JPH09302043A - Production of silane-modified polyolefin - Google Patents

Abstract

PROBLEM TO BE SOLVED: To achieve a homogeneous graft reaction to thereby prevent the variation in cross-link density by adding a radical polymerization inhibitor to a lip. mixture in the grafting of a vinylsilane compd. onto a polyolefin. SOLUTION: Di-t-butyl peroxide as a free-radical initiator is dissolved in vinyltrimethoxysilane, i.e. a vinylsilane compd. represented by the formula: RSiR'Y3-n (where R is alkenyl or alkenyloxy; R' is H or alkyl; Y is a hydrolyzable org. group; and n is 0, 1, or 2), giving a liq. compsn. High-density polyethylene is fed into a hopper 3 and then into an extruder with a screw feeder 5 at a feed rate of about 30kg/hr. The temps. of each of barrel sections and a sheet-forming die 2 are about 170 deg.C. While the liq. compsn. is injected into the extruder under a pressure of 50kg/cm<2> through a liq. injection port 4 installed at the former part at an injection rate of 330g/hr with a plunger pump 7, a resin compsn. is melt kneaded and extruded into a sheet 11, thus giving an objective product.

Description

Detailed Description of the Invention

[0001]

TECHNICAL FIELD The present invention relates to a method for producing a silane-modified polyolefin.

[0002]

2. Description of the Related Art Silane-modified polyolefin undergoes a cross-linking reaction when it comes into contact with water, and has various properties such as mechanical strength, heat resistance, creep resistance, environmental stress crack resistance, chemical resistance, etc. Since it is dramatically improved in comparison, it is preferably used as a raw material for covered electric wires, hot water supply pipes, flame-retardant materials and the like.

A method of grafting a silicone derivative onto a polyolefin by a radical reaction using an extruder which has been conventionally used for molding plastics is a known technique as a method for producing a silane-modified polyolefin, and is widely practiced today. There is.

At the beginning of the development of this technology, a solid phase polyolefin was obtained by adding a vinyl silane compound such as vinyltrimethoxysilane and a radical initiator such as an organic peroxide, mixing and stirring the mixture, and diffusing it for a certain period of time. The so-called Dow method, in which the composition is charged into an extruder to complete the graft reaction, has been the mainstream.

However, this method has a problem in that an unstable phenomenon such as a change in the composition ratio due to the release of silane from the resin in the hopper, and further, a poor bite of the material due to the adhesion of silane to the inner surface of the cylinder below the hopper occurs.

To solve this problem, Japanese Examined Patent Publication No. 52-29338
In the gazette, a method for obtaining a silane-modified polyolefin by providing a liquid injection hole in a cylinder in a region after a melting region of a polyolefin in a screw extruder and press-mixing a mixed liquid of a vinylsilane compound and a radical initiator through the injection hole is disclosed. Has been done. Further, in the above method,
A so-called one-step process of injecting a silanol condensation catalyst in the middle and second-stage region of the extruder for the purpose of shortening the hot water treatment time and discharging the obtained resin composition at once from a molding die connected to the tip to obtain a shaped product The molding method has advantages such as process simplification,
It is preferably used.

However, according to this method, since the plasticized resin is at a high temperature, decomposition of the radical initiator begins at the moment when the mixed solution of the vinylsilane compound and the radical initiator is injected and comes into contact with the polyolefin. The grafting reaction starts before the vinylsilane compound is uniformly kneaded with the polyolefin. Therefore, in the obtained silane-modified polyolefin, the graft of the silane compound becomes unevenly distributed and becomes non-uniform. As a result, the locally grafted portion has poor compatibility with the surrounding portion,
Appeared as a so-called scorch on the surface of the discharged resin composition, not only worsening the appearance of the molded product after shaping, but also the fusion property with the peripheral portion is lowered and cracks or breakage easily occur in the molded product. There is a problem such as becoming. Further, since the cross-linking density varies due to the non-uniform grafting of the vinyl silane compound, it is unavoidable that the resulting molded article is stretched and the mechanical strength such as tensile strength is lowered.

