JPH1015352A - Recovery of organic material by decomposition and device therefor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To effectively decompose an organic material such as a waste plastic material or waste material and properly recover and reuse a hydrocarbon component contained in the organic material. SOLUTION: An organic material is gasified by thermally decomposing the organic material in a primary heating chamber 1 at a temperature at which a chlorine content can be gasified, and this gaseous material is supplied to a catalytic tank 7 with an alumina catalyst 10 to catalytically decompose the chlorine content so that this content is separated from a hydrocarbon component. Further, the hydrocarbon component is recovered by a second recovery part 9.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for decomposing and recovering organic materials for recovering useful components such as hydrocarbon oil by decomposing organic materials such as waste plastic materials or waste rubber materials. TECHNICAL FIELD The present invention relates to a method and an apparatus for decomposing and recovering an organic material composed of waste organic matter and the like.

[0002]

2. Description of the Related Art Conventionally, waste plastic materials and waste rubber materials are decomposed and recovered as hydrocarbon oil. However, in the case of waste plastic materials and waste rubber materials containing a chlorine component, it is difficult to disassemble them. The chlorine component generated damages the device,
Alternatively, the treatment of the above-mentioned waste material containing a chlorine component has hardly been performed due to a problem that a generally used zeolite-based catalyst is poisoned and deteriorated early.

In some cases, for example, Japanese Patent Application Laid-Open No. Sho 53-60
As shown in Japanese Patent Publication No. 974, a high-molecular plastic waste such as polyvinyl chloride is supplied into a retort,
Heat recovery at a temperature not exceeding 0 ° C. to recover hydrogen chloride gas generated by thermal decomposition, incinerate and dispose of the distillate organic matter comprising the plasticizer and its decomposition products, and carbonize the decomposition residue Attempts to recover activated carbon or the like made of chlorinated organic matter have been made effective.

[0004]

In the structure in which the plastic material containing a chlorine component is decomposed by heating to recover hydrogen chloride gas as described above, even if hydrogen chloride can be recovered, it is properly removed. There is a problem that it is difficult to perform chlorination and recover and reuse industrially useful plasticizers and low-boiling hydrocarbon components as effective components.

SUMMARY OF THE INVENTION The present invention has been made to solve the above problems, and in particular, effectively decomposes an organic material such as waste plastic material or waste rubber material containing a chlorine-based organic substance, and decomposes the organic material into this organic material. An object of the present invention is to provide a method and an apparatus for decomposing and recovering an organic material capable of appropriately recovering and reusing a contained hydrocarbon component.

[0006]

The invention according to claim 1 is
In the method for decomposing and recovering organic materials containing chlorine components to recover useful components, the organic materials are gasified by heating and pyrolyzing the organic materials to a temperature at which the chlorine components can be gasified. This gaseous substance is supplied to a catalyst tank having an alumina-based catalyst and catalytically decomposed so that a chlorine component is separated from a hydrocarbon component, and then the hydrocarbon component is recovered.

[0007] According to the above structure, the organic material is gasified by being heated to a temperature at which the chlorine component can be gasified, and the gaseous material is supplied to the catalyst tank having an alumina-based catalyst. Chlorinated hydrocarbons such as octyl chloride contained in the gaseous body are catalytically decomposed into a chlorine component and a hydrocarbon component such as octene, and at least this hydrocarbon component is recovered and reused. Will be.

According to a second aspect of the present invention, there is provided a method for decomposing and recovering a useful component by decomposing an organic material containing a chlorine component, wherein the organic material is brought to a first set temperature at which the chlorine component can be gasified. After gasification by heating and primary pyrolysis, the gaseous material is supplied to a catalyst tank having an alumina-based catalyst, and catalytically decomposed so that a chlorine component is separated from a hydrocarbon component. After recovering the hydrogen component and heating the remaining material after heating to a temperature higher than the first set temperature and gasifying it by secondary pyrolysis, the gaseous material is converted into a solid acid catalyst. By supplying the catalyst to the catalyst tank having the catalyst, the remaining hydrocarbon component is catalytically cracked to produce a low-boiling hydrocarbon component, and then the low-boiling hydrocarbon component is recovered.

According to the above configuration, the residual material after the primary pyrolysis by heating the organic material containing the chlorine component to the first set temperature is heated to a temperature higher than the first set temperature and becomes gaseous. When the gaseous material is supplied to a catalyst tank having a solid acid catalyst, the hydrocarbon component contained in the gaseous material is catalytically cracked and reformed into a low-boiling hydrocarbon component. The low boiling hydrocarbon components will be recovered and reused.

According to a third aspect of the present invention, in the method for decomposing and recovering an organic material according to the second aspect, the first set temperature is set at 3 degrees.
The temperature was set to 50 ° C. or less.

According to the above structure, the organic material containing the chlorine component is heated to a temperature at which the chlorine component can be gasified at a temperature of 350.degree. And gasified,
The residual material after the first thermal decomposition is heated to a temperature higher than the first set temperature and is thermally decomposed to be gasified.

According to a fourth aspect of the present invention, in the method for decomposing and recovering an organic material according to the second or third aspect, a zeolite-based catalyst is used as a solid acid catalyst for catalytically decomposing a hydrocarbon component of a residual material. .

[0013] According to the above configuration, the gaseous substance produced by the secondary pyrolysis of the residual material after the primary pyrolysis is:
The organic material in the gaseous material is effectively catalytically cracked and reformed into a low-boiling hydrocarbon component by being supplied to a catalyst tank filled with a zeolite-based catalyst having excellent cracking performance. Boiling hydrocarbon components will be recovered and reused.

According to a fifth aspect of the present invention, there is provided the first to fourth aspects.
The method for decomposing and recovering an organic material according to any one of
The chlorine component separated by supplying a gaseous substance to a catalyst tank having an alumina-based catalyst is recovered as hydrogen chloride.

According to the above construction, the gaseous substance generated by heating the organic material to a temperature at which the chlorine component can be gasified is supplied to the catalyst tank having the alumina-based catalyst and catalytically decomposed. Is recovered and reused.

The invention according to claim 6 is the invention according to claims 1 to 5 above.
The method for decomposing and recovering an organic material according to any one of
When a gaseous substance is supplied to a catalyst tank having an alumina-based catalyst to separate a chlorine component from a hydrocarbon component, the hydrocarbon component is suppressed from being decomposed and recovered as an aliphatic hydrocarbon oil. .

According to the above configuration, the gaseous substance generated by heating the organic material to a temperature at which the chlorine component can be gasified is supplied to the catalyst tank having the alumina-based catalyst, and is contained in the gaseous substance. When the chlorinated hydrocarbon contained is catalytically decomposed into a chlorine component and a hydrocarbon component, the hydrocarbon component is decomposed more than necessary and decomposed to low molecular weight, so that it can be used at room temperature such as butene and propane. The conversion to gaseous hydrocarbon components is suppressed, and it is recovered as an aliphatic hydrocarbon oil such as octene having high utility value as fuel.

According to a seventh aspect of the present invention, there is provided the above-described first to sixth aspects.
The method for decomposing and recovering an organic material according to any one of
A γ-alumina catalyst is used as an alumina catalyst for separating a chlorine component.

In the above structure, the γ-alumina-based catalyst which catalytically decomposes a gaseous substance produced by heating an organic material to a temperature at which a chlorine component can be gasified can be used under the influence of hydrogen chloride. Also, the γ-alumina-based catalyst has a catalytic cracking function which is maintained in a good state for a long period of time because it has a property that the separation performance of the chlorine component hardly deteriorates.

The invention according to claim 8 is the invention according to claims 1 to 6.
The method for decomposing and recovering an organic material according to any one of
An amorphous alumina-based catalyst is used as an alumina-based catalyst for separating a chlorine component.

