JP2006193482A - Method and apparatus for treating organohalogen compound - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for treating an organohalogen compound by which the treatment is smoothly carried out without risks of increase of a distillation cost and loss of metallic sodium, and without the risk of blocking of solution sending by an alkali metal salt formed by the reaction of an alkali metal with the organohalogen compound; and to provide an apparatus for treating the compound. <P>SOLUTION: The method for treating the organohalogen compound comprises a reaction step for mixing a liquid to be treated, formed by dissolving the organohalogen compound in a hydrocarbon solvent, with the alkali metal to react the organohalogen compound with the alkali metal and to decompose the organohalogen compound to afford a reacted and treated liquid, a hydration step for feeding the reacted and treated liquid to a hydration vessel without distillation and adding water to the reacted and treated liquid in the hydration vessel to extract the alkali metal halide formed by the reaction with the water, an oil-water separation step for separating and removing the water from the reacted and treated liquid having passed the hydration step in the oil-water separation vessel, and a distillation step for distilling the reacted and treated liquid having passed the oil-water separation step in a distillation vessel to recover the hydrocarbon solvent. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to a method for treating an organic halogen compound and an apparatus for treating the same, in which an alkali metal is added to an organic halogen compound in a hydrocarbon solvent, and the hydrocarbon solvent is recovered.

  Organohalogen compounds such as polychlorinated biphenyls (PCBs) and dioxins are known as environmental pollutants. In recent years, how to safely treat contaminants such as capacitors and transformers contaminated with these organohalogen compounds. How to do is a big problem. For example, PCBs used for insulating materials such as capacitors and transformers and heat media are very chemically stable and difficult to be decomposed. At present, their production and use are prohibited for environmental reasons. The processing method has become a problem with respect to what has been used in the past.

  Therefore, a hybrid method is adopted as a method for treating this type of organic halogen compound (see, for example, Patent Document 1). In the hybrid method, an organic halogen compound (for example, PCB) dissolved in a hydrocarbon solvent is decomposed, and then the hydrocarbon solvent is recovered for reuse.

FIG. 3 shows a schematic flow diagram for explaining a conventional method for treating an organic halogen compound.
That is, according to the conventional hybrid method, first, the PCB is extracted from the capacitor or the like (S201), and the liquid to be treated in which the hydrocarbon solvent is dissolved in the PCB is transferred to the reaction step (S202). Then, a reaction accelerator and an alkali metal are added to the liquid to be treated, and the PCB and the alkali metal are reacted to perform a dehalogenation process (S202). The dehalogenated reaction treatment liquid is separated into a distillate and a bottoms by distillation, and the hydrocarbon solvent is recovered for reuse as a PCB solvent (S203). Then, hydration is performed by supplying water to the reaction processing liquid discharged as the bottoms (S204), and oil-water separation is performed into a water phase and an oil phase by stationary separation (S205). The treated oil separated by oil-water separation is distilled (S206), water as an initial distillate is supplied to the hydration process, and the late distillate is recovered as a solvent for PCB (S207). The bottoms are discarded as waste oil.

JP 2003-226658 A

  However, according to the above-described hybrid method, for example, when metallic sodium is reacted with PCB, which is an organic halogen compound, when the dechlorinated reaction treatment liquid is distilled, the reaction accelerator and the hydrocarbon solvent are first introduced. Since it is separated and removed, a reaction treatment solution having a high sodium salt concentration remains in the distillation tank. Therefore, when the reaction treatment liquid having a high sodium salt concentration is discharged as the bottoms, the deposited salt (NaCl) is deposited on the pipe, and the PCB treatment is repeated, so that the deposited salt is transferred to the hydration process. This causes a problem of making it difficult to feed liquid. Therefore, in order to smoothly feed the liquid to the hydration process, the PCB concentration in the reaction processing liquid must be set low (within 10%) in the reaction process to prevent salt deposition and the liquid must be fed. I had to.

In addition, as another method for solving the problem of salt accumulated in such a pipe, it is conceivable to install a special slurry pump or increase the diameter of the pipe connecting the distillation tank and the hydration tank. This is not preferable because a large capital investment is required.
As another method, it is conceivable to supply water directly to the distillation tank to hydrate sodium. However, when water is supplied to the distillation tank, the inside of the tank is cooled, so that enormous energy costs are required to operate again, and there is a problem that the distillation cost increases. It is also conceivable to supply water to the reaction vessel. However, if water remains in the reaction vessel, the metal sodium added in the next cycle reacts with water to generate hydrogen to sodium hydroxide, resulting in a problem of wasting metal sodium.