[0008]

SUMMARY OF THE INVENTION The object of the present invention is to solve the above-mentioned problems of the prior art, in which a polyolefin is charged from an hopper into an extruder, and a vinylsilane compound and a radical initiator are introduced into the extruder in the downstream of the hopper. It is an object of the present invention to provide a method which makes it possible to uniformly carry out the graft reaction when a vinylsilane compound is grafted onto a polyolefin by injecting the mixed solution of

[0009]

In the method for producing a silane-modified polyolefin of the present invention 1 (the invention according to claim 1), a polyolefin is charged into an extruder from a hopper, and a vinylsilane compound is fed to the extruder in the downstream of the hopper. This is a method in which a radical-initiated polymerization inhibitor is added to the mixed solution when a vinylsilane compound is grafted onto the polyolefin by injecting a mixed solution of the radical initiator and the radical initiator.

The polyolefin used in the present invention 1 is
It is a (co) polymer of an olefinic monomer and is not particularly limited, and examples thereof include low density polyethylene,
High-density polyethylene, polyethylene such as linear low-density polyethylene, polypropylene, ethylene-propylene copolymer, ethylene-propylene-diene terpolymer, ethylene-butene copolymer, ethylene-vinyl acetate copolymer, ethylene -(Meth) acrylic acid ester copolymers, chlorinated polyethylene, etc. may be mentioned.
One kind or two or more kinds is preferably used, and among them, one kind or two or more kinds such as polyethylene and polypropylene such as low density polyethylene, high density polyethylene, linear low density polyethylene and the like is more preferably used. still,
The “(co) polymer” referred to herein means a “polymer” or a “copolymer”.

The vinylsilane compound used in the present invention 1 is represented by the following general formula (I).

RSiR 'n Y3-n (I)

In the formula (I), R is an alkenyl group or an alkenyloxy group, R'is a hydrogen atom or an alkyl group, Y is a hydrolyzable organic group, and n is 0, 1 or 2.

Examples of the alkenyl group represented by R include a vinyl group, an allyl group, an isopropenyl group, a butenyl group, a cyclohexenyl group and a cyclopentadienyl group. Further, examples of the alkenyloxy group represented by R include a vinyloxy group and an allyloxy group.

Examples of the hydrolyzable organic group Y include, for example, methoxy group, ethoxy group, formyloxy group, acetoxy group, propionyloxy group, alkylamino group,
Examples thereof include an arylamino group. When n is 0 or 1, a plurality of Y may be the same or different.

Further, examples of the alkyl group represented by R'include a methyl group, an ethyl group, a propyl group and a decyl group. When n is 2, a plurality of R's may be the same or different.

Specific examples of the vinylsilane compound represented by the above general formula (I) include vinyltrimethoxysilane, vinyltriethoxysilane and vinyltriacetoxysilane when n = 0, vinyldimethoxymethylsilane when n = 1, Examples include vinyldiethoxymethylsilane, and when n = 2, vinylmethoxydimethylsilane, vinylethoxydimethylsilane and the like. These are preferably used alone or in combination of two or more.

The amount of the above-mentioned vinylsilane compound used is not particularly limited, but if it is too small, the gel fraction of the finally obtained water-crosslinked polyolefin will not be sufficiently high and the mechanical strength, heat resistance and creep resistance will be low. Properties such as properties are not sufficiently improved. On the other hand, if the amount used is too large, the melt viscosity of the silane-modified polyolefin becomes too high, the extruder is overloaded and the workability is deteriorated, and the elongation rate and heat fusion property are deteriorated. In addition to significantly deteriorating the properties, the vinylsilane compound is more likely to remain in the system as an unreacted material. Therefore, the amount of the vinylsilane compound used is preferably 0.5 to 10 parts by weight, more preferably 0.7 to 10 parts by weight, based on 100 parts by weight of the polyolefin.
5 parts by weight.