According to the above construction, the gaseous substance generated by heating the organic material to a temperature at which the chlorine component can be gasified is supplied to the catalyst tank having an amorphous alumina-based catalyst, and After the chlorinated hydrocarbons contained in the solid are effectively separated into a chlorine component and a hydrocarbon component, at least the hydrocarbon component is recovered and reused.

According to a ninth aspect of the present invention, in the method for decomposing and recovering an organic material according to the eighth aspect, a chlorine component in the organic material is separated using an alumina catalyst having a specific surface area of 140 m ² / g or more. Is what you do.

According to the above construction, the hydrocarbon contained in the gaseous substance is produced by the amorphous alumina-based catalyst having a specific surface area of 140 m ² / g or more and having excellent performance of separating a chlorine component. Is effectively catalytically decomposed into a chlorine component and a hydrocarbon component.

According to a tenth aspect of the present invention, in the organic material decomposition and recovery apparatus for decomposing an organic material containing a chlorine component to recover a useful component, the organic material is heated to a temperature at which the chlorine component can be gasified. A heating chamber for pyrolysis, a catalyst tank having an alumina-based catalyst for separating a chlorine component in a gaseous substance derived from the heating chamber from a hydrocarbon component, and a recovery for recovering the hydrocarbon component from which the chlorine component has been separated And a part.

According to the above configuration, the organic material is gasified by being heated in the heating chamber to a temperature at which the chlorine component can be gasified, and the gaseous material is supplied to the catalyst tank having the alumina-based catalyst. As a result, the chlorinated hydrocarbon contained in the gaseous body is catalytically decomposed into a chlorine component and a hydrocarbon component, and the hydrocarbon component is recovered by the recovery unit and reused.

The invention according to claim 11 is an organic material decomposition and recovery apparatus for decomposing an organic material containing a chlorine component to recover a useful component, wherein the organic material is heated to a temperature at which the chlorine component can be gasified. A primary heating chamber for primary pyrolysis, a catalyst tank having an alumina-based catalyst that catalytically decomposes the chlorine component in the gaseous substance derived from the primary heating chamber to separate it from the hydrocarbon component, and a catalyst tank derived from the catalyst tank A recovery section for recovering the hydrocarbon components, and a secondary heating chamber for heating the residual material after the primary pyrolysis at a temperature higher than the heating temperature of the primary heating chamber and for secondary pyrolysis to gasify the material. And a catalyst tank having a solid acid catalyst that catalytically decomposes the hydrocarbon component in the gaseous substance discharged from the secondary heating chamber into a low-boiling hydrocarbon component; and a low-boiling carbon derived from the catalyst tank. Turn the hydrogen component Those having a recovery unit for.

[0027] According to the above configuration, the remaining material after the primary thermal decomposition by heating the organic material containing a chlorine component to the first set temperature in the primary heating chamber is performed in the secondary heating chamber. By heating to a temperature higher than the set temperature, the gas is gasified, and the gas is supplied to a catalyst tank having a solid acid catalyst, whereby the hydrocarbon component contained in the gas is contacted. It is decomposed and reformed into a low-boiling hydrocarbon component, and this low-boiling hydrocarbon component is recovered by the recovery unit and reused.

The twelfth aspect of the present invention is directed to the tenth aspect.
Or an amorphous alumina-based catalyst having a specific surface area of 140 m ² / g or more as a catalyst for separating a chlorine component in a gaseous substance derived from a heating chamber from a hydrocarbon component in the apparatus for decomposing and recovering an organic material according to 11. It uses a catalyst.

According to the above configuration, the specific surface area is 140 m ^2.
/ G of hydrocarbons contained in a gaseous substance produced by pyrolysis in a heating chamber with an amorphous alumina-based catalyst having an excellent chlorine component separation performance set to at least / g Is effectively catalytically decomposed into a chlorine component and a hydrocarbon component, and at least the hydrocarbon component is recovered in the recovery section.

The invention according to claim 13 is the invention according to claim 11.
13. The apparatus for cracking and recovering an organic material according to item 12, wherein a zeolite-based catalyst is used as a solid acid catalyst for catalytically cracking a hydrocarbon component in a gaseous substance derived from a secondary heating chamber.

According to the above configuration, the gaseous substance produced by the secondary pyrolysis of the residual material after the primary pyrolysis in the secondary heating chamber is used as a catalyst having a zeolite-based catalyst having excellent decomposition performance. By being supplied to the tank, the hydrocarbon component in the gaseous substance is effectively catalytically cracked and reformed into a low-boiling hydrocarbon component, and this hydrocarbon component is recovered in the recovery section and reused. Will be.

The invention according to claim 14 is the invention according to claims 10 to 1
3. The apparatus for decomposing and recovering an organic material according to any one of 3), further comprising a recovery unit that recovers a chlorine component separated by the alumina-based catalyst as hydrogen chloride.

According to the above configuration, the gaseous substance generated by heating the organic material in the heating chamber to a temperature at which the chlorine component can be gasified is supplied to the catalyst tank having the alumina-based catalyst. The chlorinated hydrocarbon contained in the gaseous body is catalytically decomposed into a hydrocarbon component and hydrogen chloride, and the hydrogen chloride and the hydrocarbon component are collected and reused in separate recovery sections. Will be done.

[0034]

FIG. 1 shows a first embodiment of an organic material decomposition apparatus according to the present invention. This decomposition apparatus includes a primary decomposition system 2 having a primary heating chamber 1 for heating an organic material to a first set temperature and gasifying it by primary thermal decomposition, and a residual after primary thermal decomposition in the primary heating chamber 1. A secondary decomposition system 4 having a secondary heating chamber 3 in which the material is further heated and gasified by secondary thermal decomposition.

The primary heating chamber 1 includes a hopper 5 into which a raw material made of an organic material such as a plastic material or a rubber material, which will be described later, is charged, and a phthalate plasticizer contained in the charged organic material. A heating means (not shown) for heating the chlorine component and gasifying it by primary pyrolysis, and the remaining material left without being gasified by the primary pyrolysis is supplied to the secondary heating chamber 3. And a conveying means 6 such as a screw conveyor for conveying.

The first set temperature of the heating means is as follows: dioctyl phthalate (DOP), dibutyl phthalate (DBP), dimethyl phthalate and phthalic acid contained in an organic material such as a vinyl chloride plastic material or a rubber chloride. A temperature at which the phthalate plasticizer such as diethyl or the like and the chlorine component in the organic material can be gasified, and which does not decompose other components, that is, 350 ° C.
Below, the temperature is preferably set to 300 ° C. or lower.

The primary cracking system 2 is filled with a first catalyst filled with a catalyst for reforming a gaseous substance discharged from the primary heating chamber 1.
A catalyst tank 7, a first recovery section 8 for recovering phthalic anhydride in the gaseous substance derived from the first contact catalyst vessel 7, an aliphatic hydrocarbon derived from the first recovery section 8, A second recovery unit 9 for recovering hydrogen chloride generated by separation of the chlorine component in the organic material and chlorinated aliphatic hydrocarbon which is a reaction product of the aliphatic hydrocarbon and hydrogen chloride. Are provided.

The first catalyst tank 7 is filled with an alumina-based catalyst 10. And this alumina-based catalyst 1
0 is maintained at a temperature of about 300 to 350 ° C., so that the plasticizer in the gaseous substance is catalytically decomposed into phthalic anhydride and aliphatic hydrocarbon components such as octene and butene. .

The first collecting section 8 has a size of 80 to 200.
The phthalic anhydride generated in the first catalyst tank 7 is collected in a state of being precipitated as needle-like crystals by cooling the introduced gaseous body maintained at a temperature of about ° C. At the same time, it is configured to lead other components to the second recovery unit 9.

The second recovery section 9 recovers, if necessary, hydrogen chloride produced by melting a chlorine component in the solution contained therein, and, above the second recovery section 9, octene or the like in the gaseous body above the hydrogen chloride. Liquefied aliphatic hydrocarbons to produce aliphatic hydrocarbon oil, recovering this as fuel oil or naphtha raw material, etc., and recovering aliphatic hydrocarbon gas such as butane as gaseous fuel. I have.

