JP3178249B2 - Continuous regeneration treatment of resin with foamed polyurethane - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for continuously regenerating a foamed polyurethane resin. By contacting the contained urethane foam resin with a high-temperature, high-pressure processing liquid and / or processing liquid vapor to make it finer, and uniformly dispersing it in the molten resin,
Less decrease in physical properties than the original resin (virgin material)
The present invention also relates to a method for continuously regenerating a foamed polyurethane resin with high productivity.

According to the method of the present invention, an instrument panel (instrument panel) is formed by multi-layer molding with a urethane foam resin.
It is possible to supply the waste material of the automotive instrument panel without the skin of the material different from the base material or the skin from which the skin has been removed to the twin-screw extruder with or without the pressure adjusting mechanism. The foamed urethane resin (foaming) is supplied to the twin-screw extruder and brought into contact with a high-temperature and high-pressure processing liquid and / or processing liquid vapor under a constant temperature and pressure condition. Polyurethane) is decomposed and the resin with foamed polyurethane is refined to a level that is not harmful when reused.
By evenly dispersing in the molten resin,
By simultaneously decomposing the foamed polyurethane and uniformly dispersing it in the resin, the polyurethane can be reused as a material such as an instrument panel.

[0003]

2. Description of the Related Art Insufficient instrument panels, scrap cars, and waste instrument panels generated by repair and replacement that occur during the manufacturing stage of automobiles can be recycled as low-grade sheet materials after being crushed. An easy separation method of the bonded polyurethane foam has not been developed, and has recently been mainly landfilled. However,
The development of recycling technology has become an issue due to restrictions on landfill sites, and one of the attempts was to study the reuse of recycled materials obtained by simply pulverizing and pelletizing multi-layered instrument panels as materials for instrument panels. It was done.

However, in such a simple recycled material, relatively large foamed polyurethane pieces (100 μm or more) are dispersed in the base resin, and as foreign matter, physical properties, especially impact resistance (impact strength, brittle temperature) are reduced. It has an adverse effect and deteriorates the required performance of instrument panels and the like, and if large foamed polyurethane pieces are present on the surface of the molded article, it will have an adverse effect on the appearance and quality. Was impossible. Therefore, in order to recycle the multi-layered waste instrument panel into the original instrument panel or the like, it was necessary to perform some treatment on the foamed polyurethane, such as peeling of the foamed polyurethane bonded.

As a method for separating the polyurethane foam from the resin with the polyurethane foam, the following mechanical peeling methods are generally known, but each has the following problems.
The extrusion / screen mesh method is a method in which a resin with foamed polyurethane is pulverized, then melted by an extruder, and foamed polyurethane pieces are removed by a screen before a die. However, the screen is immediately clogged and vented up. There is a problem that the foamed polyurethane pieces pass through the screen or are forced through the screen. Specific gravity difference separation method
It is a method of separating foamed polyurethane using the difference in specific gravity between polypropylene, which is the instrument panel base material, and foamed polyurethane, but since it is necessary to finely pulverize the instrument panel material,
Development of economical pulverization technology is required. Further, it is difficult to completely peel off the bonded polyurethane foam from the base resin. The vibration compression method applies compression and vibration to the instrument panel pulverized product formed by multilayer using a special device,
This is a unique method of separating the bonded polyurethane foam, which has the advantages of low environmental load and the ability to deal with contamination adhering to the waste instrument panel, but to improve the quality of recycled instrument panel materials. However, it is difficult to completely separate the foamed polyurethane and the polypropylene base material, the entire amount of the polypropylene base material cannot be recovered, and there is still room for improvement. Further, Japanese Patent Application Laid-Open No. 6-8249 discloses that a plastic material having a bonding material such as an instrument panel is machined from a plastic body by spraying a high-pressure jet water with the bonding material separately bonded to the plastic body. A method of crushing and recycling a plastic body obtained by subjecting the resulting plastic body to specific peeling is disclosed. However, there are problems such as a long processing time and difficulty in peeling the foamed polyurethane on a complicated curved surface.

Known chemical stripping methods, such as a solvent swelling method, an alkaline solution boiling method, an acidic solution boiling method, and an organic salt-based solvent treatment method, involve immersing in an acid or alkali solvent to decompose or physically decompose the polyurethane foam. It is a method to peel off
Depending on the type of the solvent, there are problems such as swelling or erosion of the base resin and deterioration in the quality of the recycled material. In addition, a solvent that does not damage the base resin takes a very long time to peel off, which is problematic in terms of productivity. Moreover,
In addition to the necessity of a neutralization step, there is a problem that the waste liquid treatment is considerably expensive, and there is a concern that an organic solvent used in the treatment may affect the environment.

On the other hand, various methods for decomposing and regenerating urethane foam resin (polyurethane foam) have been proposed. For example, Japanese Patent Publication No. 42-10634, U.S. Pat. No. 3,117,940, U.S. Pat.
No. 03 and the like disclose a method in which foamed polyurethane is decomposed by heating with an amine.
No. 1079 and Japanese Patent Publication No. 48-5280 disclose a method for decomposing foamed polyurethane in a decomposing reagent comprising an amine compound and an alkali metal hydroxide. JP-B-46-20069 discloses a method for thermally decomposing foamed polyurethane using a glycol having 2 to 6 carbon atoms, and JP-A-48-28407 discloses a method for thermally decomposing a polyurethane having 2 to 6 carbon atoms and 0 to 10% by weight. A method for pyrolyzing foamed polyurethanes using% dialkanolamine is disclosed. Also, a method in which a foamed polyurethane is heated in a polyol together with a Lewis acid and then decomposed by adding amines (JP-A-51-39610).
), A method of subjecting foamed polyurethane to thermal decomposition using an alkoxide of an alcohol or an alkylene oxide adduct of an alcohol or an amine, or a combination of these alkoxides and an alkali hydroxide (JP-A-51-7409).
No. 7, Japanese Patent Publication No. 53-4038), a method in which a foamed polyurethane is obtained by partially alcoholating an alcohol or an amine polyol with an amine, or a metal hydroxide is added thereto and thermally decomposed ( Tokunosho 5
No. 3-40236), a polyurethane foam having 2 to 6 carbon atoms.
(Japanese Patent Publication No. 53-29359), a method of thermally decomposing a foamed polyurethane together with a mixture of an aliphatic diol and a small amount of dialkanolamine (U.S. Pat. No. 3,738,946). , Alkali metal, alkaline earth metal,
Also proposed is a method in which a hydroxide of a metal belonging to Group III, IV, VI or VIII of the Periodic Table is used as a catalyst to thermally decompose in an inert gas atmosphere (Japanese Patent Publication No. 53-19355). Have been. Furthermore, as a method for hydrolyzing polyurethane foam, Japanese Patent Application Laid-Open No. 51-16380 discloses a hydroxide of an alkali metal or an alkaline earth metal,
A method is disclosed in which foamed polyurethane is heated and hydrolyzed in an aqueous solution of a carbonate, bicarbonate, or the like.

However, the proposed methods described in the above patent publications all relate to a method for regenerating a polyurethane raw material from polyurethane waste. No method is disclosed for recovering and reusing the base resin.

[0009]

SUMMARY OF THE INVENTION It is an object of the present invention to provide a continuous and stable foamed polyurethane resin which has a simple treatment condition and a simple process, and has a small decrease in physical properties with respect to the original base resin. It is to provide a reproduction processing method.

[0010]

Means for Solving the Problems The present inventors contacted a molten resin with a foamed polyurethane with a high-temperature and high-pressure treatment liquid and / or a vapor of the treatment liquid in an extruder to thereby form the resin with a foamed polyurethane. As a result of intensive studies to develop a method for continuous and stable regeneration, we used water or a specific alcohol and devised a cylinder heating device, screw configuration, injection / exhaust system, etc. The inventors have found that the use of an extruder, particularly a twin-screw extruder, makes the above-mentioned method possible, and arrived at the present invention.

That is, the method of the present invention comprises: (a) a resin supply port with foamed polyurethane, (b) a solid transport zone,
(C) a melting zone, (d) a melt transport zone, and
(E) at least one high-pressure processing liquid and / or at a location comprising a recycled resin discharge port (die) and serving as a (c) melting zone and / or (d) a melt transport zone of a cylinder.
Alternatively, an inlet for the processing liquid vapor and at least one exhaust port (vent) are provided, and a discharge hole for the processing liquid vapor and a pipe connected thereto are provided between the injection port and the exhaust port of the cylinder. Or a pressure adjusting mechanism comprising a discharge hole for the processing liquid vapor, a pipe connected thereto, and a pressure adjusting valve provided in the pipe, and upstream of the inlet of the cylinder. The processing liquid which has been injected into a high temperature and high pressure state at a position on the side of the side (resin supply port side with foamed polyurethane) and at a position between the discharge port of the processing liquid vapor and the exhaust port of the cylinder.
Or an extruder having a structure in which a sealing portion made of a molten resin for enclosing the processing liquid vapor is provided, and a screw having a shape mainly working for kneading is provided between the sealing portions, particularly Uses a twin-screw extruder, in which the foamed polyurethane contained in the molten resin is contacted with a high-temperature and high-pressure processing liquid and / or processing liquid vapor to make the polyurethane fine, and the expanded polyurethane is (1) Water and / or hydrophilic alcohol, or (b) aliphatic saturated monohydric alcohol having 4 to 10 carbon atoms, 5 carbon atoms, Using at least one or more hydrophobic alcohols selected from the group consisting of the above alicyclic monohydric alcohols and aromatic monohydric alcohols having 7 or more carbon atoms and having a melting point of 50 ° C. or less. (2) The supply amount of the high-temperature and high-pressure processing liquid and / or the processing liquid vapor is at least 0.02 kg / H or more per 1 kg / H of the foamed polyurethane resin to be processed, and (3) When the water of (a) is used as the treatment liquid,
It can be achieved by setting the contact treatment temperature between the resin with foamed polyurethane and the treatment liquid to at least 180 ° C or higher.