The radical initiator used in the present invention 1 is
Any compound generally used in the graft reaction of polyolefin may be used, and examples thereof include benzoyl peroxide, 2,4-dichlorobenzoyl peroxide,
t-butylperoxyacetate, t-butylperoxybenzoate, dicumyl peroxide, 2,5-dimethyl-2,5-di (t-butylperoxy) hexane, di-t-butylperoxide, 2,5 Examples include organic peroxides such as dimethyl-2,5-di (t-butylperoxy) hexyne-3 and azo compounds such as azobisisobutyronitrile and dimethylazodiisobutyrate. These may be used alone or in combination of two or more. Among them, dicumyl peroxide,
2,5-dimethyl-2,5-di (t-butylperoxy) hexane, di-t-butyl peroxide, 2,5
One or more kinds of -dimethyl-2,5-di (t-butylperoxy) hexyne-3 and the like are more preferably used.

The amount of the radical initiator used is not particularly limited, but is preferably 0.01 to 5 parts by weight, more preferably 0.02 to 2 parts by weight, based on 100 parts by weight of the polyolefin. is there.

If the amount of radical initiator used is too small,
The desired gel fraction cannot be obtained because the grafting reaction does not proceed sufficiently, and conversely, if it is too large, the free radical sites in the polyolefin become too large, and so-called peroxide crosslinking proceeds, so the scorch phenomenon (premature crosslinking Object), decrease in surface smoothness, abnormal increase in viscosity, etc.
Workability deteriorates.

The radical polymerization inhibitor used in the present invention 1 is not particularly limited as long as it inhibits or strongly suppresses the radical chain polymerization reaction, but it has an action other than the radical chain inhibition action (for example, promotion of decomposition of the radical initiator). It is necessary to exert no effect), and in general, phenol-based and quinone-based radical polymerization inhibitors, antioxidants and the like are used. Specific examples include p-benzoquinone, 2,5-diphenyl-p-benzoquinone, hydroquinone, pt-butylcatechol, 2,5-di-t-butylhydroquinone, mono-t-butylhydroquinone,
2,5-di-t-amylhydroquinone, 2,6-di-t
-Butyl-p-cresol, hydroquinone monomethyl ether, 2-t-butyl-4-methoxyphenol, 3
-T-butyl 4-methoxyphenol, 2,6-di-t
-Butyl-4-ethylphenol, stearyl-β-
(3,5-di-t-butyl-4-hydroxyphenyl)
Propionate, 2,2'-methylenebis (4-methyl-6-t-butylphenol), 2,2'-methylenebis (4-ethyl-6-t-butylphenol), 4,
4'-thiobis (3-methyl-6-t-butylphenol), 4,4'-butylidenebis (3-methyl-6-t)
-Butylphenol), 3,9-bis [1,1-dimethyl-2- [β- (3-t-butyl-4-hydroxy-5
-Methylphenyl) propionyloxy] ethyl] 2,
4,8,10-Tetraoxaspiro [5,5] undecane, 1,1,3-tris (2-methyl-4hydroxy-)
5-t-butylphenyl) butane, 1,3,5-trimethyl-2,4,6-tris (3,5-di-t-butyl-
4-hydroxybenzyl) benzene, tetrakis- [methylene-3- (3 ', 5'-di-t-butyl-4'-hydroxyphenyl) propionate] methane, bis [3,3'-bis- (4'hydroxy) -3'-t-butylphenyl) butyric acid] glycol ester and the like. These may be used alone or in combination of two or more. Among them, p-benzoquinone, hydroquinone, 2,5-di-t-butylhydroquinone, mono-t-butylhydroquinone, 2,6-
Di-t-butyl-p-cresol, hydroquinone monomethyl ether, 2-t-butyl-4-methoxyphenol, 3-t-butyl 4-methoxyphenol, 2,6-
One or more of di-t-butyl-4-ethylphenol and the like are more preferably used.