The secondary heating chamber 3 heats the residual material supplied from the primary heating chamber 1 at a second set temperature higher than the first set temperature, for example, at a temperature of about 500 ° C. to perform secondary pyrolysis. A heating means (not shown) for converting the residue into a gaseous state, and a discharge means 11 comprising a screw conveyor or the like for discharging the residue remaining without being gasified by the secondary pyrolysis in the secondary heating chamber 3 to the outside. have.

The second decomposition system 4 includes a second catalyst tank 12 filled with a catalyst for catalytically decomposing and reforming a gaseous substance discharged from the second heating chamber 3, and a second catalyst tank 12. Fractionation tower 13 for fractionating the reformed gaseous matter derived from tank 12
And a cooler 14 for cooling the gaseous material discharged from the fractionation tower 13, and a hydrocarbon oil or the like liquefied by cooling the hydrocarbon component in the gaseous material in the cooler 14. A third collection unit 15 for collection is provided.

The second catalyst tank 12 is filled with a solid acid catalyst such as an alumina catalyst or a zeolite catalyst which catalytically decomposes the hydrocarbon component in the gaseous substance to lower the molecular weight. The fractionating tower 13 separates the hydrocarbon component into a low-boiling component and a high-boiling component, and guides the low-boiling hydrocarbon component to the cooler 14 as a gaseous substance. A component, for example, a high-boiling hydrocarbon component such as a tar or a wax is returned to the secondary heating chamber 3.

The cooler 14 cools the gaseous substance discharged from the fractionating tower 13 to be in a gas-liquid mixed state, and then discharges the gaseous substance to the third recovery unit 15. I have. The third recovery unit 15 is configured to form a mixture of a hydrocarbon component in a gas-liquid mixture state derived from the cooler 14, that is, a gaseous body of a hydrocarbon component such as a hydrocarbon gas and a hydrocarbon component such as a hydrocarbon oil. Among the hydrocarbon components constituted by the liquid material, the liquid material of the hydrocarbon component is stored, and the gaseous material of the hydrocarbon component is led out to a gas holder or the like (not shown).

The organic material supplied into the hopper 5 in the primary heating chamber 1 may be the following general-purpose plastic or high-performance engineering plastic or rubber in addition to the above-mentioned chlorinated beer-based plastic. . Examples of the general-purpose plastic material include polyethylene, polypropylene, polystyrene, acrylonitrile butadiene styrene, polymethyl methacrylate, and polyvinyl alcohol.

The high-performance engineering plastics include polyamide, polyacetal, polycarbonate, polyphenylene ether, polybutylene terephthalate, polysulfone, polyether sulfone, polyphenylene sulfide, polyarylate, and the like.
Examples thereof include polyimide, polyamideimide, and polyetheretherketone.

The type of the rubber material used as the organic material is not particularly limited, and styrene butadiene rubber, high styrene rubber, butadiene rubber, isoprene rubber, ethylene propylene rubber, ethylene propylene diene rubber, acrylonitrile Butadiene rubber,
Synthetic rubber such as chloroprene rubber, butyl rubber or urethane rubber, and natural rubber can be used.

At least a part of various plastic materials and rubber materials constituting the organic material is mixed with a phthalate plasticizer such as DOP (dioctyl phthalate) or DBP (dibutyl phthalate). I have. The organic material, such as the plastic or rubber waste, is usually put into the hopper 5 of the primary heating chamber 1 in a state of being crushed to a predetermined size in advance.

A decomposition and recovery method for decomposing and recovering an organic material by the decomposition apparatus having the above structure will be described. First,
An organic material made of waste plastic material or the like pulverized to a predetermined size is put into the hopper 5 of the primary heating chamber 1, and is heated to the first set temperature while being transported by the transport means 6. By thermal decomposition, the plasticizer and the chlorine component in the organic material are gasified. The gaseous material generated in the primary heating chamber 1 rises as an air current containing a mist component, and is introduced into a first catalyst tank 7 installed above the primary heating chamber 1.

The gaseous substance introduced into the first catalyst tank 7 is brought into contact with the alumina-based catalyst 10 filled therein, whereby the phthalate ester plasticizer contained in the gaseous substance is contained. Decomposes the agent to produce the following components:
Also, part of the chlorine component separated from the organic material,
Combines with hydrogen to form hydrogen chloride.

The plasticizer composed of dioctyl phthalate (DOP) is mixed with phthalic anhydride and
It is catalytically decomposed into an octene or other aliphatic hydrocarbon, and a part of it is reacted with the chlorine component to form a chlorinated aliphatic hydrocarbon such as octyl chloride. The plasticizer composed of dibutyl phthalate (DBP) is catalytically decomposed into phthalic anhydride and an aliphatic hydrocarbon composed of butene or the like in the first catalyst tank 7, and a part of the plasticizer reacts with chlorine. To a chlorinated aliphatic hydrocarbon such as butyl chloride.

Then, the reformed gaseous substance discharged from the first catalyst tank 7 is supplied to the first recovery section 8 and cooled, so that the gaseous substance is recovered in the first recovery section 8. After recovering the phthalic anhydride component in the needle-like crystallization,
The remaining components are led out to the second recovery section 9 where the hydrogen chloride, the aliphatic hydrocarbon oil, the aliphatic hydrocarbon gas, and the aliphatic hydrocarbon Separated from chlorinated product and recovered.

Further, the residual material left without being gasified in the primary heating chamber 1 is supplied to the secondary heating chamber 3 and is supplied to the second heating chamber 3 at a temperature higher than the first set temperature. 2. Gasification is performed by heating to a set temperature and secondary pyrolysis. Next, the gaseous substance discharged from the secondary heating chamber 3 is supplied to the second catalyst tank 12 and brought into contact with a solid acid catalyst having at least one of an alumina catalyst or a zeolite catalyst filled therein. By doing so, after reducing the hydrocarbon component of the remaining material to low molecular weight,
The fraction is supplied to the fractionating tower 13, the cooler 14 and the third recovery unit 15 sequentially.

Then, after the hydrocarbon component reduced in molecular weight in the second catalyst tank 12 is fractionally distilled in the fractionating unit 13 and the like, the evaporated component is supplied to a cooler 14 to be cooled, whereby the low-boiling carbon After generating the hydrogen oil, the low-boiling hydrocarbon oil is recovered in the third recovery section 15.
The high-boiling hydrocarbon component fractionated in the fractionation tower 13 is returned to the secondary heating chamber 3 and is recovered again after being heated and catalytically decomposed to lower the boiling point.

FIG. 2 shows a conversion reaction system 3 for converting chlorinated aliphatic hydrocarbons recovered in the second recovery section 9 of the primary cracking system 2 into aliphatic hydrocarbons and recovering them.
In the conversion reaction system 30, an aliphatic hydrocarbon component derived from an aliphatic hydrocarbon oil and a chlorinated aliphatic hydrocarbon derived from the upper part of the second recovery section 9 is shown. A storage portion 31 for storing the liquid material, a conversion heating chamber 32 for heating the liquid material derived from the storage portion 31 to be gasified, and a gaseous substance in the gaseous material derived from the conversion heating chamber 32. Dechlorination catalyst 33 for separating chlorine components
And a fractionation tower 35 for fractionating a gaseous substance derived from the dechlorination medium tank 34,
A cooler 36 for cooling the gaseous material discharged from the fractionation tower 35 and a final recovery unit 37 for recovering the liquid material cooled in the cooler 36 are provided.

The dechlorination catalyst 33 filled in the dechlorination catalyst tank 34 is formed by decomposing an aliphatic hydrocarbon component such as octene or the like into a gaseous state at room temperature, such as butene or propane, by decomposing more than necessary. Suppresses conversion to hydrogen components,
Also, it is made of an alumina-based catalyst having a property of hardly deteriorating even when affected by a chlorine component.