Hereinafter, the method of the present invention will be described in detail. In the method of the present invention, the foamed polyurethane is decomposed by contact with a high-temperature and high-pressure processing liquid and / or processing liquid vapor.
At the same time as degradation occurs, it is mechanically pulverized, reduced in molecular weight, decomposed into fine particles, and dispersed in the base resin. Therefore, the urethane component of the resin with foamed polyurethane used in the present invention may be any urethane component that is subdivided by decomposition / degradation or the like upon contact with at least a high-temperature / high-pressure processing liquid and / or processing liquid vapor. Although not limited, a resin having a urethane bond, in particular, a rigid, semi-rigid, or soft foamed polyurethane is preferably used.

In the method of the present invention, the base resin to which the foamed polyurethane component is adhered may be decomposed under the conditions of contact between the foamed polyurethane and a high-temperature / high-pressure treatment liquid and / or a vapor of the treatment liquid. It is not particularly limited as long as it is a hard thermoplastic resin, but, for example, polypropylene, elastomer-modified polypropylene, polyolefin such as polyethylene, polyphenylene oxide, polyphenylene oxide-based resin such as modified polyphenylene oxide, ABS resin, AS resin and these A resin obtained by reinforcing the above resin with an inorganic filler is preferable. Among them, preferred are polyolefins, which are the mainstream of instrument panel materials for automobiles, particularly resins mainly composed of polypropylene, and inorganic filler reinforced resins of AS resins.

As the resin with foamed polyurethane used in the method of the present invention, the resin having a urethane bond is bonded to all or a part of the above-mentioned base resin regardless of the outer surface or the inner surface. Resin products. That is, they are used in their original applications and are used products, or products manufactured for use but have become defective products, and have the urethane bond. A resin in which the resin having the urethane bond is bonded to all or a part of the outer surface or inner surface of the base resin, regardless of the outer surface or the inner surface of the base resin, which is formed into various shapes by bonding and forming the resin and the base resin. It is a product in general. As a typical example of the resin with a foamed polyurethane, an instrument panel (instrument) for an automobile in which a foamed polyurethane is bonded to a base made of an inorganic filler reinforced resin of polypropylene or an AS resin can be preferably mentioned. .

The treatment liquid for decomposing the foamed polyurethane upon contact with the resin with the foamed polyurethane in the method of the present invention includes (1) water, (2) at least one or more hydrophilic alcohols, and (3) hydrophilic alcohols. One selected from the group consisting of an aqueous solution and (4) at least one or more hydrophobic alcohols is used. The hydrophilic alcohol is not particularly limited as long as it is an alcohol that mixes with water at an arbitrary ratio to form a uniform phase at room temperature. Specifically, methyl alcohol,
Preferable examples include ethyl alcohol, n-propyl alcohol, isopropyl alcohol, ethylene glycol, methyl cellosolve, and ethyl cellosolve. These hydrophilic alcohols may be used alone or in combination of two or more. Also,
When using the aqueous solution of the hydrophilic alcohol as the treatment liquid, the mixing ratio of water and the hydrophilic alcohol,
The weight ratio can be arbitrarily selected in the range of water / alcohol = 100/0 to 0/100, and is not particularly limited.

The hydrophobic alcohol used in the method of the present invention includes (a) an aliphatic saturated monohydric alcohol having 4 to 10 carbon atoms, an alicyclic monohydric alcohol having 5 or more carbon atoms, or 7 or more carbon atoms. (B) having a melting point of 50 ° C. or less;
Preferably, it is a liquid at normal temperature, and (c) a hydrophobic alcohol that does not freely mix with water at room temperature at an arbitrary ratio, that is, a hydrophobic alcohol having a solubility in water at room temperature of 90 g / l or less. Must satisfy the following three conditions. However,
Even if the hydrophobic alcohol satisfies the above conditions (a) and (c), the one having a melting point of more than 50 ° C. takes a long time to melt the alcohol when it is supplied into the extruder, and also has a low energy cost. This is also disadvantageous in view of the situation and is therefore preferable. Note that, in the above description, the ordinary temperature refers to a room temperature of 25 ° C. or less.

The aliphatic saturated monohydric alcohol having 4 to 10 carbon atoms includes n-butyl alcohol, isobutyl alcohol, sec-butyl alcohol, tert-butyl alcohol, n-amyl alcohol, isoamyl alcohol, 1-hexanol, -Hexanol, 3-hexanol, 1-heptanol, 2-heptanol, 1
-Octanol, 2-octanol, 1-nonanol,
Specific examples include 2-nonanol, 1-decanol, and 2-decanol. Examples of the alicyclic monohydric alcohol having 5 or more carbon atoms include cyclopentanol and cyclohexanol. Specific examples of the aromatic alcohol having 7 or more carbon atoms include benzyl alcohol, β-phenylethyl alcohol, and methylphenylcarbinol. These hydrophobic alcohols may be used alone or as a mixture of two or more types that are mixed with each other.

In the method of the present invention, among the above-mentioned hydrophilic and hydrophobic alcohols, hydrophilic alcohols such as methyl alcohol, ethyl alcohol and isopropyl alcohol, and n-butyl The use of hydrophobic alcohols such as alcohols, 1-hexanol, 1-heptanol, cyclohexanol, benzyl alcohol is preferred.

In the method of the present invention, the foamed polyurethane is decomposed by bringing the resin with foamed polyurethane into contact with the high-temperature and high-pressure treatment liquid and / or the vapor of the treatment liquid. May be added. Examples of the alkali catalyst used in the present invention include hydroxides of alkali metals such as lithium hydroxide, sodium hydroxide and potassium hydroxide, and hydroxides of alkaline earth metals such as calcium hydroxide, magnesium hydroxide and barium hydroxide. Alkali metal carbonates such as sodium carbonate and potassium carbonate, alkaline earth metal carbonates such as magnesium carbonate and calcium carbonate, and alkali metal carbonates such as sodium hydrogen carbonate and potassium hydrogen carbonate Hydrogen salts, acetates of alkali metals such as sodium acetate, sodium methylate, sodium methylate, potassium methylate, alkali metal alcoholates such as potassium ethylate and the like are preferred. Among these, particularly the alkali metals and Hydroxidation of alkaline earth metals Use of and aluminum hydroxide are preferable. In the case where the above-mentioned alcohol is used as the treatment liquid and the alkali metal alcoholate is added as an alkali catalyst, the alkali metal alcoholate is preferably prepared in advance. The metal may be added directly to the alcohol to form the alcoholate. These alkali catalysts are preferably supplied in a state of being dissolved in a processing liquid to be used or in the form of a powder, as described later. Promotes the decomposition reaction due to the contact with, that is, catalyzes the decomposition reaction.

The amount of the alkali catalyst to be added is not particularly limited as long as it does not impair the performance of the base resin even when mixed with the resin with foamed polyurethane supplied to the extruder. When the base resin is polypropylene, the content is desirably 2.5% by weight or less. 2.5 added
If the amount is more than the weight percentage, it is not preferable that the added alkali catalyst erodes the base resin, and the alkali catalyst mixed into the regenerated resin adversely affects the physical properties of the regenerated resin. As the method of adding the alkali catalyst, a method of adding to a crushed product of a resin containing foamed polyurethane and supplying the resin through a resin supply port with foamed polyurethane at the upstream end of the cylinder of the extruder, or supplying the resin into the extruder from the injection port A method of dissolving and supplying the solution in the treatment liquid is appropriate.