The amount of the radical polymerization inhibitor used is not particularly limited, but the polyolefin 100 may be used.
With respect to parts by weight, preferably 0.001 to 0.5 parts by weight,
It is more preferably 0.005 to 0.2 parts by weight.

If the amount of radical polymerization inhibitor used is too small, the effect of suppressing the grafting reaction immediately after injection into the extruder is insufficient, and the graft reaction proceeds before the vinylsilane is uniformly dispersed. On the other hand, if the amount is too large, the time for suppressing the grafting reaction in the extruder becomes long and the desired graft reaction amount cannot be obtained.

The radical polymerization inhibitor is preferably sent in a state of being dissolved in the reaction solution. The above radical polymerization inhibitor is easily dissolved in the vinylsilane compound and there is no particular problem. However, if it is difficult to dissolve it, it may be dissolved in an organic solvent such as acetone, methanol or ethyl acetate in advance and then added to the reaction solution and dispersed therein.

In the modified polyolefin, if necessary, a silanol condensation catalyst, a process heat stabilizer, other antioxidants and ultraviolet absorbers, organic and inorganic fillers, pigments, One or more of various additives such as dyes and processing aids may be contained.

In the method for producing a silane-modified polyolefin according to the second aspect of the present invention (the invention according to claim 2), a polyolefin is charged from an hopper into an extruder, and a vinylsilane compound and a radical initiator are mixed into the extruder in the downstream of the hopper. When the liquid is injected and the vinylsilane compound is grafted to the polyolefin, the same as in the present invention 1 except that the mixed solution is diluted with an organic solvent instead of the radical polymerization inhibitor and then injected.

The above-mentioned organic solvent is not particularly limited as long as it is compatible with the mixed solution of the vinylsilane compound and the radical initiator and does not inhibit the radical reaction, but an inexpensive solvent having a low boiling point and easily recovered is preferably used. . As a specific example,
Methyl alcohol, ethyl alcohol, isopropyl alcohol, benzene, toluene, xylene, acetone,
Ethyl acetate, ethylene glycol monomethyl ether,
Tetrahydrofuran and the like may be used, and these may be used alone or in combination of two or more kinds.

If the amount of the organic solvent used is too small, the vinylsilane compound and the radical initiator will be insufficiently diluted, so that a high concentration of the vinylsilane compound and the radical initiator will be mixed in the extruder, and the graft reaction will not be uniform. If it is too much, not only the recovery efficiency will deteriorate, but it may also remain in the product.
It is preferably 0.1 to 10 parts by weight, and more preferably 0.2 to 5 parts by weight, based on parts by weight.

The extruder used in the production method of the present invention is
It is an extruder generally used for plastic molding, and is not particularly limited, but a single screw extruder, a twin screw extruder, a multi-screw extruder having three or more screws, etc. And any of them is preferably used.

As the above single-screw extruder, in addition to a general full flight type screw, an extruder equipped with a discontinuous flight type screw, a pin barrel, a mixing head and the like can be used. As the twin-screw extruder, a meshing co-rotating extruder, a meshing counter-rotating extruder, a non-meshing counter-rotating extruder, or the like can be preferably used.

Among the various screw type extruders mentioned above,
Considering the kneading performance and the like, a meshing (self-wiping) co-rotating twin-screw extruder is more preferably used. The screw shape of the extruder is preferably a two- or three-thread type full-flight type, which partially has screw elements such as a kneading disc, a seal ring, a reverse screw, and a rotor. obtain. Further, providing a vacuum vent in the extruder is effective for removing unnecessary substances such as water, residual monomers, and initiator residues.

The polyolefin is usually charged from the hopper of the extruder. In addition, in order to increase quantitativeness, a screw type feeder, a weight control type feeder or the like may be provided.