According to the above configuration, the liquid of the aliphatic hydrocarbon component comprising the aliphatic hydrocarbon oil such as octene and the chlorinated aliphatic hydrocarbon such as octyl chloride is heated in the conversion heating chamber 32 by about 300 ° C. After heating at a temperature of at least C to form a gas, the gaseous material is supplied to a dechlorination catalyst tank and heated at a temperature of about 300 ° C. or more while dechlorination comprising an alumina-based catalyst or the like. By contacting the catalyst with the conversion catalyst 33, the chlorine component is separated from the chlorinated product of the aliphatic hydrocarbon and converted into the aliphatic hydrocarbon.

The gaseous substance discharged from the dechlorination catalyst tank 34 is separated into a gaseous component of an aliphatic hydrocarbon and a chlorinated product thereof in a fractionation tower 35, and the gaseous component of the aliphatic hydrocarbon is separated. The gaseous component is liquefied by being cooled to 120 ° C. or lower in the cooler 36 and is recovered as a low-boiling-point aliphatic hydrocarbon oil in the final recovery section 37. After being returned to the conversion heating chamber 32 and subjected to a conversion reaction and a dechlorination treatment again to be converted into an aliphatic hydrocarbon, it is recovered as a low-boiling aliphatic hydrocarbon oil.

Further, as shown in FIG.
A first processing system 41 for taking out the liquid material downward from the bottom wall of the first recovery unit 8 and a second processing system 42 for taking out the gaseous material from the upper wall of the first recovery unit 8 and processing the same. And the first recovery unit 8 may be configured to separate the aliphatic hydrocarbon component into a liquid material and a gaseous material, and to separately discharge the components.

The first processing system 41 includes a first cooler 43 for supplying a cooling water to the liquid of the aliphatic hydrocarbon component to separate a liberated component of the hydrogen chloride from the aliphatic hydrocarbon. And a first storage part 44 for storing the liquid material. In the second treatment system 42, a part of the gaseous substance of the aliphatic hydrocarbon component is liquefied by cooling it with cooling water, and a free component of hydrogen chloride is separated from the aliphatic hydrocarbon. 2 cooler 45,
A second storage section 46 for storing a mixture of a liquid material and a gaseous material of the aliphatic hydrocarbon led out from the second cooler 45 is provided.

The first processing system 41 and the second processing system 4
2 are joined at a joining portion 47, and the joining portion 47
A heating chamber 48 for heating the liquid material of the aliphatic hydrocarbon component led out of the storage section 44 and the second storage section 46 to about 350 ° C. and gasifying the liquid, and a gas chamber drawn out of the heating chamber 48 A dechlorination catalyst tank 50 having a dechlorination catalyst 49 such as γ-alumina for catalytically decomposing the body into an aliphatic hydrocarbon and a chlorine component, and cooling a gaseous substance derived from the dechlorination catalyst tank 50 To liquefy a part of it and remove the separated chlorine component as aqueous hydrochloric acid.
A cooler 51 and a final recovery section 52 for containing a mixture of a liquid material and a gaseous material derived from the third cooler 51 are provided.

Then, the first storage section 44 and the second storage section 46, the heating chamber 48, the dechlorination catalyst tank 50, the third cooler 51, and the final recovery section 52 are used for the conversion shown in FIG. A conversion reaction system corresponding to the reaction system 30 is configured, and the liquid and gaseous aliphatic hydrocarbons are recovered as fuel in the final recovery section 52, and the chlorine component is converted to hydrogen chloride or the like as necessary. It is to be collected.

As described above, the gaseous substance produced by heating and thermally decomposing the organic material containing a chlorine component in the primary heating chamber 1 and the heating chambers 32 and 48 has the alumina-based catalyst 10. By supplying the gas to the dechlorination catalyst tanks 34 and 50 having the first catalyst tank 7 and the dechlorination catalysts 33 and 49, the chlorine component in the gaseous body is catalytically decomposed so as to be separated from the hydrocarbon component, Since the hydrocarbon component is recovered in the first and second recovery sections 8, 9 and the final recovery sections 37, 52, the chlorine component in the gaseous body is effectively separated and removed from the hydrocarbon component. By doing so, hydrocarbon oil or hydrocarbon gas used as fuel can be recovered and used effectively.

That is, since the gaseous substance contains a hydrocarbon component produced by thermal decomposition of an organic material and a chlorinated hydrocarbon, these are recovered as they are and burned. When used as such, it is necessary to provide a treatment facility to prevent generation of harmful substances containing chlorine. In contrast, in this example,
The chlorine component in the gaseous substance is effectively separated and removed by a dechlorination catalyst comprising an alumina-based catalyst, and the hydrocarbon component obtained by decomposing the organic material is removed. Even if the fuel is recovered and burned as fuel, no harmful substance containing chlorine is generated, and the hydrocarbon component composed of aliphatic hydrocarbon oil such as octene can be effectively used as fuel.

In addition, since the primary decomposition system 2 is filled with an alumina-based catalyst having a property that it is hardly deteriorated even under the influence of the chlorine component, even when the chlorine component is supplied to the catalyst tank, In addition, the catalytic action of the alumina-based catalyst can be maintained in a good state for a long period of time without being deteriorated. Further, the alumina-based catalyst has a lower decomposition performance of the hydrocarbon component than the zeolite-based catalyst, so that the hydrocarbon component supplied to the alumina-based catalyst is decomposed more than necessary and becomes a gaseous substance at room temperature. Butene (boiling point -6.47 ° C), propane (boiling point -42.
(1 ° C.) can be effectively suppressed from being converted into a hydrocarbon component. Therefore, by adopting the above configuration, it is possible to suppress the hydrocarbon component supplied to the catalyst tank from being unnecessarily decomposed, and to effectively recover an aliphatic hydrocarbon oil having high utility value as a fuel. Can be.

Further, as shown in the above embodiment, a gaseous substance produced by heating and thermally decomposing an organic material containing a phthalate plasticizer and a chlorine component in the first heating chamber 1 is used. The phthalic anhydride is supplied to the first catalyst tank 7, and the plasticizer is brought into contact with the alumina-based catalyst 10 to be catalytically decomposed into phthalic anhydride and a hydrocarbon component, and the phthalic anhydride is recovered in the first recovery section 8. In this case, the industrially useful phthalic anhydride can be effectively used, and the phthalic anhydride can be recovered in the second recovery section 9 and the third recovery section 15 of the secondary decomposition system 4. Since it is possible to prevent the aliphatic hydrocarbon oil or the like from being mixed into the aliphatic hydrocarbon oil or the like, the purity of the aliphatic hydrocarbon oil or the like can be improved and the commercial value thereof can be increased.

Further, as described above, the secondary heating chamber 3 in which the residual material after the primary thermal decomposition in the primary heating chamber 1 is heated and secondary pyrolyzed to be gasified, and the secondary heating chamber 3
The secondary cracking system 4 having a second catalyst tank 12 for catalytically cracking the gaseous matter generated in the above and a third recovery section 15 for recovering the catalytically cracked low-boiling hydrocarbon component is provided. When the residual material after the decomposition is configured to be decomposed and recovered, the organic material is effectively decomposed while preventing the equipment of the primary decomposition system 2 and the secondary decomposition system 4 from being corroded by hydrogen chloride. Can be recovered.

That is, when the chlorine component decomposed in the primary decomposition system 2 is in a high temperature state, each component of the primary decomposition system 2 is easily corroded by the chlorine component. It is desirable to set the heating temperature (first set temperature) of the primary heating chamber 1 to a relatively low temperature of, for example, 350 ° C. or lower, at which the chlorine component can be gasified. When the first set temperature for heating the organic material in the primary heating chamber 1 is set to a relatively low temperature as described above, a considerable amount of tar-like or wax-like material or the like after the primary pyrolysis is obtained. The organic material remains as the high-boiling hydrocarbon component. The remaining material is heated in the secondary heating chamber 3 to a second set temperature higher than the first set temperature, and is heated. After gasification, it is supplied to the second catalyst tank 12 and catalytically cracked, whereby the high-boiling hydrocarbon component having a large molecular weight can be converted into a low-boiling hydrocarbon component and recovered.