In the method of the present invention, the temperature at which the resin with foamed polyurethane is brought into contact with the treatment liquid and / or the vapor of the treatment liquid in the extruder is selected depending on the type of the base resin and the foamed polyurethane used. Usually, the temperature may be higher than the melting point of the base resin and lower than the thermal degradation temperature. Within this range, the temperature may be maintained at a constant temperature suitable for decomposition of the polyurethane foam. However, as long as the deterioration of the base resin does not occur, it is preferable that the temperature is as high as possible because the decomposition and miniaturization of the foamed polyurethane are efficiently performed. The pressure at this time may be any pressure that can create a gas-liquid coexistence state in a contact zone between the resin with foamed polyurethane and the processing liquid and / or the processing liquid vapor in the extruder. Therefore, the temperature and pressure of the high-temperature and high-pressure processing liquid and / or the processing liquid vapor in the extruder used in the method of the present invention are optimal for decomposition of the expanded polyurethane depending on the type of the resin with the expanded polyurethane used. Conditions should be selected and cannot be limited in general, but when the instrument panel made of polypropylene to which urethane foam resin (foamed polyurethane) is bonded is subjected to contact treatment with water and / or steam, 180 to 250
C, 9.2 to 39.5 kg / cm ² G is appropriate.
90-235 ° C and 11.8-30.2 kg / cm ² G are more preferable. When the instrument panel material is subjected to contact treatment with ethyl alcohol and / or its vapor, 16
0 to 212 ° C and 13 to 40 kg / cm ² G are appropriate, and 180 to 188 ° C and 21 to 25 kg / cm ² G are more preferable. When water and / or steam is used as the treatment substance, if the contact treatment temperature is lower than 180 ° C,
The decomposition rate of the foamed polyurethane decreases significantly, and 25
When the temperature is higher than 0 ° C., thermal deterioration of the polypropylene as the base resin occurs, and both are not preferable. Further, when ethyl alcohol and / or vapor of ethyl alcohol is used as the treatment substance, the contact treatment temperature is 160 ° C.
If the temperature is lower than 0 ° C., the melting of the polypropylene as the base resin becomes insufficient, and it becomes difficult to continuously regenerate the resin with foamed polyurethane. If the temperature is higher than 212 ° C., the pressure in the contact zone becomes 40 kg / cm ² G. And the creation of a gas-liquid coexistence state in the contact zone becomes insufficient.
Either case is not preferred. On the other hand, when the contact treatment pressure is lower than 9.2 kg / cm ² G (when water and / or steam is used as a treatment substance) or when the pressure is 13 k
When it is lower than g / cm ² G (when ethyl alcohol and / or vapor of ethyl alcohol is used as a treatment substance), the decomposition reaction rate of the foamed polyurethane is undesirably reduced. When water and / or steam is used as the treatment liquid, the pressure is 39.5 kg /
cm ² G, the temperature of the contact zone becomes 250 ° C.
When the pressure becomes higher than 40 kg / cm ² G, the contact temperature becomes higher when the pressure becomes higher than 40 kg / cm ² G. In either case, the gas-liquid coexistence state in the zone is insufficiently created, and the decomposition reaction rate of the foamed polyurethane is reduced. In order to surely prevent the occurrence of these undesired phenomena and to effectively decompose the foamed polyurethane, the contact treatment temperature and pressure should preferably be within the above-mentioned preferred ranges.

By the way, the method of the present invention melts a crushed product of the resin with foamed polyurethane, and then decomposes and miniaturizes the foamed polyurethane by contact with a high-temperature and high-pressure treatment liquid and / or vapor of the treatment liquid. It is characterized by using an extruder having a function of allowing the foamed polyurethane and the molten resin to be kneaded and uniformly dispersed in the molten resin, and then discharged to the outside of the system. As the extruder, a twin-screw extruder (intermeshing / non-intermeshing, co-rotating / different-rotating), a special single-screw extruder, a multi-screw extruder, a twin-screw reactor and the like are suitable. It is listed in. Among these, a twin-screw extruder of the twin-screw type and the same direction (or different direction) rotation is particularly preferable.

As described above, the twin-screw extruder particularly preferably used in the method of the present invention has a resin supply port with a foamed polyurethane at one end and a recycled resin discharge port, ie, a die at the other end. Provided cylinder,
In the cylinder, rotationally driven and meshing with each other 2
A screw for the shaft and a heat transfer device for heating or cooling the cylinder from the outside around the cylinder are provided.

The screw in the cylinder has a solid transport zone, a melting zone (plasticizing zone), and a melt transport zone. The melt transport zone further includes a high-temperature and high-pressure treatment liquid and It preferably comprises a contact zone with the processing liquid vapor, a devolatilization zone, and a pressurization zone. Resin with foamed polyurethane, the space portion formed by the cylinder and the screw in the cylinder, by the rotation drive of the screw, in the order of solid transport zone, melting zone, contact zone, devolatilization zone and pressure rising zone. Although it moves, the screw length should be as long as possible, especially in order to increase the residence time of the resin containing foamed polyurethane in the contact zone. Usually, the length is preferably 20 to 60 times the cylinder diameter. For a twin-screw reactor, the length is preferably 5 to 20 times the cylinder diameter.

The zones constituting the screw in the method of the present invention have the following functions. The solid transport zone is formed by a biaxial screw that crushes a foamed resin with foamed polyurethane such as a foamed polyurethane foamed instrument panel waste material supplied from a foamed polyurethane with resin supply port provided at the upstream end of the cylinder by rotational driving. By the driving force, it is transferred to the next melting zone, that is, the plasticizing zone. The resin with foamed polyurethane supplied to the solid transport zone can be supplied from a resin supply port with foamed polyurethane provided at the upstream end of the cylinder, and a high-temperature and high-pressure treatment liquid and / or treatment at the downstream side is provided. In order to efficiently decompose and miniaturize the polyurethane foam in the contact zone with the liquid vapor, it is desirable to use a crushed product which has been crushed in advance by a crusher or the like to 30 mm or less, preferably 10 mm or less.

In the melting zone, a crushed product of the resin with foamed polyurethane is kneaded with a kneading element (kneading disc).
And plasticizes by heating. The cylinder near the upstream end of this melting zone, or the point of contact with the high temperature and high pressure processing liquid and / or processing liquid vapor, which is the most upstream part of the next melt transport zone, At least one inlet for a high-pressure processing liquid and / or a high-temperature and high-pressure processing liquid vapor is provided. From this injection port, a predetermined amount of the processing liquid is fed into a high-pressure liquid state (in the case of using alcohol which is solid at room temperature as the processing liquid, the liquid state is maintained by heating in advance) and / or at a high temperature. It is supplied as a high-pressure vapor. And a point to be a melting zone or a point to be a contact zone with the high-temperature and high-pressure processing liquid and / or the processing liquid vapor, wherein the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor inlet is provided. On the upstream side (on the side of the resin supply port with foamed polyurethane), a processing liquid and / or processing liquid vapor that has been brought into a high-temperature and high-pressure state in the contact zone is sealed in a space formed by the cylinder and the screw. Therefore, a filling region of the molten resin, that is, a seal portion is formed so that the vapor pressure can be maintained by overcoming the pressure of the high-temperature and high-pressure processing liquid and / or the processing liquid vapor. Backflow of steam to the resin feed side can be prevented.

Further, in the method of the present invention, in order to efficiently perform the decomposition reaction of the foamed polyurethane in the contact zone, the retained high-pressure processing liquid and / or the high-temperature / high-pressure processing liquid vapor retain the vapor. It is necessary to provide a region, that is, a void portion based on the gas-liquid coexistence state of the processing liquid vapor / processing liquid-molten resin system. For this purpose, as described above, the cylinder and the cylinder in the melting zone or the contact zone are used. While forming a filled region (seal portion) of the molten resin in the space defined by the screw and from the downstream side (recycled resin discharge port side) of a processing liquid vapor discharge hole described later provided in the contact zone, An empty space composed of the cylinder and the screw is provided upstream (toward the resin supply port with foamed polyurethane) of an exhaust port (vent) described later provided in the next devolatilization zone. Filling zone of the molten resin (seal portion) is formed in part. The length of the filled area of the molten resin should be such a length as to create a resin seal portion that resists the pressure of the gap for the above-mentioned purpose. And the amount of high-pressure processing liquid and / or high-temperature and high-pressure processing liquid vapor injected, the temperature and pressure of the processing liquid and / or processing liquid vapor in the extruder, and the inner diameter of the extruder cylinder used. Although it cannot be said unconditionally, it is usually preferably 1 to 10 times the cylinder diameter.

The pressure of the processing liquid and / or processing liquid vapor supplied from the inlet of the processing liquid and / or processing liquid vapor is such that the high-temperature and high-pressure processing liquid and / or processing liquid vapor In order to create a region for holding steam by the above-mentioned method, it is preferable that the pressure be equal to or higher than the steam pressure of the processing liquid in the contact zone. When injecting a high-pressure processing liquid from the inlet, the temperature of the processing liquid is not particularly limited, but a processing liquid at room temperature (however, when using an alcohol that is solid at room temperature, it is preliminarily heated to a liquid state. Is convenient for handling. Then, the high-pressure processing liquid injected into the extruder is heated in the extruder and brought into a high-temperature and high-pressure state suitable for the decomposition of the foamed polyurethane as described above.

Further, in the present invention, in the area where the gap is formed in the contact zone, the foamed polyurethane existing inside the molten resin is positively moved to the surface (the gap between the resin and the gap) by the rotation of the screw. The boundary surface) is exposed, and the surface renewal portion is provided so that the processing liquid and / or the processing liquid vapor is actively penetrated into the molten resin to increase the chance of contact with the foamed polyurethane inside the resin. It is desirable.