The introduced polyolefin is melted by heat transfer from the cylinder barrel in the plasticizing region while being transferred to the downstream by screw rotation. After this plasticizing region, the polyolefin becomes a melt and is further transferred to the downstream.

The mixed solution of the vinyl silane compound and the radical initiator is supplied to the extruder through a liquid injection hole provided after the plasticizing section.

The liquid injection hole may be provided in either the cylinder barrel portion or the screw portion, but it is generally easy to design and generally provided in the cylinder barrel portion.

The mixed solution of the vinylsilane compound, the radical initiator, the radical polymerization inhibitor or the organic solvent is preferably sent by a pressure-feeding pump such as a plunger pump.

(Function) According to the production method of the present invention 1, since the radical polymerization inhibitor is added to the mixed solution comprising the vinylsilane compound and the radical initiator, the graft reaction is started before the vinylsilane is sufficiently dispersed. Can be prevented. In the downstream region after the action of the radical polymerization inhibitor has weakened, vinyl silane has already been sufficiently dispersed, so the radical initiator whose resin temperature has risen due to shearing heat generation and heating from the cylinder acts on the polyolefin, resulting in uniform distribution. It is possible to perform various graft reactions. According to the production method of the present invention 2, the mixed solution of the vinylsilane compound and the radical initiator is in a state of being diluted with the organic solvent, and the vinylsilane compound and the radical initiator are added to the molten resin immediately after being injected into the extruder. It becomes possible to disperse and carry out a uniform graft reaction.

[0039]

BEST MODE FOR CARRYING OUT THE INVENTION Next, the method for producing a silane-modified polyolefin of the present invention will be specifically described with reference to the drawings.

The extruder (1) shown in FIG. 1 is a screw (diameter 47 m) composed of a self-wiping type double-thread screw element and a kneading disc element.
m, L / D = 45) and a cylinder barrel divided into 12 parts, and is a meshing type co-rotating twin screw extruder (model “TEX-44”, manufactured by Japan Steel Works).
At the tip of this extruder (1), width 200mm, thickness 5mm
The sheet forming dies (2) are connected. In addition, the above 12
The divided cylinder barrel is composed of a first barrel section to a twelfth barrel section arranged in the extrusion direction,
The fifth barrel section is provided with a front stage liquid injection hole (4), and the tenth barrel section is provided with a rear stage liquid injection hole (6).

In FIG. 1, (3) is a hopper, (5) is a screw feeder, (7) and (8) are plunger pumps for liquid delivery, (9) is a vinylsilane compound and a radical initiator, and a radical polymerization inhibitor. Or a mixed solution tank with an organic solvent,
(10) is a silanol condensation catalyst tank, and (11) is a silane-modified polyolefin sheet molding.

Next, a method for producing a silane-modified polyolefin using the extruder having the above construction will be described.

[0043]

【Example】

Example 1 First, 800 g of di-t-butyl peroxide and 200 g of hydroquinone as a radical initiator were added to 10 kg of vinyltrimethoxysilane, which is a vinylsilane compound, and dissolved to prepare a liquid composition (A).

High density polyethylene (trade name "HIZEX 2200J", manufactured by Mitsui Petrochemical Co., Ltd.) in the hopper (3)
, And use the screw feeder (5) for 30K
It was supplied into the extruder through the supply port at a supply rate of g / hour.
Further, the temperature of each barrel section and the sheet forming die (2) is 170 ° C. in the first barrel section to the fourth barrel section and the fifth barrel section.
The barrel section to the twelfth barrel section are set to 170 ° C, and the sheet forming die (2) is set to 170 ° C.

The above liquid composition (A) was injected into the extruder at a pressure of 50 kg / cm ² using the plunger pump (7) from the liquid injection hole (4) in the previous stage at a supply rate of 330 g / hour. . After the resin composition was melt-kneaded in the extruder, a silane-modified polyethylene sheet molding (11) was discharged from the sheet die discharge port to obtain a product.