Further, since the chlorine component contained in the organic material is treated in the primary decomposition system 2, the chlorine component is not supplied to the secondary heating chamber 3 of the secondary decomposition system 4. . For this reason, even when the heating temperature (second set temperature) of the secondary heating chamber 3 is set to a high temperature, there is no possibility that the devices constituting the secondary decomposition system 4 are corroded. Therefore, by setting the second set temperature to a high temperature of about 500 ° C., the residue after the first thermal decomposition can be effectively gasified and decomposed and recovered.

The second catalytic tank 12 of the secondary cracking system 4
Since the chlorine component does not affect the solid acid catalyst filled in the inside, the decomposition performance of the hydrocarbon component as this solid acid catalyst is higher than that of the alumina-based catalyst, and the influence of the chlorine component It is possible to use a zeolite-based catalyst having a property that is susceptible to heat, and when this zeolite-based catalyst is used, the high-boiling hydrocarbon component is efficiently decomposed and converted into a low-boiling hydrocarbon oil or the like. be able to.

Therefore, according to the above configuration, even when a chlorine-based plastic material or a chlorine-based rubber material containing a chlorine component is mixed in the organic material, the chlorine-based plastic material or the chlorine-based rubber material is effectively treated and the anhydrous phthalic material is treated. Acid, hydrogen chloride, low-boiling hydrocarbon oil and the like can be efficiently recovered.
In addition, the secondary decomposition system 4 is omitted, and in the primary decomposition system 2, the phthalic anhydride generated by decomposing the phthalate ester plasticizer contained in the organic material is mixed with the phthalic anhydride. May be configured to recover hydrogen chloride generated by the decomposition of the chlorine component and the aliphatic hydrocarbon component.

As shown in FIG. 2, a conversion reaction system 30 is provided in the first decomposition system 2.
In the case where the chlorinated product of the aliphatic hydrocarbon is configured to be catalytically decomposed into an aliphatic chlorine component and a hydrocarbon component to be converted into an aliphatic hydrocarbon and recovered, the chlorinated product is recovered in the final recovery unit 37. Since chlorinated substances can be effectively prevented from being mixed into the aliphatic hydrocarbon, the purity of the aliphatic hydrocarbon can be effectively improved.

The chlorine component generated by the above-mentioned conversion reaction may be recovered in the final recovery section 37 of the conversion reaction system 30 as hydrogen chloride or the like. Further, in the dechlorination catalyst tank 34, a chlorinated product of an aliphatic hydrocarbon is reliably separated into an aliphatic hydrocarbon and a chlorine component, and the chlorinated product is converted to approximately 100% of an aliphatic hydrocarbon. In this case, a structure in which the fractionating tower 35 is omitted can be adopted.

As shown in FIG. 3, the liquid of the aliphatic hydrocarbon component led out from the bottom wall of the first recovery section 8 is supplied to a dechlorination means comprising the first cooler 43. ,
While removing hydrogen chloride in the liquid, the first
The gaseous body of the aliphatic hydrocarbon component derived from the upper wall of the recovery unit 8 is supplied to the dechlorination means comprising the second cooler 45 so that the hydrogen chloride in the gaseous body is removed. When constituted, the chlorine component in a free state can be effectively prevented from being mixed into the aliphatic hydrocarbon oil or the aliphatic hydrocarbon gas.

In the above embodiment, the first cooler 43
The liquid material of aliphatic hydrogen chloride led out of the first storage section 44 is supplied to the heating chamber 48 and heated to be gasified, and then the gaseous substance is degassed in the dechlorination catalyst tank 50.
Is supplied to a dechlorination means consisting of, and is subjected to a dechlorination treatment by contacting with a dechlorination catalyst 49 made of γ-alumina or the like, whereby a chlorine component is separated from the chlorinated product of the aliphatic hydrocarbon. As a result, the separated chlorine component is effectively removed in the third cooler 51, and converted into an aliphatic hydrocarbon oil and an aliphatic hydrocarbon gas having excellent characteristics as a fuel. At 52, it can be recovered.

Further, since the gaseous substance of the aliphatic hydrocarbon led out from the second cooler 45 is supplied to the second storage part 46, the gaseous substance is supplied to the second storage part 46 by the fuel. It can be recovered as gas. The liquid of the aliphatic hydrocarbon component liquefied in the second cooler 45 is supplied from the second recovery unit 46 to the heating chamber 48.
After the liquid material is gasified in the heating chamber 48, the dechlorination catalyst tank 4
9, the aliphatic hydrocarbon oil and the aliphatic hydrocarbon gas are separated from the chlorinated aliphatic hydrocarbon by the final recovery section 52 in a state where the chlorine component is separated from the chlorinated product of the aliphatic hydrocarbon.
, And can be effectively used.

The second cooler 45 and the second recovery section 46 are omitted, and the gaseous aliphatic hydrocarbon component derived from the upper wall of the first recovery section 8 is supplied to the dechlorination catalyst tank. 4
9 may be directly supplied to the dechlorination catalyst tank 49 to separate a chlorine component in the gaseous substance and perform a dechlorination treatment. Further, a dechlorination catalyst tank and a final recovery section are provided in each of the first processing system 41 and the second processing system 42, and the aliphatic hydrocarbon oil and the aliphatic hydrocarbon gas are separately recovered in each final recovery section. May be configured. In addition, it is not always necessary to install both the first processing system 41 and the second processing system 42 in the first recovery unit 8, and one of them may be omitted.

(Experimental Example) An experimental example conducted to confirm the effect of the apparatus and method for decomposing and recovering an organic material according to the present invention will be described below. In this experiment, as shown in FIG. 4, an organic material 17 made of 10 g of polyvinyl chloride (PVC) containing DOP as a plasticizer was placed in a quartz glass container 16 and nitrogen was introduced from one end of the quartz glass container 16. The analysis was performed by analyzing components generated by heating the organic material 17 at a temperature of about 300 ° C. for about 30 minutes while supplying a gas.

In the first experimental example in which a solid acid catalyst 18 composed of a γ-alumina-based catalyst (specific surface area 300 m ² / g) is placed in the quartz glass container 16 and catalytically cracked, A needle-like crystal 19 generated in the first recovery unit maintained at a temperature of about 80 ° C., a gaseous component recovered in the second recovery unit 20 provided at the other end of the quartz glass container 16, When the decomposition residue was weighed, FIG.
(A) was obtained. From this data, it was confirmed that 0.9 g of phthalic anhydride composed of needle-like crystals was generated, and that approximately 100% of the plasticizer in the organic material 17 was recovered.

In the quartz glass container 16, a synthetic zeolite (trade name “H-ZS” manufactured by Mobil Sekiyu KK) was used.
In a second experimental example in which a zeolite-based catalyst composed of M-5 "
As shown in FIG. 5B, 1.0 g of phthalic anhydride comprising needle-like crystals 19 was obtained, and it was confirmed that approximately 100% of the plasticizer in the organic material 17 was recovered.

On the other hand, in the third experimental example in which the organic material 17 was thermally decomposed without installing the solid acid catalyst 18, as shown in FIG. Phthalic anhydride comprising crystals was obtained, and it was confirmed that the recovery of the plasticizer was about 30%. Further, by repeating the experiment using the solid acid catalyst 18, in the fourth and fifth experimental examples using the γ-alumina catalyst and the zeolite catalyst exposed to hydrogen chloride,
The data shown in (D) and (E) of FIG. 5 was obtained.

From this data, it can be seen that when the solid acid catalysts 18 were exposed (poisoned) by hydrogen chloride, the recovery of the plasticizer was reduced to 70% and 40%, and the decomposition function was reduced. It can be seen that, especially in the case of the zeolite-based catalyst, the decomposition function is significantly reduced as compared with the γ-alumina-based catalyst. That is, based on the above experimental data, it was confirmed that the γ-alumina-based catalyst was less likely to be degraded than the zeolite-based catalyst even when affected by chlorinated compounds.