Incidentally, the resin containing the foamed polyurethane which has passed through the contact zone and has been miniaturized to the desired degree contains a processing liquid vapor or a processing liquid, and is directly used as a recycled resin discharge port of the cylinder described later. When the resin is extruded from a die nozzle provided in the (die), the resin may be in a foamed state, and the strand may not be drawn. Therefore, the extruder used in the method of the present invention is provided with a devolatilization zone on the downstream side of the contact zone of the melt transport zone, and at least one cylinder is provided at a location where the zone is formed. An exhaust port (vent) is provided. Then, the treatment liquid in the resin is removed by discharging the gas into the atmosphere from the exhaust port (vent) or by performing a vacuum vent with a known vacuum device such as a Nash pump.

However, since only volatile components such as water and alcohol can be removed by air release from the exhaust port or vacuum venting, the impurities are discharged together with the resin to discharge the impurities together with the resin for the purpose of positively discharging the impurities. It can be discharged in a foamed state from a die nozzle portion of an outlet (die) and then washed with hot water or the like. Therefore, the devolatilization zone is not absolutely required as the screw configuration of the extruder used in the method of the present invention.

The final stage of the melt transport zone is the pressurization zone. In the pressure rising zone, a die nozzle portion is provided at the regenerated resin discharge port (die) at the end thereof, and the molten resin devolatilized in the devolatilization zone, or
By compressing the molten resin which still contains water and / or alcohol which has not been devolatilized depending on the purpose, by applying pressure sufficient to overcome the resistance of the die nozzle portion and pass through the nozzle hole, The resin is extruded from a nozzle hole and discharged from the recycled resin discharge port (die) in the form of a strand or in a foamed state. Therefore, the pressure in the pressure increasing zone is preferably about ^{2 to} 150 kg / cm ² G, although it varies depending on the type and the treatment amount of the resin with foamed polyurethane supplied to the extruder.

As described above, the resin with foamed polyurethane supplied from the resin supply port with foamed polyurethane into the extruder is supplied to the melt transport zone, that is, the contact zone, the devolatilization zone, While sequentially moving through the pressure increasing zone, the foamed polyurethane piece is decomposed and miniaturized to a level usable as a recycled material, and the foamed polyurethane piece is kneaded and included in the molten resin, so that the foamed polyurethane piece becomes It is uniformly finely dispersed in the molten resin. The degree of micronization of the foamed polyurethane is determined by reusing the foamed polyurethane piece extruded from the recycled resin discharge port (die) provided at the end of the cylinder as an instrument panel material or the like. The presence is not particularly limited as long as it does not detrimentally affect physical properties and the like, but is usually preferably 25 μm or less, more preferably 15 μm or less. The recycled molten resin discharged from the recycled resin discharge port (die) in the form of a strand is not particularly limited, but is preferably further cooled in a water-cooled water tank, cut with a pelletizer, and pelletized. These water-cooled water tanks and pelletizers
Normally used ones are sufficient. In the method of the present invention, it is possible to cut the recycled molten resin discharged from the recycled resin discharge port (die) by a method such as hot cutting or cutting with an underwater cutter. Also,
Pelletization of the reclaimed molten resin is not essential, and the reclaimed resin is discharged in a strand form from the reclaimed resin discharge port (die) by various molding methods such as injection molding, extrusion molding, blow molding, transfer molding, and press molding. It is also possible to form the final product directly from the molten resin.

Next, among the operating parameters of the extruder in the method of the present invention, in particular, the twin-screw extruder having the above-mentioned screw configuration, the main ones will be described. The degree of decomposition and miniaturization of foamed polyurethane is
The temperature, pressure and residence time of the resin containing the foamed polyurethane in the contact zone, the foamed polyurethane inside the resin is exposed to the surface where the treatment liquid and / or the vapor of the treatment liquid intervenes, or conversely, the treatment liquid and / or the treatment It is determined by the ability of the liquid vapor to permeate and disperse inside the resin and come into contact with the polyurethane foam inside the resin. Therefore, these include the reaction conditions (temperature and pressure) in the contact zone, as well as these. The processing amount of the resin with foamed polyurethane, the supply amount of the processing liquid and / or the processing liquid vapor, the screw configuration of the extruder, the number of rotations of the screw, and the like have an influence.

When the reaction temperature in the contact zone is lower than the melting point of the supplied base resin, the base resin is not sufficiently melted in the contact zone, and as a result, the foamed polyurethane and the base resin are melted. Is insufficiently kneaded, and furthermore,
A high torque is required for kneading, and in some cases, the operation of the kneading extruder is not possible. Further, if the reaction temperature in the contact zone exceeds the thermal degradation temperature of the supplied base resin, the resin with foamed polyurethane is locally heated to the thermal degradation temperature of the base resin or higher,
It is not preferable because the base resin deteriorates and the obtained resin cannot be used as a recycled material.

On the other hand, in the present invention, as described above, the reaction pressure in the contact zone is set so as to create a gas-liquid coexistence state of the treatment liquid vapor / treatment liquid-molten resin system in the contact zone. It is desirable that the vapor pressure of the processing liquid corresponds to the reaction temperature selected under the conditions of the above conditions. A third component (for example, an inert gas such as a nitrogen gas, a helium gas, an argon gas, or the like) may be injected into the contact zone. However,
If the reaction pressure is lower than the vapor pressure of the processing liquid corresponding to the set reaction temperature, the decomposition reaction rate of the foamed polyurethane is slowed, so that the foamed polyurethane is reduced to a desired degree in order to reuse the resin containing the foamed polyurethane. It is not preferable because it cannot be miniaturized. Further, when the reaction pressure in the contact zone is higher than the vapor pressure of the processing liquid corresponding to the set reaction temperature, a high-temperature / high-pressure processing liquid and / or a processing liquid is applied to the contact zone due to the pressure. A region on the upstream side of the high-pressure processing liquid and / or a high-temperature / high-pressure processing liquid vapor inlet for appropriately forming a vapor pressure holding region by steam, that is, a void based on a gas-liquid coexistence state; Insufficient sealing with the molten resin at a location between the discharge hole for the processing liquid vapor and the exhaust port described above, and therefore, the contact between the resin containing foamed polyurethane and the high-temperature processing liquid and / or the processing liquid vapor Is not performed efficiently, and the decomposition reaction rate of the foamed polyurethane becomes low, which is not preferable. Here, in the method of the present invention, when a low boiling alcohol such as methyl alcohol or ethyl alcohol is used as the treatment liquid, the reaction pressure is 40 kg.
/ Cm ² G, when the reaction pressure in the contact zone is higher than the vapor pressure of the processing liquid corresponding to the set reaction temperature, the melting in the filling region (sealing portion) of the molten resin described later is performed. Insufficient sealing with the resin, vapor of alcohol leaks from the area filled with the molten resin, and insufficient creation of a gas-liquid coexistence state in the contact zone,
It should be noted that the physical properties of the recycled resin may vary. Therefore, when the above-mentioned hydrophilic alcohol or hydrophobic alcohol is used as the treatment liquid, the reaction pressure in the contact zone is preferably at least 40 kg / cm ² G or less.

In the method of the present invention, a pressure adjusting mechanism may be provided in the contact zone. This pressure adjusting mechanism makes the vapor pressure holding region formed by the high temperature and high pressure processing liquid and / or processing liquid vapor formed in the contact zone coexist with the gas and liquid, and maintains the vapor pressure of the processing liquid. A method for maintaining a temperature corresponding to the vapor pressure of the treatment liquid, thereby maintaining the high-temperature and high-pressure state in the contact zone under constant conditions (temperature and pressure) suitable for a decomposition reaction of the polyurethane foam. It is. Therefore, the pressure adjusting mechanism is not particularly limited as long as the above-described object can be achieved. However, the pressure adjusting mechanism is not limited to the cylinder located upstream of the devolatilization zone and near the end of the contact zone. A discharge hole for the processing liquid vapor, a pipe connected thereto, and a pipe are provided in the pipe (an intermediate portion between the inlet of the high-pressure processing liquid and / or the high-temperature high-pressure processing liquid vapor and the exhaust port). It is preferable that the pressure control valve is formed. In the method of the present invention, the pressure adjusting mechanism is not always necessary, but it is preferable to provide the pressure adjusting mechanism, as described above, in the decomposition reaction conditions (temperature and pressure) of the foamed polyurethane in the contact zone. Is preferable because it is possible to maintain a constant value and to prevent a surging phenomenon (fluctuation in extrusion rate) during operation of the extruder.

Further, in the method of the present invention, the discharge hole of the processing liquid vapor and the pipe connected thereto and the stop valve are provided in the pipe, or the pressure adjusting mechanism is provided. Excess water and / or alcohol and their vapors (treatment liquid and / or treatment liquid vapor) present in the extruder are discharged out of the extruder system through pipes from the discharge holes of the treatment liquid vapor, and thus, fresh and constantly fresh water is discharged. Processing liquid and / or processing liquid vapor will be supplied into the extruder. Until the excess water and / or alcohol or their vapor passes through the pressure regulating valve or the stop valve, part or all of the excess water and / or alcohol is kept in a hot liquid state. The decomposition product in the contact zone, which is a component soluble in the liquid, is discharged out of the extruder system together with the hot liquid. As a result, impurities in the recycled resin are reduced, and recombination of the decomposed foamed polyurethane component can be reduced.

