis of the graph indicates the liquid water temperature [°C]
  • the horizontal axis indicates the elapsed time [hr]
  • the solid line 31a indicates the water temperature of the water to be treated recovered from the wet recovery device value 4 to the circulation device 7, and the broken line.
  • 31a indicates the water temperature of the clean water supplied from the circulation device 7 to the wet recovery device value 4;
  • FIG. 10 shows various types of exhaust gas contained in the exhaust before and after the wet recovery device 4 when the pollutant treatment system 1 was used to treat pollutants containing persistent organic fluorine compounds under various conditions on a trial basis.
  • the measured concentrations of by-products and the removal rate of each by-product from the exhaust are tabulated.
  • the test was conducted for eight cases of conditions 1 to 8 while changing the conditions such as the properties of contaminants and the amount of input. Also, in the table, the parts indicated by "-" are those for which no measured values were obtained.
  • the dioxin concentration contained in the exhaust gas after passing through the wet recovery device 4 and the dioxin concentration in the circulating water used in the wet recovery device 4 were measured, and the results are shown in FIG. Concerning the concentration of dioxins in the exhaust gas, only a very small amount of dioxins, which is barely detectable, was detected in both the measured concentration and the converted concentration. ng-TEQ/m 3 ], it can be evaluated that dioxins are substantially absent in the exhaust. That is, the pollutant treatment system 1 sufficiently suppresses the de novo synthesis of dioxins in the high-temperature exhaust.
  • both the measured concentration and the toxicity equivalent are on the order of picograms per cubic meter, which is extremely small and is considered to have virtually no impact on the environment. This also indicates that the de novo synthesis of dioxins in the high-temperature exhaust gas is sufficiently suppressed by the pollutant treatment system 1 .
  • the contaminant treatment system 1 and the contaminant treatment method by the contaminant treatment system 1 described above are shown as specific examples of the system and method for treating contaminants, and the specific shape, arrangement, and number of devices used. etc. may be changed as appropriate, and the present invention is not intended to be limited to such specific shapes, arrangements, and numbers.

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Abstract

L'invention concerne un système de traitement de polluants (1) comprenant : un four de chauffage (2) qui pyrolyse des polluants ; et un dispositif de récupération par voie humide (4) qui amène les effluents à haute température à 500°C ou plus évacués du four de chauffage (2) en contact avec de l'eau liquide pour récupérer, dans l'eau liquide, des sous-produits dans les effluents à haute température et qui refroidit les effluents à haute température jusqu'à 300°C ou moins.
PCT/JP2022/014537 2021-03-30 2022-03-25 Système de traitement de polluants et procédé de traitement de polluants WO2022210389A1 (fr)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS405999B1 (fr) * 1962-05-26 1965-03-25
JPS4960058A (fr) * 1972-10-13 1974-06-11
JPS5980693U (ja) * 1982-11-25 1984-05-31 三建産業株式会社 パネル式組立加熱炉
JPH0985048A (ja) * 1995-07-20 1997-03-31 Nisso Eng Kk 有機ハロゲン化合物の分解方法
JPH1094716A (ja) * 1996-09-24 1998-04-14 Hitachi Ltd フロン分解処理方法及びその処理装置
JPH10225618A (ja) * 1997-02-14 1998-08-25 Ueda Sekkai Seizo Kk 立型石灰焼成炉を用いた有機ハロゲン化合物の分解処理方法及び分解処理装置
JP2000354733A (ja) * 1999-06-15 2000-12-26 Sumitomo Seika Chem Co Ltd 排ガスの処理方法およびそれを用いた装置

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS405999B1 (fr) * 1962-05-26 1965-03-25
JPS4960058A (fr) * 1972-10-13 1974-06-11
JPS5980693U (ja) * 1982-11-25 1984-05-31 三建産業株式会社 パネル式組立加熱炉
JPH0985048A (ja) * 1995-07-20 1997-03-31 Nisso Eng Kk 有機ハロゲン化合物の分解方法
JPH1094716A (ja) * 1996-09-24 1998-04-14 Hitachi Ltd フロン分解処理方法及びその処理装置
JPH10225618A (ja) * 1997-02-14 1998-08-25 Ueda Sekkai Seizo Kk 立型石灰焼成炉を用いた有機ハロゲン化合物の分解処理方法及び分解処理装置
JP2000354733A (ja) * 1999-06-15 2000-12-26 Sumitomo Seika Chem Co Ltd 排ガスの処理方法およびそれを用いた装置

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