  The present invention has been made in view of the above problems, and there is no possibility that distillation cost increases or metal sodium is wasted, and an alkali metal produced when an alkali metal is reacted with an organic halogen compound. It is an object of the present invention to provide a method for treating an organic halogen compound and a treatment apparatus thereof that can be smoothly carried out with almost no risk of liquid feeding being inhibited by salt.

  A liquid to be treated in which an organic halogen compound is dissolved in a hydrocarbon solvent and an alkali metal are mixed, the organic halogen compound and the alkali metal are reacted in a reaction vessel, and the organic halogen compound is decomposed to obtain a reaction treatment liquid. Water for supplying the reaction treatment liquid to the hydration tank without distilling, adding water to the reaction treatment liquid in the hydration tank, and extracting the alkali metal halide salt produced by the reaction into water. Summing step, oil-water separation step of separating and removing the water from the reaction treatment liquid that has undergone the hydration step in an oil-water separation tank, and distillation of the reaction treatment liquid that has undergone the oil-water separation step in the distillation tank, And a distillation method for recovering the system solvent. A method for treating an organic halogen compound is provided.

  According to the method for treating an organic halogen compound having the above structure, since the hydration step is performed before the distillation step, the alkali metal salt produced in the reaction step is concentrated during the distillation and is not deposited on the pipe. , Liquid feeding can be performed smoothly. Further, since hydration is performed in a hydration tank, there is no possibility that the distillation cost increases or metal sodium is wasted, as in the case where water is added to the reaction tank or distillation tank.

  Examples of the organic halogen compounds in the present invention include harmful organic halogens such as PCBs, dioxins, dibenzofurans having halogen, polychlorobenzene, methylene chloride, or bromides in which chlorine atoms contained therein are substituted with bromine atoms. A compound can be mentioned. Examples of the alkali metal include sodium, lithium, potassium, rubidium, etc. Among them, sodium is preferable from the viewpoint of reaction rate and ease of handling, and in particular, the alkali metal is dispersed in a dispersion medium such as trans oil. It is preferable to use it as an alkali metal dispersion. As the dispersion medium, trans-oil containing PCB and normal paraffin used as a cleaning solvent can be preferably used.

  In the present invention, the hydrocarbon solvent may be a paraffinic, naphthenic, isoparaffinic or the like having no —OH group or —O— group that reacts with an alkali metal. In addition, normal paraffin is preferable from the viewpoint of easily dissolving the organic halogen compound. In addition, when normal paraffin is used, the reactivity between the organic halogen compound and the alkali metal in the reaction step is improved, and when a conventional insulating oil is used, about 3 times the chemical equivalent required for the reaction is required. Further, the amount of alkali metal can be reduced to, for example, about 2.4 to 2.8 times. Furthermore, normal paraffins are less likely to be oxidized and are less likely to take up water in the hydration tank and can be reused, so that the amount of organic solvent used for cleaning contaminants can be reduced. The number of carbon atoms of normal paraffin is preferably 9 to 13, and if the carbon number is 9 or more, the normal paraffin does not boil during the reaction in the PCB treatment step usually performed at 130 ° C. or lower, and the reaction is safely performed. When the carbon number is 13 or less, the viscosity is lower than that of the electrical insulating oil, the handling is easy, and the dispersibility of the alkali metal during the reaction is also good.

  The reaction step includes a first reaction step in which the organic halogen compound and the alkali metal are reacted in a reaction vessel, the alkali metal added to adjust the alkali metal concentration to a predetermined concentration, and the liquid to be treated. It is preferable to provide the 2nd reaction process which makes a reaction processing liquid by adding. Thereby, when the dehalogenation reaction is performed by reacting the organic halogen compound and the alkali metal, the remaining amount of the remaining alkali metal can be reduced.

  In the hydration step, it is preferable to supply a part of the reaction treatment liquid in the reaction tank that has undergone the reaction step. As a result, the dehalogenation reaction can be repeated without increasing the capacity of the reaction vessel.

  The alkali metal is preferably an alkali metal dispersion having an average particle diameter of 7 μm or less. Thus, the dehalogenated compound can be suitably decomposed by repeating the dehalogenation reaction several times.