The longer the residence time of the resin containing foamed polyurethane in the contact zone, that is, the longer the decomposition reaction time of the foamed polyurethane, the more the foamed polyurethane is decomposed and miniaturized. Therefore, the pressure and temperature of the resin containing the foamed polyurethane in the contact zone, the supply amount of the high-temperature and high-pressure processing liquid and / or the processing liquid vapor, the cylinder diameter of the extruder, the screw configuration, the screw length and the screw rotation speed, etc. The reaction time is proportional to the throughput of the resin containing the foamed polyurethane, as long as the extruder is operated with the above operating parameters kept constant. In other words, the smaller the amount of the resin containing the foamed polyurethane is, the more the decomposition reaction of the foamed polyurethane proceeds, and the finer the foamed polyurethane becomes, but the opposite effect is brought about from the viewpoint of the production efficiency of the recycled resin. The preferable range of the treatment amount of the resin containing the foamed polyurethane in the method of the present invention is complicatedly influenced by the various operating parameters described above, and cannot be unconditionally determined. However, in practice, a cylinder diameter of 55 mmφ and L / D In the case of an extruder in which (the ratio of the screw length to the cylinder diameter) = 60, the extruder is preferably 10 to 150 kg / H, particularly preferably 20 to 100 kg / H. When the cylinder diameter is other than 55 mmφ, the processing amount is preferably within the range limited by the following mathematical expression 1.

[0040]

(Equation 1)

In the method of the present invention, in order to efficiently contact the resin containing foamed polyurethane with the high-temperature and high-pressure processing liquid and / or the processing liquid vapor in the contact zone,
As described above, a gas-liquid coexistence state of the processing liquid vapor / processing liquid-molten resin system is created in the contact zone, and the high-temperature and high-pressure processing liquid and / or the gap that holds the vapor pressure of the processing liquid vapor is removed. Must be properly formed and therefore
The porosity in the contact zone, that is, the ratio of the void portion in the contact zone and the processing liquid supply rate, that is, the supply amount of the high-pressure processing liquid and / or the high-temperature / high-pressure processing liquid vapor is appropriate. It is necessary to make it. The appropriate supply amount of the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor is determined by the type of foamed polyurethane and the base resin, the pressure and temperature of the resin containing the foamed polyurethane in the contact zone, and the processing to be supplied. Depending on the pressure and temperature of the liquid and / or the processing liquid vapor, in an extruder having a cylinder diameter of 55 mmφ, the resin with foamed polyurethane to be treated (resin including foamed polyurethane) 1 kg /
0.02-1 kg / H per H, preferably 0.05-
Preferably, it is 0.5 kg / H. When the supply amount of the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor is less than the above range, the decomposition reaction rate of the foamed polyurethane in the contact zone is undesirably low. Conversely, when the supply amount of the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor is larger than the above range, it is not expected that the decomposition reaction rate of the foamed polyurethane in the contact zone is further improved. In addition, the removal of the processing liquid and / or the processing liquid vapor from the resin with foamed polyurethane in the devolatilization zone becomes insufficient, and as described above, the recycled resin discharged from the recycled resin discharge port (die) of the cylinder. Is in a foamed state, and the strand may not be drawn, which is not preferable. If the supply amount of the high-pressure processing liquid and / or the high-temperature / high-pressure processing liquid vapor is less than the preferred range, the decomposition reaction rate of the foamed polyurethane in the contact zone tends to decrease, and If the amount exceeds the preferable range, the processing liquid and / or the processing liquid vapor may not be sufficiently removed from the resin with the foamed polyurethane in the devolatilization zone. In the method of the present invention, as described above, high-pressure processing liquid and / or high-temperature and high-pressure processing liquid vapor can be injected from the inlet of the high-pressure processing liquid and / or high-temperature and high-pressure processing liquid vapor. In order to increase the contact efficiency between the resin containing foamed polyurethane and the high-temperature and high-pressure processing liquid and / or processing liquid vapor in the contact zone, a high-pressure processing liquid is injected from the injection port,
It is preferable to create a vapor-liquid coexistence state of a processing liquid vapor / processing liquid-molten resin system in the contact zone by generating a vapor of the processing liquid in the contact zone.

In the present invention, a pipe is connected to the above-mentioned high-pressure processing liquid and / or a high-temperature and high-pressure processing liquid vapor inlet, and the high-pressure processing liquid such as a constant-rate pump is connected to the upstream end of the pipe. And / or by providing a device for quantitatively supplying the high-temperature and high-pressure processing liquid vapor, the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor are supplied into the contact zone in the appropriate amount described above. It can feed quantitatively.

The screw rotation speed of the extruder depends on the processing amount of the resin with foamed polyurethane and the surface renewal function of the molten resin in the contact zone, that is, the decomposition reaction of the foamed polyurethane contained in the molten resin in the contact zone. Affect. In the method of the present invention, when using an extruder having a cylinder diameter of 55 mmφ, the screw rotation speed is set to 100 to 40.
It is preferable to set it to about 0 rpm. If the screw rotation speed is less than 100 rpm, the kneading of the foamed polyurethane and the base resin in the contact zone becomes insufficient, and the foamed polyurethane inside the resin is exposed to the treatment liquid and / or the intervening surface of the treatment liquid vapor. Alternatively, the chance that the treatment liquid and / or the vapor of the treatment liquid permeates into the resin and comes into contact with the foamed polyurethane inside the resin decreases, so that the surface renewal function of the so-called molten resin decreases, and the decomposition reaction rate of the foamed polyurethane decreases. Is undesirably low. When the screw rotation speed is more than 400 rpm, the output power of the molten resin by the rotation of the screw increases,
The transport amount of the resin with foamed polyurethane with respect to the supply amount of the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor in the contact zone increases, and the residence time of the resin with foamed polyurethane in the contact zone is reduced. At the same time, the filling area of the molten resin in the resin seal portion is shortened, and the sealing with the molten resin is weakened, so that the decomposition reaction rate of the foamed polyurethane is reduced, while the temperature of the base resin is increased, and the deterioration of the base resin is deteriorated. Undesirably occurs. The control of the screw rotation speed can be performed by a known method, for example, a method using a variable speed motor as a driving device can be suitably adopted.

By the way, in the method of the present invention, in order to stabilize the quality of the regenerated material, the resin containing foamed polyurethane existing in the space defined by the cylinder and the screw in the cylinder is used. Temperature conditions need to be kept constant. In other words, a heating mechanism is necessary to raise the temperature at the start or to adjust the set temperature that differs depending on the type of the resin with the foamed polyurethane to be treated. In order to increase the temperature, a cooling mechanism is necessary. For the cylinder, temperature control such as heating and cooling is performed in several sections according to the length of the screw. It is necessary. Therefore, the extruder used in the present invention adopts a block system for the cylinder, and is provided with a heat transfer device for heating or cooling the cylinder from the outside around the cylinder in each block unit. desirable. As such a heat transfer device, a known device such as an electric heater or a jacket structure wound around the cylinder can be used, and for each block of the cylinder, as desired, a heating medium such as steam, or What is necessary is just to flow a cooling medium such as cooling water through the heat transfer device.

As described above, the extruder used in the method of the present invention, particularly the twin-screw extruder of the mesh type co-rotating (or counter-rotating), which is preferably used, has a self-cleaning property. It is a mechanical device that is excellent in temperature control, accurate in temperature control, and excellent in surface renewal function and devolatilization capability of molten resin. (1) Processing amount of resin with foamed polyurethane, screw configuration, screw rotation speed (2) Since the screw is of a segment type and the cylinder is of a block type, it is possible to control the time required for the molten resin to stay in the extruder. It is easy to change the screw configuration such as adding or removing a volatilization zone, and to change the axial length of the kneading part. (3) Pressure adjustment When a structure is provided, by changing the set pressure of the installed pressure regulating valve, the conditions (pressure and temperature) suitable for the decomposition reaction of the foamed polyurethane can be easily adjusted according to the type of foamed polyurethane resin to be treated. It is also a flexible machine for the production process with considerable flexibility in processing conditions, such as being able to hold.

In the present invention, as described above, the exhaust gas is discharged through a pipe connected to the discharge hole of the processing liquid vapor of the extruder, or through a pressure regulating valve constituting a pressure regulating mechanism of the extruder. It is discharged outside the extruder system. The exhaust gas mainly contains decomposition products of the foamed polyurethane based on the contact between the resin with the foamed polyurethane and the treatment liquid and / or the treatment liquid vapor in the contact zone of the extruder, and the treatment liquid vapor. The decomposition products of the foamed polyurethane include a compound having an isocyanate group such as a polyisocyanate due to cleavage of a urethane bond and an alcohol having a hydroxyl group such as a polyether. Accordingly, the exhaust gas is subjected to, for example, a distillation treatment with a distillation apparatus to make the low-boiling compounds and high-boiling compounds separated non-polluting, while recovering water and / or alcohol and forming the resin with foamed polyurethane. Is preferably circulated and used as a treatment liquid for the decomposition treatment of the phenol.