In the third experimental example in which the solid acid catalyst 18 was not used, and in the fourth and fifth experimental examples in which the exposed solid acid catalyst 18 was used, each of FIGS.
~ (E), 2.0 g, 1.4 g and 2.
0 g of the liquid component 21 was produced in the quartz glass container 16. On the other hand, the solid acid catalyst 18 not exposed
When no was used, the production of the liquid component 21 was not confirmed.

When the liquid component 21 produced in the quartz glass container 16 was analyzed by gas chromatography, data as shown in FIGS. 6 to 8 were obtained. From this data, a third experimental example not using the solid acid catalyst,
No. 4 using a γ-alumina catalyst exposed to hydrogen chloride
In the experimental example and the fifth experimental example using a zeolite catalyst exposed to hydrogen chloride, in addition to octene, octyl chloride and octanol generated by the decomposition of the organic material, a plasticizer consisting of a predetermined amount of DOP was used. Was not decomposed and remained as it was.

In the fourth experimental example using the γ-alumina catalyst exposed to hydrogen chloride, it was confirmed that the residual amount of the plasticizer was smaller than in the third and fifth experimental examples.
This experimental data also shows that the γ-alumina catalyst is less susceptible to chlorinated compounds than the zeolite catalyst.

When the gaseous components recovered in the recovery part 21 installed in the quartz glass container 16 were analyzed by gas chromatography, data as shown in FIGS. 9 to 13 were obtained. From this data, it was found that in the first experimental example using the solid acid catalyst 18 composed of a γ-alumina catalyst, as shown in FIG. 9, a low molecular weight aliphatic hydrocarbon component composed of a large amount of octene was generated. Was confirmed.

On the other hand, in the second experimental example using the solid acid catalyst 18 composed of a zeolite-based catalyst, as shown in FIG. 10, a large amount of propylene in which the aliphatic hydrocarbon component was further reduced in molecular weight was produced. Is confirmed that
In the third experimental example using no solid acid catalyst and the fifth experimental example using a zeolite-based catalyst exposed to hydrogen chloride, as shown in FIGS. 11 to 13, a low-molecular-weight aliphatic material such as benzene or octene was used. It was confirmed that only a small amount of the hydrocarbon component was produced.

In the fourth experimental example using the γ-alumina catalyst exposed to hydrogen chloride, the low-molecular-weight aliphatic hydrocarbon component composed of octene and the like is reduced to some extent as compared to before the exposure. The amount is larger than that of the third and fifth experimental examples, and it is understood that the γ-alumina-based catalyst is less susceptible to the adverse effects of chlorinated compounds than the zeolite-based catalyst.

Next, when an experiment was performed to measure the gasification rate of the organic material in the primary heating chamber 1 of the primary decomposition system 2, data as shown in FIG. 14 was obtained. That is, 1 g of an organic material made of polyvinyl chloride (PVC)
Was heated at a temperature of 300 ° C. and its vaporization rate was measured. The maximum vaporization rate was about 0.1 g / min. In order to gasify all organic materials, at least 10 g / min.
It was confirmed that it took a minute.

The first catalytic tank 10 of the primary cracking system 2
The experiment was conducted to measure the decomposition efficiency of the plasticizer in Example 1. The amount of the solid acid catalyst used per 1 g of the gaseous component of the plasticizer composed of DOP contained in the organic material was changed, and the heating temperature was varied. However, data as shown in FIG. 15 was obtained. In addition, an amorphous alumina-based catalyst (specific surface area: 200 m ² / g) was used as the solid acid catalyst.
It was used.

That is, the weight ratio between the amount of the catalyst in the first catalyst tank 10 and the amount of the gaseous component of the plasticizer is set to 0.5 / 1, 1/1.
And 2/1, the temperature of the solid acid catalyst was set to 300 ° C., 350 ° C. and 400 ° C., and the decomposition rate of the plasticizer was measured. It is desirable to set the weight ratio to 1/1 or more, and to set the heating temperature of the catalyst to 350 °
It has been confirmed that it is desirable to set C or more.

Next, an experimental example in which a chlorine component is removed from a chlorinated product of an aliphatic hydrocarbon in the conversion reaction system 30 to convert the chlorinated product into an aliphatic hydrocarbon will be described below. That is, the reaction apparatus having the primary decomposition system 2 decomposes the organic material composed of waste polyvinyl chloride containing the plasticizer composed of DOP, and recovers the liquid material of the aliphatic hydrocarbon component recovered in the second recovery section 9. Was subjected to a conversion reaction by a reactor having the above-mentioned conversion reaction system 30, and the components thereof were analyzed. As a result, data as shown in FIGS. 16 and 17 were obtained. An amorphous alumina-based catalyst (specific surface area: 300 m ² / g) was used as the dechlorination catalyst in the conversion reaction system 30.

As shown in FIG. 16, the hydrocarbon component recovered in the first recovery section 9 includes, in addition to the aliphatic hydrocarbon component composed of octene, the chlorine of the aliphatic hydrocarbon composed of a large amount of octyl chloride. Whereas, as shown in FIG. 17, the presence of the chlorinated product was not recognized in the hydrocarbon component recovered by the reaction apparatus of the conversion reaction system 30, and almost all of the compound was mixed. It was confirmed that it was converted to an aliphatic hydrocarbon.

Similar experiments were carried out using waste polyvinyl chloride containing a plasticizer made of DNP (dinonyl phthalate) as the organic material. The following data was obtained. That is, as shown in FIG. 18, the hydrocarbon components recovered in the first recovery section 9 include, in addition to the aliphatic hydrocarbon components composed of octene and nonene, the aliphatic components composed of a large amount of octyl chloride and nonyl chloride. As shown in FIG. 19, only a small amount of the chlorinated product was confirmed in the hydrocarbon component recovered by the reaction apparatus of the conversion reaction system 30 while the chlorinated product of the hydrocarbon was mixed. It was confirmed that most of them were converted to aliphatic hydrocarbons.

A small amount of chlorinated aliphatic hydrocarbons composed of octyl chloride and nonyl chloride recovered in the conversion reaction system 30 is returned from the fractionation tower 35 to the storage section 31 to perform the conversion reaction again. As a result, it is converted into an aliphatic hydrocarbon such as octene and nonene.

Next, an experimental example performed to confirm the dechlorination promoting action of the dechlorination catalyst 33 filled in the dechlorination catalyst tank 34 of the conversion reaction system 30 will be described. That is, an amorphous alumina-based catalyst (specific surface area 30
After the octyl chloride was supplied to the dechlorination catalyst tank 34 filled with 0 m ² / g) and heated at a temperature of about 300 ° C., and the recovered oil was analyzed, data as shown in FIG. Obtained. From this data, it was confirmed that most of the octyl chloride was converted to octene, and the residual amounts of octyl chloride and its isomers were extremely small.

A similar experiment was conducted by supplying octyl chloride to the dechlorination catalyst tank 34 filled with an amorphous alumina catalyst (specific surface area 200 m ² / g).
The data as shown in FIG. In this experimental example, the residual amount of octyl chloride was larger than that in the above experimental example using an alumina-based catalyst having a specific surface area of 300 m ² / g, but a considerable amount of the supplied octyl chloride was large. It was confirmed that it was converted to octene.

Next, octyl chloride was supplied to a dechlorination catalyst tank 34 filled with an amorphous alumina-based catalyst (specific surface area 140 m ² / g), and the same experiment was carried out. As shown in FIG. Although the residual amount of octyl chloride was further increased, it was confirmed that the supplied octyl chloride was converted to octene to some extent. These data show that the conversion efficiency is higher as the specific surface area of the dechlorination catalyst 33 is larger.