  In the present invention, the liquid to be treated in which an organic halogen compound is dissolved in a hydrocarbon solvent is mixed with an alkali metal, and the organic halogen compound and the alkali metal are reacted in a reaction vessel to decompose the organic halogen compound. The reaction means (1) as a reaction treatment liquid is supplied to the hydration tank (2a ′) without distilling the reaction treatment liquid from the reaction tank, and the reaction treatment liquid is supplied to the hydration tank (2a ′). Hydration means (2a) for adding water to extract the alkali metal halide salt produced by the reaction into water, and the water from the reaction treatment solution supplied from the hydration tank (2a ′) to the oil-water separation tank And an oil / water separation means (2b) for separating and removing, and a distillation means (2c) for distilling the reaction treatment liquid separated in the oil / water separation tank in the distillation tank and recovering the hydrocarbon solvent. Treatment equipment for organic halogen compounds To provide. According to the organic halogen compound processing apparatus having such a configuration, the processing method according to claim 1 can be suitably carried out.

  As described above, according to the present invention, there is no possibility that the distillation cost increases or metal sodium is wasted, and the liquid is fed by the alkali metal salt produced when the alkali metal is reacted with the organic halogen compound. There is an advantage that it can be carried out smoothly with almost no risk of obstruction.

  Hereinafter, as a preferred embodiment of the present invention, as an organic halogen contaminant, PCB contained in a contaminant such as a capacitor and a transformer, normal paraffin as a hydrocarbon solvent, and metallic sodium as an alkali metal are taken as examples. The processing method and the processing apparatus will be described with reference to the drawings.

  FIG. 1 is a schematic block diagram for explaining a PCB processing apparatus according to the present embodiment. As shown in FIG. 1, first, a capacitor or the like removes filled oil (PCB) and collects it in a high-concentration PCB tank, and disassembles the main body. And it wash | cleans with normal paraffin after dismantling, collect | recovers solvent oil after washing | cleaning in a low concentration PCB tank, and discards or reuses the dismantlement after washing | cleaning after drying.

  Subsequently, the PCB processing apparatus includes a reaction means 1 for reacting metallic sodium with PCB and normal paraffin to be treated in a reaction tank, and a reaction treatment liquid dechlorinated with metallic sodium via the reaction means 1. And a solvent recovery means 2 for recovering normal paraffin from the solvent. Each means will be specifically described below.

  The reaction means 1 includes a PCB-contaminated oil reservoir 1a for storing a high-concentration PCB extracted from a condenser, a transformer, etc., and a low-concentration PCB washed with normal paraffin after dismantling the condenser, the transformer, etc. Accelerator supply unit 1d for supplying a reaction accelerator to the contaminated oil reservoir 1a, and metal sodium as an alkali metal in the liquid to be treated supplied from the PCB contaminated oil reservoir 1a (here, sodium metal is dispersed in trans oil) And a sodium supply unit 1b for supplying the metallic sodium to the dechlorination unit 1c. ing. The reaction accelerator is for donating hydrogen to dechlorinated biphenyl to promote the decomposition of PCB and to prevent the polymerization of biphenyl. In this embodiment, isopropyl is used as the reaction accelerator. Alcohol is used. Note that water may be used instead of isopropyl alcohol.

  The solvent recovery means 2 includes a hydration part (hydration means) 2a for adding water to the reaction treatment liquid subjected to the dechlorination reaction in the reaction tank, and the reaction treatment liquid after passing through the hydration part 2a. An oil / water separation part (oil / water separation means) 2b for separation and separation, and a distillation part (distillation means) 2c for distilling the reaction processing solution that has passed through the oil / water separation part 2b are provided.

  The hydration unit 2a supplies water to the reaction treatment liquid supplied from the dechlorination unit 1c to perform hydration, and a hydration tank 2a ′ separate from the reaction tank and distillation tank, and the water The water supply part 2a '' which supplies water to the Japanese tank 2a 'is provided. In the hydration part 2a, by adding water to the reaction treatment liquid, sodium chloride and the like present in the reaction treatment liquid are dissolved in water, and unreacted sodium and alkoxide react with water to form sodium hydroxide. Dissolved in water. Then, the hydrated reaction treatment liquid is supplied to the oil / water separator 2b.

  The oil / water separation unit 2b is an oil / water solution that separates the reaction treatment liquid to which water has been added in the hydration unit 2a into a water phase containing sodium chloride and an oil phase containing biphenyl, normal paraffin, and the like by stationary separation. A separation tank is provided. And the solution by the side of the water phase containing sodium chloride etc. is discarded as waste water. In addition, in this embodiment, although the hydration part 2a and the oil-water separation part 2b may each be provided with a separate hydration tank and an oil-water separation tank, they may share the same tank.