In the method of the present invention, if the required quality of the regenerated product is severe, an impact modifier or a compatibilizer may be added during the kneading process in the extruder, or the regenerated pellets may be re-formed in the extruder. To supply to the resin supply port with foamed polyurethane and pass through the extruder or, if necessary, to the recycled resin discharge port (die) of the extruder to continuously remove foamed polyurethane pieces that have not been completely decomposed. It goes without saying that the quality of the recycled product can be made closer to that of the virgin material by installing the automatic backwash filter.

The method of the present invention will now be described in detail with reference to the accompanying drawings. FIG. 1 is a schematic flow chart showing one embodiment of the method of the present invention. In FIG.
1 is a tank, 2 is a metering pump, 3 is a pressure regulating valve, 4 is 2
Shaft screw type extruder, 41 is a cylinder, 42 is a screw, 43 is a resin supply port with foamed polyurethane attached to the cylinder 41, 44 is a recycled resin discharge port attached to the cylinder 41, and 45 is attached to the cylinder 41. A high-pressure processing liquid and / or high-temperature and high-pressure processing liquid vapor inlet, 46 is a processing liquid vapor discharge hole mounted on the cylinder 41, 47 is an exhaust port mounted on the cylinder 41, and 48 is a heat transfer device. .

The cylinder 4 of the twin screw type extruder 4
A screw 42 is disposed in the screw 1, and the screw 42 is rotatably driven at one end by a driving device not shown in FIG. 1. A resin supply port 43 with foamed polyurethane is provided on the drive device side of the cylinder 41, and a recycled resin discharge port 44 is provided at the other end of the cylinder 41. When the resin is supplied, the resin is carried to the recycled resin discharge port 44 side with the rotation of the screw. A heat transfer device 48 is attached to the outer periphery of the cylinder 41, and the cylinder 41 is heated or cooled. As it proceeds, it is melted and maintained at a suitable temperature.

The screw 42 is connected to the solid transport zone 42
1, a melting zone 422 and a melt transport zone 423. The melt transport zone 423 further includes a contact zone 424, a devolatilization zone 425, and a pressurization zone 4.
26, and at least a part of the contact zone 424 serves as a surface updating portion 427. FIG.
In the melting zone 422, the crushed product of the foamed polyurethane resin supplied to the foamed polyurethane resin supply port 43 and crushed by a crushing device not shown in FIG. The mixture is heated and melted by a kneading element (kneading disk) which is not heated, and is plasticized.

At a position near the upstream end of the contact zone 424 of the cylinder 41, a high-pressure processing liquid and / or a high-temperature and high-pressure processing liquid vapor inlet 45 is provided. And connected to the tank 1 by piping. The tank 1 is filled with water and / or alcohol as a treatment liquid for the resin with foamed polyurethane. When an alkali catalyst is used for the treatment of the foamed polyurethane resin with the treatment liquid and / or the treatment liquid vapor, the treatment liquid is supplied to the tank 1 and a predetermined amount of the alkali catalyst is used. Is supplied, and the both are stirred and mixed, whereby a processing solution containing an alkali catalyst having a predetermined concentration is filled. When an alcohol that is solid at room temperature is supplied, the alcohol is heated by a suitable heating device (not shown in FIG. 1) provided in the tank 1 prior to the addition of the alkali catalyst. It is in a liquid state. An appropriate amount of the processing liquid, that is, water and / or alcohol, enters the metering pump 2 from the tank 1 through the pipe, is pressurized to a predetermined pressure by the metering pump 2, and again flows through the pipe to obtain a high-pressure processing liquid and / or high temperature. High-pressure processing liquid vapor inlet 4
5 is supplied. The high pressure processing liquid and / or the high temperature / high pressure processing liquid vapor inlet 45 is connected to the contact zone 42.
The water and / or alcohol fed to the contact zone 4 contacts the molten resin containing the foamed polyurethane, which is also sent to the contact zone 424, and is heated by the high-temperature molten resin. And / or vapor of alcohol is generated. At the same time, due to this contact, the decomposition reaction of the foamed polyurethane proceeds, and the foamed polyurethane is reduced in molecular weight and fined to a desired level.

A high-pressure processing liquid and / or a high-temperature and high-pressure processing liquid vapor inlet 45 is provided at a portion of the cylinder 41 located near the end of the contact zone 424.
A processing liquid vapor discharge hole 46 for discharging the processing liquid vapor generated by the evaporation of the processing liquid fed to the fuel cell 24, that is, water vapor and / or alcohol vapor, is provided. Is provided. The melting zone 42 of the space 420
2 from the vicinity of the terminal end to the position upstream of the high-pressure processing liquid and / or high-temperature and high-pressure processing liquid vapor inlet 45 and near the upstream end of the contact zone 424; On the downstream side of the liquid vapor discharge hole 46,
In addition, a portion from a position near the end of the contact zone 424 to a position near the upstream end of the devolatilization zone 425 includes:
By providing a kneading element (not shown in FIG. 1), the molten resin can be sealed with high-temperature and high-pressure processing liquid and / or processing liquid vapor based on the processing liquid fed to the contact zone 424. 428 and 429 are formed.

Thus, in the contact zone 424, a vapor pressure holding region 430 based on the evaporation of the high-pressure processing liquid and / or the processing liquid fed into the contact zone 424 from the high-temperature and high-pressure processing liquid vapor inlet 45 is formed. Secured. Therefore, the contact zone 42
While the foamed polyurethane existing inside the resin is positively exposed to the surface (the boundary surface between the processing liquid vapor layer and the resin layer) by the screw provided mainly in the kneading and working mainly for kneading, the processing liquid and the processing liquid And / or the surface renewing portion 42 that actively infiltrates the processing resin vapor into the molten resin to increase the chance of contact with the foamed polyurethane existing inside the resin.
7 is expressed.

By securing the vapor pressure holding region 430 in the contact zone 424, the pressure regulating valve 3 is set to a pressure corresponding to the saturated vapor pressure of the processing liquid at a temperature suitable for the decomposition reaction of the polyurethane foam. For example, the vapor pressure holding region 430 is maintained in a saturated vapor state, and the temperature is maintained at a temperature corresponding to the saturated vapor pressure, and the contact zone 424 is maintained.
Is maintained under constant temperature and pressure conditions that are optimal for the decomposition reaction of the polyurethane foam.

As described above, the molten resin containing the polyurethane foam which has been miniaturized to a desired level is carried to the next devolatilization zone 425. An exhaust port 47 is attached to the cylinder 41 located in the devolatilization zone 425, and the exhaust port 47 is further connected to a vacuum device (not shown in FIG. 1) through a pipe connected thereto. The molten resin delivered to the devolatilization zone 425 contains a processing liquid vapor and / or a processing liquid that causes foaming at the time of discharge from the recycled resin discharge port 44 described later,
When the pressure is reduced by the vacuum device, the molten resin expands, and volatile components such as water and alcohol contained therein are discharged from the exhaust port 47 to the vacuum device side.

The molten resin devolatilized in the devolatilization zone 425 is sent to a pressure rising zone 426 which is the final stage of the screw configuration of the twin screw type extruder 4. A recycle resin discharge port 44 is attached to the cylinder 41 located at the end of the pressure rising zone 426, and a die nozzle portion (not shown in FIG. 1) is provided at the recycle resin discharge port 44. Have been. The molten resin delivered to the pressurizing zone 426 is compressed under pressure, and can only pass through the nozzle holes (also not shown in FIG. 1) of the die nozzle portion, overcoming the resistance of the die nozzle portion. A sufficient pressure is applied, the resin is extruded from the nozzle hole, and discharged from the recycled resin discharge port 44 in the form of a strand.

The foamed polyurethane that has passed through the contact zone 424 and has been refined to a desired level is kneaded into the molten resin while being advanced through the devolatilizing zone 425 and the pressurizing zone 426 by rotation of the screw 42. -Included. As a result, the recycled resin in which the foamed polyurethane finely divided to a level usable as a recycled material is uniformly finely dispersed in the base resin is discharged in a strand form from the recycled resin discharge port 44.

The recycled resin discharged in the form of a strand from the recycled resin discharge port 44 is cooled and solidified in a water-cooled water tank (not shown in FIG. 1), and is also shown in FIG. The pellet is cut by a pelletizer that is not used.

[0059]

EXAMPLES Next, the method of the present invention will be described in more detail with reference to Examples and Comparative Examples, but the method of the present invention is not limited thereto.

In the following Examples and Comparative Examples, the measurement of the surface smoothness of the pellets obtained when a material containing no foamed polyurethane (crushed instrument panel molded product before multilayer molding) was used as a raw material (Comparative Example 1) Leave the result blank,
The measurement results of the surface smoothness of the pellets obtained in each Example and Comparative Example (excluding Comparative Example 1) were relatively compared with the blank. That is, the measurement results of each Example and Comparative Example (excluding Comparative Example 1) in the case where the measurement result of the blank was “O” were compared with the blank,
It was expressed in three stages of “○”, “△” and “×”. Further, the embrittlement temperature is defined as a mechanical property value by ASTM D746.
Measured according to -79.