On the other hand, an experiment was conducted to convert octyl chloride to octene by heating the octyl chloride to 300 ° C. without using the dechlorination catalyst 33, as shown in FIG. Almost no conversion to octene was observed. From this data, it is not possible to effectively convert the chlorinated product of the aliphatic hydrocarbon into the aliphatic hydrocarbon unless the dechlorination catalyst 33 is used. It was confirmed that when the catalyst 33 was used, a chlorinated product of an aliphatic hydrocarbon could be effectively decomposed into an aliphatic hydrocarbon component and a chlorine component.

Next, an experiment was conducted to measure the rate of gasification of chlorinated aliphatic hydrocarbons in the heating chamber 32 of the conversion reaction system 30, and the data as shown in FIG. 24 was obtained. That is, 1 g of octyl chloride is added at 300 ° C.
When heated at a temperature of and measured its thermal weight loss rate,
The maximum weight loss rate was about 0.1 g / min, and it was confirmed that it took at least 10 minutes to gasify all octyl chloride.

An experiment was conducted to measure the conversion rate of octyl chloride to octene in the dechlorination catalyst tank 34 of the conversion reaction system 30, and the amount of the dechlorination catalyst 33 used per gram of octyl chloride was changed. When the heating temperature was changed variously, data as shown in FIG. 25 was obtained.

That is, the weight ratio between the amount of catalyst in the dechlorination medium tank 34 and octyl chloride is set to 0.5 / 1, 1/1 and 2/1, and the temperature of the dechlorination catalyst 33 is The conversion ratio of octyl chloride to octene was measured at 300 ° C., 350 ° C., and 400 ° C., respectively. As a result, in order to perform the conversion effectively, the weight ratio was set to 1/1 or more. It has been confirmed that it is desirable to set the heating temperature of the dechlorination catalyst 33 to 300 ° C. or higher. The dechlorination catalyst 3
Amorphous alumina catalyst (specific surface area 200 m ²⁾
/ G) was used.

Next, using the experimental apparatus shown in FIG. 4, a sample made of polyvinyl chloride containing DBP as a plasticizer was used.
An experiment was conducted in which 0 g of the organic material was heated at a temperature of about 300 ° C. to recover the aliphatic hydrocarbon gas generated by decomposing the plasticizer, and the following data was obtained. That is, when the solid acid catalyst 18 made of an alumina catalyst is used, as shown in FIG.
Needle-like crystals consisting of 1.0 g of phthalic anhydride; 4.1 g
Was obtained. And, it was confirmed that a hydrochloric acid gas, a butene gas, and a butyl chloride gas were mixed in the gaseous component, and a considerable amount of aliphatic hydrocarbon gas could be recovered.

On the other hand, when the above solid acid catalyst was not used, as shown in FIG. 27, 2.0 g of the liquid component, 0.4 g of the needle-like crystals, and 3.5 g of the gaseous The gaseous components were mostly hydrochloric acid gas and butyl chloride gas, and it was confirmed that only a small amount of butene gas was obtained. The above liquid component was mainly composed of DBP which is an undecomposed plasticizer.

[0105]

As described above, the invention according to claim 1 and claim 10 is directed to a method and an apparatus for decomposing and recovering an organic material for decomposing an organic material containing a chlorine component to recover useful components. The organic material is heated to a temperature at which the chlorine component can be gasified and gasified by thermal decomposition, and the gaseous material is supplied to a catalyst tank having an alumina-based catalyst to separate the chlorine component from the hydrocarbon component. After the catalytic cracking so that the hydrocarbon component was recovered, the chlorine component in the gaseous body was separated and removed from the hydrocarbon component, thereby containing the chlorine component even when burned. Hydrocarbon components that do not generate harmful substances can be collected and reused as fuel. Further, since the alumina-based catalyst has a property of hardly deteriorating even under the influence of the chlorine component, even when the chlorine component is supplied to the catalyst tank having the alumina-based catalyst, the catalytic action is not affected. There is an advantage that a good state is maintained for a long time without lowering.

The invention according to claim 2 and claim 11 is characterized in that the organic material is heated to a first set temperature at which the chlorine component can be gasified and gasified by primary thermal decomposition, and then the gas is heated. The solid is supplied to a catalyst tank having an alumina-based catalyst and catalytically cracked so as to separate a chlorine component from a hydrocarbon component. Then, the hydrocarbon component is recovered, and the remaining material after the heating is heated to a first set temperature. By heating at a higher temperature to gasify by secondary pyrolysis, and supplying this gaseous substance to a catalyst tank having a solid acid catalyst,
After the hydrocarbon component of the residual material is catalytically cracked to generate a low-boiling hydrocarbon component, the low-boiling hydrocarbon component is recovered, so that the heating temperature of the primary pyrolysis is set to a relatively low temperature. By setting, while preventing each device from being adversely affected by the chlorine component, by recovering the residue after the first thermal decomposition by secondary pyrolysis, the efficiency of decomposition and recovery of hydrocarbon components is effectively improved. Can be improved.

Further, in the invention according to claim 3, since the first set temperature is set to 350 ° C. or less, it is possible to prevent each device used for primary pyrolysis of the organic material from being adversely affected by chlorine components. Can be suppressed.

In the invention according to claims 4 and 13, since the zeolite catalyst is used as the solid acid catalyst for catalytically cracking the hydrocarbon component of the residual material, the residual material after the primary thermal decomposition is subjected to the secondary thermal decomposition. The high-boiling hydrocarbon component in the gaseous substance is effectively catalytically decomposed by supplying the gaseous substance produced by the above-described process to a catalyst tank filled with the zeolite-based catalyst having excellent decomposition performance. Then, it is reformed into a low-boiling hydrocarbon component, and the low-boiling hydrocarbon component can be recovered and reused.

The invention according to claim 5 and claim 14 is:
Since the chlorine component separated by supplying the gaseous substance to the catalyst tank having the alumina-based catalyst is configured to be recovered as hydrogen chloride, the chlorinated hydrocarbon contained in the gaseous substance is converted into a hydrocarbon. It is possible to collect and reuse the hydrogen chloride generated by separating the component into chlorine and the chlorine component, and to prevent the chlorine component in the free state from being mixed into the hydrocarbon component and reducing its utility value. It can be effectively prevented.

Further, the invention according to claim 6 suppresses the decomposition of the hydrocarbon component when the gas component is supplied to the catalyst tank having the alumina-based catalyst to separate the chlorine component from the hydrocarbon component. And the oil is recovered as an aliphatic hydrocarbon oil. Therefore, there is an advantage that the above-mentioned aliphatic hydrocarbon having high utility value as a fuel can be effectively recovered and reused.

Further, the invention according to claim 7 uses a γ-alumina catalyst which has a property that it is not easily degraded even when affected by the chlorine component, as the alumina catalyst for separating the chlorine component. Can be maintained in a good state for a long period of time.

Further, the invention according to claim 8 uses an amorphous alumina catalyst having an excellent function of separating a chlorine component as the alumina catalyst for separating a chlorine component.
There is an advantage that a chlorine component in a gaseous substance generated by heating and thermally decomposing an organic material can be effectively separated from a hydrocarbon component.

Further, the invention according to claims 9 and 12 has a feature of 140 m having a particularly excellent chlorine component separation function.
^Since the chlorine component in the gaseous material is separated from the hydrocarbon component using an amorphous alumina-based catalyst having a specific surface area of ² / g, it is produced by heating and thermally decomposing organic materials. The chlorine component in the gaseous body thus separated can be more effectively separated from the hydrocarbon component.

[Brief description of the drawings]

FIG. 1 is an explanatory view showing an embodiment of an organic material decomposition and recovery apparatus according to the present invention.

FIG. 2 is an explanatory diagram showing a configuration of a conversion reaction system.

FIG. 3 is an explanatory view showing an embodiment of a decomposition and recovery apparatus having a first processing system and a second processing system.

FIG. 4 is an explanatory view showing an experimental apparatus of a method for decomposing and recovering an organic material according to the present invention.