  The distillation unit 2c includes a distillation tank that separates the oil phase side solution separated by the oil / water separation unit 2b into a distillate and a bottoms. Specifically, the inside of the distillation tank is heated and depressurized to distill the solution on the oil phase side, cool the distillate vapor to form a distillate, and collect the distillate. Yes. Here, normal paraffin is recovered from the upper part of the distillation tower (recovered solvent), and other oils such as biphenyl are extracted from the lower part of the distillation tower (recovered oil).

  Next, among the recovered solvent recovered in the distillation unit 2c, the isopropyl alcohol dissolved in the oil is distilled from the initial distillate, so that it is supplied to the accelerator supply unit 1d as a reaction accelerator, Since normal paraffin is distilled from the distillate, the distillate is supplied to the distillation regeneration unit 3 as a solvent oil for washing and dilution and reused.

  The distillation regeneration unit 3 supplies the normal paraffin recovered from the distillation unit 2c to the cleaning unit by using rectification or the like in order to use the distillate as cleaning oil, and the can is discharged to the PCB via the high-concentration PCB tank. It supplies to the contaminated oil storage part 1a. In the distillation regeneration section 3, the solvent oil of the dismantled product once washed is collected through a low-concentration PCB tank, and rectification or the like is performed in the same manner.

In the above embodiment, metal sodium that has not been used in the dechlorination reaction remains in the reaction treatment liquid in which the dechlorination reaction has been performed in the reaction tank. If it supplies to 2a 'and it hydrates, the metal sodium which remains will be consumed wastefully. Therefore, after the dechlorination reaction is performed in the reaction tank, metal sodium is added from the sodium supply unit 1b and the liquid to be treated is added from the PCB-contaminated oil storage unit 1a in order to adjust to a predetermined metal sodium concentration. Thus, the dechlorination reaction may be repeated. Further, a part of the reaction treatment liquid in the reaction tank after the dechlorination reaction has been repeatedly performed is supplied to the hydration tank 2a ′, and the reaction treatment liquid remaining in the reaction tank is again sodium as in the above. It is good also as a structure which adds metallic sodium from the supply part 1b and adds a to-be-processed liquid from the PCB contaminated oil storage part 1a.
In this way, once the dechlorination reaction has been performed, by adding metal sodium and the liquid to be treated again and performing the dechlorination reaction, normally, after the reaction step The metallic sodium remaining after the dechlorination reaction that was wasted in the hydration process can be effectively used. Furthermore, by removing a part of the reaction solution after the dechlorination reaction repeatedly performed in the reaction tank, the dechlorination reaction can be repeatedly performed without increasing the capacity of the reaction tank.

  In addition, as the number of times of performing the dechlorination reaction in the reaction vessel increases, the remaining metallic sodium can be effectively used without being wasted by the hydration step. The reaction product generated in the treatment liquid inhibits the dechlorination reaction, and PCB may remain in the liquid to be treated after the reaction. Therefore, the number of times of performing the dechlorination reaction is preferably 2 to 4 times, more preferably 3 to 4 times.

  Further, the sodium dispersion to be added preferably has an average particle size of 7 μm or less, more preferably 5 μm or less. By using a sodium dispersion having an average particle diameter of 7 μm or less, PCB can be suitably decomposed by repeating the dechlorination reaction several times (2 to 4 times). Moreover, when an average particle diameter is 5 micrometers or less, the quantity of the sodium dispersion to add can be reduced (2.4-2.8 times the chemical equivalent required for reaction). If the average particle diameter exceeds 7 μm, a large amount of sodium metal must be added when the dechlorination reaction is repeated (for example, 3 to 4 times the chemical equivalent required for the reaction), and the reaction Since the amount of metallic sodium remaining after the completion also increases, it is not preferable. The lower limit of the average particle size of the sodium dispersion to be added is preferably 1 μm or more. If the average particle size is less than 1 μm, it is difficult to handle and there is a risk of ignition, which is not preferable.