Example 1 A cylinder having a cylinder configuration and a screw configuration shown in FIG.
0mm and the same length rotation 60D screw length 2
Using a screw-type extruder 4, raw materials (crushed propylene instrument panel waste including ethylene-propylene rubber,
24kg / with foamed polyurethane, average particle size: 8mm)
H was supplied. Then, 9.6 of water is supplied from the high pressure processing liquid and / or the high temperature / high pressure processing liquid vapor inlet 45.
kg / H (accordingly, the supply amount of water to the raw material: 40% by weight), and set the cylinder temperature to the melting zone 422 and the contact zone 42 in the cylinder 41.
4. In each of the devolatilizing zone 425 and the pressure rising zone 426, the temperature was set to 220 ° C., and the pressure regulating valve 3 was adjusted to maintain the internal gas pressure at 20 to 23 kg / cm ² G. When the twin screw type extruder 4 was operated at a rotation speed of the screw 42 of 300 rpm, the average residence time of the raw material in the cylinder 41 was about 450 seconds, was gotten. The strand was cooled in a water-cooled water bath, and the pellets obtained by cutting with a pelletizer were dried, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured.
Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Embodiments 2 to 4 The supply rate of water from the high-pressure processing liquid and / or the high-temperature / high-pressure processing liquid vapor inlet 45 was changed to 9.6 kg / H. H (hence
The supply amount of water to the raw material: 30% by weight), 2.4 kg / H in Example 3 (therefore, the supply amount of water to the raw material: 10% by weight), and in Example 4, 1.
2 kg / H (therefore, the water supply to the raw material: 5
% By weight), and dried pellets were produced in the same manner as in Example 1, and the surface smoothness and mechanical properties (brittle temperature) of these pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Comparative Example 1 As a blank test, a crushed polypropylene instrument panel waste material containing ethylene-propylene rubber as a raw material in Example 1 (with foamed polyurethane, average particle size: 8 mm)
Was changed to a material not containing foamed polyurethane (crushed instrument panel molded product before multilayer molding, average particle size: 8 mm), and dried pellets were produced in the same manner as in Example 1, and the pellets were produced. Was measured for surface smoothness and mechanical properties (brittle temperature). Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

COMPARATIVE EXAMPLE 2 The supply rate of water from the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor inlet 45 was changed to 9.6 kg / H, and 0.24 kg / H (therefore, water relative to the raw material). (Dry weight: 1% by weight), dried pellets were produced in the same manner as in Example 1, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Example 5 The cylinder set temperature was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilization zone 425, and the pressure rising zone 426 in the cylinder 41 to 250 ° C.
° C and adjusting the pressure control valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 38 to 4
Dry pellets were produced in the same manner as in Example 2 except that the pellets were maintained at 0 kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Example 6 The cylinder set temperature was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilization zone 425, and the pressure rising zone 426 in the cylinder 41.
° C and adjusting the pressure control valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 14 to 1
Dry pellets were produced in the same manner as in Example 2 except that the pellets were maintained at 6 kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Example 7 The temperature of the cylinder was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilizing zone 425, and the pressure increasing zone 426 in the cylinder 41 by changing the temperature to 220 ° C.
° C and adjusting the pressure control valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 8 to 10 kg.
Dry pellets were produced in the same manner as in Example 2 except that the pellets were kept at kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Comparative Example 3 The temperature of the cylinder was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilizing zone 425 and the pressure increasing zone 426 in the cylinder 41,
° C and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 6 to 8 k
Dry pellets were produced in the same manner as in Example 2 except that the pellets were maintained at g / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

Example 8 Sodium hydroxide previously adjusted to a concentration of 0.33% by weight from a high pressure processing liquid and / or a high temperature / high pressure processing liquid vapor inlet 45 to 7.2 kg / H of water. Example 2 except that the aqueous solution was supplied at a rate of 7.2 kg / H (the supply amount of water to the raw material: 30% by weight, and the addition amount of sodium hydroxide to the raw material: 0.1% by weight). Produce dried pellets in the same manner as
The surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 1 shows the measurement results of the surface smoothness and the mechanical properties.

[0070]

[Table 1]

Example 9 From the vapor inlet 45 of the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid, water was changed to 9.6 kg / H, and benzyl alcohol was added at a rate of 9.6 kg / H (therefore, based on the raw material). (Amount of supply of benzyl alcohol: 40% by weight), and adjusting the pressure control valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 1 to 3 kg.
/ Cm ² G, except that dried pellets were produced in the same manner as in Example 1, and the surface smoothness and mechanical properties (brittleness temperature) of the pellets were measured. Table 2 shows the measurement results of the surface smoothness and the mechanical properties.

Examples 10 to 12 The supply ratio of benzyl alcohol from the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor inlet 45 was 9.6.
kg / H, 7.2 kg / H in Example 10.
H (therefore, the supply amount of benzyl alcohol to the raw material: 30% by weight), and in Example 11, 2.4 kg
/ H (therefore, the supply of benzyl alcohol to the raw material: 10% by weight), and in Example 12, 1.2 kg / H (therefore, the supply of benzyl alcohol to the raw material: 5% by weight), Dried pellets were produced in the same manner as in Example 9, and the surface smoothness and mechanical properties (brittleness temperature) of these pellets were measured.
Was measured. Table 2 shows the measurement results of the surface smoothness and the mechanical properties.

Comparative Example 4 The supply ratio of benzyl alcohol from the high-pressure processing liquid and / or the high-temperature and high-pressure processing liquid vapor inlet 45 was 9.6.
Dry pellets were produced in the same manner as in Example 9 except that the weight was changed to 0.24 kg / H (therefore, the supply amount of benzyl alcohol based on the raw material: 1% by weight). The surface smoothness and mechanical properties (brittle temperature) were measured. Table 2 shows the measurement results of the surface smoothness and the mechanical properties.

Examples 13 to 15 The cylinder set temperature was set to 220 ° C. in Example 10 for each of the melting zone 422, the contact zone 424, the devolatilizing zone 425 and the pressure increasing zone 426 in the cylinder 41.
In Example 13, dried pellets were produced in the same manner as in Example 10 except that the temperature was changed to 250 ° C., 180 ° C., and 170 ° C. in Examples 13, 14 and 15, respectively. The surface smoothness and mechanical properties (brittle temperature) were measured. Table 2 shows the measurement results of the surface smoothness and the mechanical properties.

Example 16 Dry pellets were produced in the same manner as in Example 9 except that a stop valve was provided in place of the pressure regulating valve 3 in the treatment liquid vapor discharge line, and the surface smoothness of the pellets was obtained. And mechanical properties (brittle temperature) were measured. Immediately after the start of the operation of the extruder 4, the opening of the stop valve was frequently adjusted so that the internal gas phase pressure became 1 to 3 kg / cm ² G, but after the steady state was reached, the stop valve was opened. The adjustment of the degree was not required, the extruder 4 could be operated stably, and no variation was observed in the measurement results of the surface smoothness and mechanical properties (brittle temperature) of the pellets. Table 2 shows the measurement results of the surface smoothness and the mechanical properties.

[0076]

[Table 2]

Example 17 At a rate of 7.2 kg / H of cyclohexanol (therefore, based on the raw material (Supply amount of cyclohexanol: 30% by weight), and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to ² to 4 kg.
/ Cm ² G, except that dried pellets were produced in the same manner as in Example 1, and the surface smoothness and mechanical properties (brittleness temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 18 The temperature of the cylinder was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilizing zone 425, and the pressure rising zone 426 in the cylinder 41 by changing the temperature to 220 ° C.
° C and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to ² to 4 kg / cm ² G to 0 to 1 kg /
Dry pellets were produced in the same manner as in Example 17 except that the pellets were kept at cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 19 1-heptanol was added at a rate of 7.2 kg / H (according to the starting material And the internal gas phase pressure was changed to 20 to 23 kg / cm ² G to 1 to 3 kg / c by adjusting the pressure regulating valve 3.
Dry pellets were produced in the same manner as in Example 1 except that the pellets were maintained at m ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 20 The temperature of the cylinder was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilizing zone 425 and the pressure increasing zone 426 in the cylinder 41 by changing the temperature to 220 ° C.
° C and adjusting the pressure regulating valve 3 to change the internal gas phase pressure from 1 to 3 kg / cm ² G to 0 to 1 kg /
Dry pellets were produced in the same manner as in Example 19 except that the pellets were kept at cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 21 From the high pressure processing liquid and / or high temperature / high pressure processing liquid vapor inlet 45, 1-hexanol was changed to water at 9.6 kg / H at a rate of 7.2 kg / H (accordingly, And the internal gas phase pressure was changed to 20 to 23 kg / cm ² G by adjusting the pressure regulating valve 3 to 3 to 5 kg / c.
Dry pellets were produced in the same manner as in Example 1 except that the pellets were maintained at m ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 22 The temperature of the cylinder was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilizing zone 425, and the pressure increasing zone 426 in the cylinder 41.
° C and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 3 to 5 kg / cm ² G to 0.5 to 1.
Dry pellets were produced in the same manner as in Example 21 except that the pellets were kept at 5 kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 23 n-Butyl alcohol was changed to 7.2 kg / H at a rate of 7.2 kg / H by changing water to 9.6 kg / H from the high pressure processing liquid and / or high temperature / high pressure processing liquid vapor inlet 45. (Amount of supply of n-butyl alcohol to the raw material: 30% by weight)
And adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 13 to
Dry pellets were produced in the same manner as in Example 1 except that the pellets were kept at 15 kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

Example 24 The cylinder set temperature was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilization zone 425, and the pressure rising zone 426 in the cylinder 41 to 180 ° C.
° C and adjusting the pressure control valve 3 to change the internal gas pressure to 13 to 15 kg / cm ² G to 4 to 6 k
Dry pellets were produced in the same manner as in Example 23 except that the pellets were kept at g / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 3 shows the measurement results of the surface smoothness and the mechanical properties.