Example 2 Vinyltrimethoxysilane 10 was used as the liquid composition (B).
1.2 kg of 2,5-dimethyl-2,5-di (t-butylperoxy) hexane and 0.1 kg of hydroquinone monomethyl ether were added to and dissolved in kg.
In addition, the temperature of each barrel section and the sheet forming die (2) was set to 170 ° C in the first barrel section to the fourth barrel section,
Example 1 except that the temperature was set at 170 ° C in the barrel section to the 12th barrel section and 180 ° C in the sheet forming die (2), and the liquid composition (B) was injected into the extruder at a supply rate of 339 g / hour. It was similar.

Example 3 Vinyltrimethoxysilane 10 was used as the liquid composition (C).
1.2 kg of 2,5-dimethyl-2,5-di (t-butylperoxy) hexane and 0.3 kg of 2,6-di-t-butyl-p-cresol were added to and dissolved in kg. The temperature of each barrel section and pipe forming die is 170 ° C. in the first to fourth barrel sections, 150 ° C. in the fifth to twelfth barrel sections, and 170 in the pipe forming die (2). It was set to ° C.

High density polyethylene (trade name "Hi-Zex 2200J", manufactured by Mitsui Petrochemical Co., Ltd.) in the hopper (3)
20 k using the screw feeder (5).
The extruder was fed through the feed port at a feeding rate of g / hour.
At the same time, the liquid composition (C) was added to 2 by using a micro pump.
The extruder was fed through the same feed port as above at a feed rate of 30 g / hour. Further, using a plunger pump (8) from the liquid injection hole (6) in the latter stage, a di-n-butyltin dilaurate (manufactured by Wako Pure Chemical Industries, Ltd.) was used as a silanol condensation catalyst.
It was fed to the extruder through a press-fit nozzle at a feed rate of g / hour. During this period, the extruder was operated at a screw rotation speed of 40 rpm, and the silane-modified polyethylene pipe molding (11) was discharged from the pipe die discharge port to obtain a product. Others are the same as in the first embodiment.

Example 4 15 kg of acetone and 10 kg of vinyltrimethoxysilane
And 800 g of di-t-butyl peroxide were added and dissolved to prepare a liquid composition (D).

High density polyethylene (trade name "Hi-Zex 2200J", manufactured by Mitsui Petrochemical Co., Ltd.) in the hopper (3)
, And use the screw feeder (5) for 30K
It was supplied into the extruder through the supply port at a supply rate of g / hour.
Further, the temperature of each barrel section and the sheet forming die (2) is 170 ° C. in the first barrel section to the fourth barrel section and the fifth barrel section.
The barrel section to the 12th barrel section were set at 170 ° C, and the sheet forming die (2) was set at 180 ° C.

The liquid composition (D) was supplied at a rate of 774 g / hour through the liquid injection hole (4) in the preceding stage, a vent hole (not shown) was provided in the ninth barrel, and the solvent was recovered by a vacuum pump. In the same manner as in Example 1, the silane-modified polyethylene molded body (11) was discharged to obtain a product. Example 5 10 kg of acetone and 10 kg of vinyltrimethoxysilane
And 2,5-dimethyl-2,5 di (t-butylperoxy) hexane (1.2 kg) were added and dissolved to obtain a liquid composition.
Prepared (E).

High density polyethylene (trade name "Hi-Zex 2200J", manufactured by Mitsui Petrochemical Co., Ltd.) in the hopper (3)
, And use the screw feeder (5) for 30K
It was supplied into the extruder through the supply port at a supply rate of g / hour.
Further, the temperature of each barrel section and the sheet forming die (2) is 170 ° C. in the first barrel section to the fourth barrel section and the fifth barrel section.
The barrel section to the 12th barrel section were set at 150 ° C, and the sheet forming die (2) was set at 190 ° C.