Here, the average particle diameter (d ₃₂ (mm)) of the sodium dispersion means an average volume diameter determined by the following equation. That is, the average volume diameter was obtained by photographing n (n = 1300) sodium particles with an optical microscope (fluorescence microscope) and analyzing the image with a fluorescence image analysis system (product name: Lumina Vision, manufactured by Mitani Corp.). Then, the particle diameter (projected area equivalent diameter; d _i ) of each particle is measured, and the particles overlapped at this time are also processed on the system, and the average value of the measured particle diameter (d _i ) is calculated. Was determined by

  Further, when normal paraffin is used as the cleaning oil, the specific gravity difference can be used when a part is extracted from the reaction treatment liquid in the reaction tank after the dechlorination reaction. Specifically, most of the reaction treatment liquid obtained as a supernatant liquid is normal paraffin, and unreacted sodium settles, so that only part of the supernatant liquid is removed to leave unreacted metallic sodium. Is possible.

  With respect to the organic halogen compound processing apparatus configured as described above, a processing method using a hybrid method will be described below with reference to the drawings. FIG. 2 is a schematic flowchart for explaining the organic halogen compound processing method according to this embodiment.

  First, PCB is extracted from a capacitor or the like (S101), and the liquid to be treated in which normal paraffin is dissolved in the PCB is transferred to the reaction step (S102).

  In the reaction step (S102), isopropyl alcohol is supplied as a reaction accelerator to the liquid to be treated. A metal sodium dispersion is supplied to the reaction layer in advance, and a PCB diluted with normal paraffin is supplied to the reaction layer, and the metal sodium dispersion and PCB are reacted to perform a dechlorination reaction. At this time, the supply amount of the metal sodium dispersion is about 2.4 to 2.8 times the chemical equivalent required for the reaction. As the dispersion medium for the metallic sodium dispersion, it is preferable to use the same kind of hydrocarbon solvent, but it is also possible to use an electrical insulating oil or the like. In the reaction treatment liquid dechlorinated by the reaction step (S102), hydrogen is supplied from isopropyl alcohol, the polymerization is suppressed, and biphenyl, sodium chloride, unreacted sodium, alkoxide, etc. are contained in normal paraffin. Will exist.

  Next, in the hydration step (S103), the dechlorinated reaction treatment liquid is supplied to the hydration tank without obtaining a distillation step that has been conventionally performed, and water is supplied. By this process, sodium chloride in normal paraffin is dissolved in water, alkoxide is extracted into water as isopropyl alcohol and sodium hydroxide, and residual sodium is extracted into water as sodium hydroxide, so that the alkali in the reaction solution is extracted. The metal salt is dissolved. A part of isopropyl alcohol is extracted into oil. And the reaction processing liquid in which the hydration process was performed transfers to an oil-water separation process (S104).

  In the oil-water separation step (S104), the aqueous phase (water, sodium chloride, sodium hydroxide, some isopropyl alcohol) and the oil phase (insulating oil, normal paraffin, biphenyl, some isopropyl alcohol) are obtained by static separation. The aqueous phase side solution is discharged out of the system as waste alkali, the oil phase side solution is extracted, and the process proceeds to the distillation step (S105).

  In the distillation step (S105), the solution on the oil phase side is heated and distilled, and due to the difference in boiling point, isopropyl alcohol for the initial distillate is supplied to the accelerator supply unit 1d, and the normal paraffin for the late distillate is supplied. It is supplied to the distillation regeneration unit 3 and reused for cleaning oil such as a condenser, diluted oil for PCB, and the like (S106). And the bottoms containing biphenyl etc. are discarded as waste oil.

  As described above, according to the method and apparatus for treating an organic halogen compound according to the present embodiment, the alkali metal is reacted with the liquid to be treated in which the organic halogen compound is dissolved in the hydrocarbon-based solvent in the reaction tank to remove the halogen. The dehalogenated reaction treatment solution is supplied to the hydration tank without adding water, and water is added to dissolve the halogenated alkali metal salt and unreacted alkali metal. The remaining reaction solution was distilled in a distillation tank to recover the hydrocarbon solvent. Therefore, since the hydration step is performed before the distillation step, the alkali metal salt generated in the reaction step is concentrated during the distillation and can be smoothly fed without being deposited on the pipe. Further, since hydration is performed in a hydration tank, there is no possibility that the distillation cost increases or metal sodium is wasted, as in the case where water is added to the reaction tank or distillation tank.

  In this embodiment, when the dehalogenation reaction is repeatedly performed in the reaction vessel, the sodium concentration may be adjusted every time the liquid to be treated is added, or at the first addition of the liquid to be treated. A large excess of sodium dispersion is added, and at the end of the dehalogenation reaction, the amount of sodium is adjusted to a concentration not more than 3.5 times the chemical equivalent required for the reaction, preferably 2.4 to 2.8 times. It may be.