[0085]

[Table 3]

Example 25 High-pressure processing liquid and / or high-temperature high-pressure processing liquid vapor injection
From the inlet 45, the water was changed to 9.6 kg / H, and
Alcohol at a rate of 7.2 kg / H
Supply amount of n-propyl alcohol to the raw material: 30 weight
%) And adjusting the pressure control valve 3
And the internal gas pressure is 20-23 kg / cm ^TwoChange to G
23-25 kg / cm^TwoExcept that it was held at G
Dry pellets were prepared in the same manner as in Example 1,
Was measured for surface smoothness and mechanical properties (brittle temperature).
Table 4 shows the measurement results of surface smoothness and mechanical properties.
You.

Example 26 The cylinder set temperature was changed to 220 ° C. in each of the melting zone 422, the contact zone 424, the devolatilization zone 425, and the pressure rising zone 426 in the cylinder 41 to 180 °.
° C and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 23 to 25 kg / cm ² G to 9 to 11
Dry pellets were produced in the same manner as in Example 25 except that the pellets were kept at kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 4 shows the measurement results of the surface smoothness and the mechanical properties.

Example 27 Ethyl alcohol was used instead of water at a rate of 7.2 kg / H in Example 7 from the high-pressure processing liquid and / or high-temperature / high-pressure processing liquid vapor inlet 45. 2kg
/ H (accordingly, the supply amount of ethyl alcohol with respect to the raw material: 30% by weight), and adjusting the pressure regulating valve 3 to adjust the internal gas phase pressure from 8 to 8 in Example 7.
19-21 kg / cm ² G instead of 10 kg / cm ² G
, Dried pellets were produced in the same manner as in Example 7, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 4 shows the measurement results of the surface smoothness and the mechanical properties.

EXAMPLE 28 Methyl alcohol was used instead of water at a rate of 7.2 kg / H in Example 7 from the high pressure processing liquid and / or high temperature / high pressure processing liquid vapor inlet 45. 2kg
/ H (accordingly, the supply amount of methyl alcohol to the raw material: 30% by weight), and adjusting the pressure control valve 3 to adjust the internal gas phase pressure from 8 to 8 in Example 7.
25 to 27 kg / cm ² G instead of 10 kg / cm ² G
, Dried pellets were produced in the same manner as in Example 7, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 4 shows the measurement results of the surface smoothness and the mechanical properties.

Example 29 A high-pressure processing liquid and / or a high-temperature and high-pressure processing liquid vapor injection port 45 was changed to water of 9.6 kg / H, and a solution having a weight ratio of ethyl alcohol to water of 1: 1 was changed to 7. .2 kg / H (accordingly, the supply amount of a mixed solution of ethyl alcohol and water with respect to the raw material: 30% by weight);
The cylinder set temperature was changed to 220 ° C. for each of the melting zone 422, the contact zone 424, the devolatilizing zone 425, and the pressure increasing zone 426 in the cylinder 41,
° C, and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 18 to ² kg.
Dry pellets were produced in the same manner as in Example 1 except that the pellets were kept at 0 kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 4 shows the measurement results of the surface smoothness and the mechanical properties.

Example 30 A high-pressure processing liquid and / or a high-temperature and high-pressure processing liquid vapor injection port 45 was changed to water of 9.6 kg / H, and a solution having a weight ratio of methyl alcohol to water of 1: 1 was changed to 7%. .2 kg / H (therefore, the supply amount of the mixed solution of methyl alcohol and water to the raw material: 30% by weight);
The cylinder set temperature was changed to 220 ° C. for each of the melting zone 422, the contact zone 424, the devolatilizing zone 425, and the pressure increasing zone 426 in the cylinder 41,
° C and adjusting the pressure regulating valve 3 to change the internal gas phase pressure to 20 to 23 kg / cm ² G to 23 to ² kg.
Dry pellets were produced in the same manner as in Example 1 except that the pellets were kept at 5 kg / cm ² G, and the surface smoothness and mechanical properties (brittle temperature) of the pellets were measured. Table 4 shows the measurement results of the surface smoothness and the mechanical properties.

[0092]

[Table 4]

[0093]

As described above in detail, in the method for regenerating the resin with foamed polyurethane of the present invention, the molten resin is melted in an extruder with or without a pressure adjusting mechanism, particularly in a twin-screw extruder. The resin with foamed polyurethane is brought into contact with a high-temperature, high-pressure treatment liquid and / or a treatment liquid vapor under a certain temperature and pressure condition to decompose and miniaturize the foamed polyurethane, uniformly and finely disperse it in the resin, and from an extruder. Because of the extrusion, the foamed polyurethane is peeled off from the resin to which the foamed polyurethane has been bonded. In addition to solving problems such as badness, the processing conditions and processing steps are simple and continuous and stable. It is possible to reproduce the fat. When an instrument panel is manufactured using the regenerated product thus obtained, the appearance (surface smoothness) of the virgin material is improved.
And the decrease in physical properties is extremely small.

[Brief description of the drawings]

FIG. 1 is a schematic flow chart showing a preferred embodiment of a method for continuously regenerating a resin with a foamed polyurethane according to the present invention.

[Explanation of symbols]

DESCRIPTION OF SYMBOLS 1 Tank 2 Metering pump 3 Pressure control valve 4 Twin screw type extruder 41 Cylinder 42 Screw 43 Resin supply port with foamed polyurethane 44 Regenerated resin discharge port 45 High-pressure processing liquid and / or high-temperature / high-pressure processing liquid vapor inlet 46 Processing liquid vapor discharge hole 47 Exhaust port 48 Heat transfer device 420 Space 421 Solid transport zone 422 Melting zone 423 Melt transport zone 424 Contact zone 425 Volatilization zone 426 Boosting zone 427 Surface renewal portion 428 Molten resin filling area 429 Molten resin Area 430 vapor pressure holding area

Claims (4)

(57) [Claims] In an extruder, a resin with foamed polyurethane is brought into contact with a high-temperature and high-pressure treatment liquid and / or a treatment liquid vapor in a molten state, and the polyurethane foam is finely dispersed in the molten resin to form the foamed polyurethane. When regenerating the resin with polyurethane, (1) water and / or hydrophilic alcohol, or (b) an aliphatic saturated monohydric alcohol having 4 to 10 carbon atoms and 5 or more carbon atoms, (2) using at least one kind of hydrophobic alcohol selected from the group consisting of alicyclic monohydric alcohols and aromatic monohydric alcohols having 7 or more carbon atoms and having a melting point of 50 ° C. or less; The supply amount of the high-pressure processing liquid and / or the processing liquid vapor is at least 0.02 kg / H or more per 1 kg / H of the foamed polyurethane resin to be processed. , And (3) when water is used for the as the treatment liquid (a),
A method for continuously regenerating a resin with a foamed polyurethane, wherein the temperature of the contact treatment between the resin with a foamed polyurethane and the treatment liquid is at least 180 ° C. or higher. 2. A pressure adjusting mechanism is provided in a contact zone between the resin with foamed polyurethane and the high-temperature and high-pressure treatment liquid and / or the vapor of the treatment liquid in an extruder, and the foamed polyurethane is kept under constant temperature and pressure conditions. 2. The method for continuously regenerating a resin with foamed polyurethane according to claim 1, wherein the resin is decomposed and finely dispersed in a molten resin. 3. An extruder comprising: (a) a resin supply port with foamed polyurethane, (b) a solid transport zone, (c) a melting zone, (d) a melt transport zone, and (e) a recycled resin discharge port ( Die), and at least one inlet and at least one outlet for high-pressure processing liquid and / or processing liquid vapor at a point of the cylinder which is to be (c) a melting zone and / or (d) a melt transport zone. ), And a discharge hole for the processing liquid vapor and a pipe connected thereto are provided at an intermediate portion between the inlet and the exhaust port of the cylinder, or a discharge hole for the processing liquid vapor and the pipe connected thereto. A pressure adjusting mechanism including a pipe and a pressure adjusting valve provided in the pipe, and an upstream side of the injection port of the cylinder (a resin supply port with foamed polyurethane). And a seal made of a molten resin for enclosing the processing liquid and / or the processing liquid vapor which has been injected into a high-temperature and high-pressure state at a location between the discharge hole of the processing liquid vapor and the exhaust port of the cylinder. Part, and between the seal parts,
3. The method for continuously regenerating a resin with foamed polyurethane according to claim 1, wherein the extruder is a twin-screw extruder provided with a screw having a shape mainly performing kneading. 4. The method for continuously regenerating a foamed polyurethane resin according to claim 1, wherein the foamed polyurethane resin is a crushed product of an instrument panel of an automobile.