FIGS. 5A to 5E are graphs showing analytical data of component amounts generated by experiments.

FIG. 6 is a gas chromatography showing analysis data of a liquid component in a third experimental example without a catalyst.

FIG. 7 is a gas chromatography showing analytical data of liquid components in a fourth experimental example using an exposed γ-alumina catalyst.

FIG. 8 is a gas chromatograph showing analytical data of a liquid component in a fifth experimental example using an exposed zeolite catalyst.

FIG. 9 is a gas chromatography showing analysis data of gaseous components in a first experimental example using a γ-alumina-based catalyst.

FIG. 10 is a gas chromatography showing analysis data of gaseous components in a second experimental example using a zeolite-based catalyst.

FIG. 11 is a gas chromatography showing analysis data of gaseous components in the third experimental example.

FIG. 12 is a gas chromatography showing analysis data of gaseous components in the fourth experimental example.

FIG. 13 is a gas chromatography showing analysis data of gaseous components in the fifth experimental example.

FIG. 14 is a graph showing measured data of a gasification rate of polyvinyl chloride in a primary decomposition chamber.

FIG. 15 is a graph showing measurement data of a decomposition rate of a plasticizer in a dechlorination catalyst tank.

FIG. 16 is a gas chromatography showing analysis data of a hydrocarbon component recovered in a primary pyrolysis system.

FIG. 17 is a gas chromatography showing analysis data of a hydrocarbon component recovered in a conversion reaction system.

FIG. 18 is a gas chromatography showing analysis data of a hydrocarbon component recovered in a primary cracking system.

FIG. 19 is a gas chromatography showing analysis data of a hydrocarbon component recovered in a conversion reaction system.

FIG. 20 is a gas chromatography showing octyl chloride conversion data.

FIG. 21 is a gas chromatography showing octyl chloride conversion data.

FIG. 22 is a gas chromatography showing octyl chloride conversion data.

FIG. 23 is a gas chromatography showing octyl chloride conversion data.

FIG. 24 is a graph showing measured data of the gasification rate of octyl chloride in the heating chamber of the conversion reaction system.

FIG. 25 is a graph showing measured data of the conversion of octyl chloride in the dechlorination catalyst tank.

FIG. 26 is a graph showing experimental data on the decomposition of DBP when an alumina-based catalyst was used.

FIG. 27 is a graph showing experimental data on the decomposition of DBP when no alumina-based catalyst was used.

[Explanation of symbols]

 Reference Signs List 1 primary heating chamber 3 secondary heating chamber 7 first catalyst tank 8 first recovery section 9 second recovery section 10 alumina-based catalyst 12 second catalyst tank 15 third recovery section 32 heating chamber 33 dechlorination catalyst 34 dechlorination Catalyst tank 37 Final recovery section 41 First processing system 42 Second processing system 49 Dechlorination catalyst 50 Dechlorination catalyst layer 52 Final recovery section

──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. ⁶ Identification number Agency reference number FI Technical indication location C01B 7/01 9547-4H C10G 1/10 ZAB C10G 1/10 ZAB 9279-4H 11/02 11 / 02 9279-4H 17/095 17/095 9279-4H 53/00 53/00 B09B 3/00 302A (72) Inventor Akemi Muraoka No.3-1 Shinchi, Fuchu-cho, Aki-gun, Hiroshima Prefecture Mazda Corporation

Claims (14)

[Claims] 1. A method for decomposing and recovering an organic material for decomposing an organic material containing a chlorine component and recovering a useful component,
After the organic material is heated to a temperature at which the chlorine component can be gasified and gasified by thermal decomposition, the gaseous material is supplied to a catalyst tank having an alumina-based catalyst to convert the chlorine component into a hydrocarbon component. After catalytic cracking to separate from
A method for decomposing and recovering an organic material, comprising recovering the hydrocarbon component. 2. A method for decomposing and recovering an organic material, which decomposes an organic material containing a chlorine component to recover a useful component,
After the organic material is heated to a first set temperature at which the chlorine component can be gasified and gasified by primary pyrolysis, the gaseous material is supplied to a catalyst tank having an alumina-based catalyst to remove the chlorine component. After catalytic cracking to separate from the hydrocarbon component, this hydrocarbon component is recovered, and the remaining material after the heating is heated at a temperature higher than the first set temperature and subjected to secondary pyrolysis to thereby form a gaseous state. After that, by supplying this gaseous body to a catalyst tank having a solid acid catalyst,
A method for cracking and recovering an organic material, comprising the step of catalytically cracking the hydrocarbon component of the residual material to generate a low-boiling hydrocarbon component, and then recovering the low-boiling hydrocarbon component. 3. The method according to claim 2, wherein the first set temperature is set at 350 ° C. or lower. 4. The method for decomposing and recovering an organic material according to claim 2, wherein a zeolite catalyst is used as a solid acid catalyst for catalytically decomposing hydrocarbon components of the remaining material. 5. The organic material according to claim 1, wherein a chlorine component separated by supplying a gaseous substance to a catalyst tank having an alumina-based catalyst is recovered as hydrogen chloride. Decomposition and recovery method. 6. When a gaseous substance is supplied to a catalyst tank having an alumina-based catalyst to separate a chlorine component from a hydrocarbon component, the hydrocarbon component is suppressed from being decomposed to produce an aliphatic hydrocarbon oil. The method for decomposing and recovering an organic material according to claim 1, wherein the organic material is recovered. 7. The method for decomposing and recovering an organic material according to claim 1, wherein a γ-alumina catalyst is used as an alumina catalyst for separating a chlorine component. 8. The method for decomposing and recovering an organic material according to claim 1, wherein an amorphous alumina-based catalyst is used as the alumina-based catalyst for separating a chlorine component. 9. The method for decomposing and recovering an organic material according to claim 8, wherein the chlorine component in the organic material is separated using an alumina-based catalyst having a specific surface area of 140 m ² / g or more. 10. An apparatus for decomposing and recovering a useful component by decomposing an organic material containing a chlorine component, comprising: a heating chamber for heating the organic material to a temperature at which the chlorine component can be gasified; Equipped with a catalyst tank having an alumina-based catalyst that catalytically decomposes a chlorine component in a gaseous substance derived from a hydrocarbon component to separate it from a hydrocarbon component, and a recovery unit that recovers the hydrocarbon component from which the chlorine component has been separated. An organic material decomposition and recovery device, characterized in that: 11. An apparatus for decomposing and recovering a useful component by decomposing an organic material containing a chlorine component, wherein the primary heating is performed by heating the organic material to a temperature at which the chlorine component can be gasified. Chamber, a catalyst tank having an alumina-based catalyst that catalytically decomposes the chlorine component in the gaseous substance derived from the primary heating chamber to separate it from the hydrocarbon component, and a hydrocarbon component derived from the catalyst tank. A recovery section for recovering, a secondary heating chamber for heating the residual material after the primary pyrolysis at a temperature higher than the heating temperature of the primary heating chamber to gasify it by secondary pyrolysis, and the secondary heating A catalyst tank having a solid acid catalyst for catalytically decomposing hydrocarbon components in a gaseous substance derived from the chamber into low-boiling hydrocarbon components,
A recovery unit for recovering low-boiling hydrocarbon components derived from the catalyst tank. 12. A catalyst for separating a chlorine component in a gaseous substance discharged from a heating chamber from a hydrocarbon component.
12. The organic material decomposition and recovery apparatus according to claim 10, wherein an amorphous alumina catalyst having a specific surface area of at least m ² / g is used. 13. A zeolite-based catalyst is used as a solid acid catalyst for catalytically cracking a hydrocarbon component in a gaseous substance discharged from a secondary heating chamber. Organic material decomposition and recovery equipment. 14. The organic material decomposition and recovery apparatus according to claim 10, further comprising a recovery unit that recovers a chlorine component separated by the alumina-based catalyst as hydrogen chloride.