  Moreover, it is preferable to perform reaction temperature in the reaction tank in this embodiment at 80-130 degreeC. If the reaction temperature is less than 80 ° C., a long time is required for the dechlorination reaction, and if it exceeds 130 ° C., a by-product (polymer) is easily generated during the dechlorination reaction, which is not preferable.

  Also, when reacting the organic halogen compound and sodium dispersion in the reaction vessel, if the concentration of the organic halogen compound is low, the organic halogen compound is first charged in the reaction vessel, and the sodium dispersion is added later. In the case where the concentration of the organic halogen compound is high, it is preferable to prepare the sodium dispersion in the reaction tank first and add the organic halogen compound later. If the concentration of the organic halogen compound is high, adding a sodium dispersion later may cause a rapid reaction between the dispersion and the organic halogen compound, causing the temperature in the reaction vessel to rise locally. By preparing the body, the concentration of the organic halogen compound is apparently reduced and can be suitably dispersed, and the production of reaction byproducts such as a polymer can be suppressed. Furthermore, since an organic halogen compound is added to a large excess of sodium dispersion, it is possible to dehalogenate the organic halogen compound in a short time. Here, the high concentration means an organic halogen compound concentration of 1% or more, preferably 10% or more.

It is a schematic block diagram for demonstrating the processing apparatus of the organic halogen compound of one Embodiment. It is a schematic flowchart for demonstrating the processing method of the organic halogen compound of the embodiment. It is a schematic flowchart for demonstrating the processing method of the conventional organic halogen compound.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 ... Reaction means 1a ... PCB contaminated oil storage part 1b ... Sodium supply part 1c ... Dechlorination part 1d ... Accelerator supply part 2 ... Solvent recovery means 2a ... Hydration part 2a '... Hydration tank 2a''... Water supply Part 2b ... Oil / water separation part 2c ... Distillation part 3 ... Distillation regeneration part

Claims (5)

A liquid to be treated in which an organic halogen compound is dissolved in a hydrocarbon solvent and an alkali metal are mixed, the organic halogen compound and the alkali metal are reacted in a reaction vessel, and the organic halogen compound is decomposed to obtain a reaction treatment liquid. A reaction process;
A hydration step of supplying the reaction treatment liquid to the hydration tank without distillation, adding water to the reaction treatment liquid in the hydration tank, and extracting the alkali metal halide generated by the reaction into water;
An oil-water separation step of separating and removing the water from the reaction treatment liquid that has undergone the hydration step in an oil-water separation tank;
A method for treating an organic halogen compound, comprising: a distillation treatment step of distilling the reaction treatment liquid that has undergone the oil-water separation step in a distillation tank and recovering the hydrocarbon solvent.   The reaction step includes a first reaction step in which the organic halogen compound and the alkali metal are reacted in a reaction vessel, the alkali metal added to adjust the alkali metal concentration to a predetermined concentration, and the liquid to be treated. And a second reaction step in which a reaction treatment liquid is added to the organic halogen compound, and the organic halogen compound treatment method according to claim 1.   3. The method for treating an organic halogen compound according to claim 2, wherein in the hydration step, a part of the reaction treatment liquid in the reaction tank that has undergone the reaction step is supplied.   The method for treating an organohalogen compound according to any one of claims 1 to 3, wherein the alkali metal is an alkali metal dispersion having an average particle diameter of 7 µm or less. A liquid to be treated in which an organic halogen compound is dissolved in a hydrocarbon solvent and an alkali metal are mixed, the organic halogen compound and the alkali metal are reacted in a reaction vessel, and the organic halogen compound is decomposed to obtain a reaction treatment liquid. Reaction means (1);
The reaction treatment liquid is supplied from the reaction tank to the hydration tank (2a ′) without being distilled, water is added to the reaction treatment liquid in the hydration tank (2a ′), and the alkali metal halide generated by the reaction. Hydration means (2a) for extracting the salt into water;
Oil-water separation means (2b) for separating and removing the water from the reaction treatment liquid supplied from the hydration tank (2a ′) in an oil-water separation tank;
An apparatus for treating an organic halogen compound, comprising: distillation means (2c) for distilling the reaction treatment liquid separated in the oil / water separation tank in a distillation tank and recovering the hydrocarbon solvent.

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