Example 4 except that the liquid composition (E) was fed through the liquid injection hole (4) in the preceding stage at a rate of 636 g / hour.
A molded product (11) of silane-modified polyethylene was discharged in the same manner as in 1. to obtain a product.

Example 6 Vinyltrimethoxysilane 10 k in 15 kg of ethyl acetate
g and 2,5-dimethyl-2,5 di (t-butylperoxy) hexane 1.2 kg, 2,6-di-t-butyl-p
-Using a solution prepared by adding 0.3 kg of cresol,
A liquid composition (F) was prepared. In addition, the temperature of each barrel section and the pipe forming die is 170 ° C in the first barrel section to the fourth barrel section, 150 ° C in the fifth barrel section to the 12th barrel section, and 170 ° C in the pipe forming die (2). Set.

High-density polyethylene (trade name "Hi-Zex 2200J", manufactured by Mitsui Petrochemical Co., Ltd.) in the hopper (3)
20 k using the screw feeder (5).
The extruder was fed through the feed port at a feeding rate of g / hour.
At the same time, the liquid composition (F) 2
The extruder was fed through the same feed port as above at a feed rate of 30 g / hour. Further, using a plunger pump (8) from the liquid injection hole (6) in the latter stage, a di-n-butyltin dilaurate (manufactured by Wako Pure Chemical Industries, Ltd.) was used as a silanol condensation catalyst.
It was fed to the extruder through a press-fit nozzle at a feed rate of g / hour. During this period, the extruder was operated at a screw rotation speed of 40 rpm, and the silane-modified polyethylene pipe molding (11) was discharged from the pipe die discharge port to obtain a product.

Comparative Example 1 Vinyltrimethoxysilane 10 was used as the liquid composition (G).
The liquid composition (G) was used in an amount of 324 g / g by dissolving 0.8 kg of di-t-butylperoxide in the solution.
A silane-modified polyethylene molded body (11) was discharged in the same manner as in Example 1 except that the product was supplied at a supply rate of time to obtain a product.

Occurrence of scorch of the obtained product was visually evaluated. Regarding the evaluation criteria for the occurrence of scorch, excellent ... no scorch was observed, good ... almost no scorch was observed, no ... scorch was generated and appearance was poor.

Further, the above product was subjected to 1
After 2 hours of treatment, the water-crosslinking process is completed, followed by JIS
The gel fraction was calculated based on K 6769.

The evaluation results are shown in Table 1.

[0060]

[Table 1]

[0061]

According to the production method of the present invention, since the graft reaction starts after the vinylsilane compound is uniformly dispersed in the polyolefin resin, the appearance reaction such as scorch does not occur even if the graft reaction occurs sufficiently.
A silane-modified polyolefin molded product can be produced.

[Brief description of drawings]

FIG. 1 is a schematic view showing an example of an extruder.

[Explanation of Codes] 1: Twin-screw extruder 2: Molding die 3: Hopper 4: Front liquid injection hole 5: Screw feeder 6: Rear liquid injection hole 7: Liquid feed pump 8: Liquid feed pump 9: Vinylsilane Mixture tank of compound and radical initiator 10: Silanol condensation catalyst tank 11: Silane-modified polyolefin molding

Claims (2)

[Claims] 1. When a polyolefin is charged into an extruder from a hopper and a mixed solution of a vinyl silane compound and a radical initiator is injected into the extruder in the downstream of the hopper to graft the vinyl silane compound onto the polyolefin, the mixed solution is added to the mixed solution. A method for producing a silane-modified polyolefin, which comprises adding a radical-initiated polymerization inhibitor. 2. When a polyolefin is charged into an extruder from a hopper and a mixed solution of a vinyl silane compound and a radical initiator is injected into the extruder in the downstream of the hopper to graft the vinyl silane compound onto the polyolefin, the mixed solution is mixed. A method for producing a silane-modified polyolefin, which comprises diluting with an organic solvent and injecting.