JPH05255444A - Production of ethylene copolymer - Google Patents

Abstract

PURPOSE:To make reaction stable for a long period of time in copolymerizing ethylene with an alpha-olefin by fluidized bed vapor-phase copolymerization and to obtain the subject copolymer having excellent physical properties by using a new catalyst. CONSTITUTION:First, a porous inorganic oxide (preferably silica) is successively brought into contact with (A) a reaction product of an aluminum halide (preferably AlCl3) and an organosilicon (preferably methyltriethoxysilane) of formula I (R<1> is 1-8C alkyl or phenyl; R<2> is 1-8C alkyl; (m) is 0-3), (B) a Grignard compound of the formula R<3>MgX<1> (R<3> is R<2>; X<1> is halogen) (preferably one wherein X<1> is Cl), (C) a Ti compound (preferably tetrachlorotitanium) of formula II (R<4> is R<1>; X<2> is X<1>; (n) is 0-4) and (D) an organometallic compound (preferably trialkylaluminum) to give a solid catalytic component. Then in the presence of a catalyst consisting of the catalytic component and an organoaluminum compound, ethylene is copolymerized with an alpha-olefin.

Description

Detailed Description of the Invention

[0001]

FIELD OF THE INVENTION The present invention relates to a method for producing a copolymer of ethylene and α-olefin.

[0002]

2. Description of the Related Art Copolymerization of ethylene and .alpha.-olefin using a Ziegler-Natta type catalyst has hitherto been produced by a polymerization method such as solution polymerization, bulk polymerization, slurry polymerization and gas phase polymerization. In recent years, a process that does not require a step of separating a catalyst residue from a copolymer produced by increasing the catalyst activity has become widespread, and an inorganic solid is used for the purpose of preparing catalyst particles having high catalyst activation and good fluidity. Furthermore, many highly active catalysts in which a transition metal component such as titanium or vanadium is supported on an inorganic solid having a specific particle size have been proposed. Japanese Patent Publication No. 54-129983,
JP-A-58-17206, JP-A-59-49242 and JP-B-2-33045 disclose supported high-activity catalysts for copolymerization of ethylene and α-olefins to which the present invention relates. ..

When a copolymer of ethylene and α-olefin is produced by fluidized bed gas phase polymerization, the temperature in the fluidized bed is destabilized due to local accumulation of heat of polymerization, and a large lump polymer is formed. It is known that the fluid state is difficult to maintain. Therefore, for example, Japanese Examined Patent Publication No. 52-40350,
In JP-A-52-45749, JP-A-60-53044, and JP-A-59-30806, a prepolymer is prepared in advance, and the prepolymer is used in a fluidized bed polymerization reactor so that the weight per transition metal can be increased. Increase the amount of coalescence,
Also disclosed is a method for preventing rapid heat generation and particle agglomeration in the solid catalyst portion immediately after introduction into the fluidized bed polymerization reactor.

In this case, the particle shape of the polymer is likely to be a replica of the particle shape of the catalyst, and in order to efficiently and stably produce the polymer, the catalyst solid and the prepolymer used in the fluidized bed polymerization reaction are used. Control of particle shape, i.e.
It is important to form the catalyst solids and prepolymers that remain spherical. JP-A-55-94909 and 58-1
79209, 61-87703, 55-115.
For example, publications such as 405 and 60-233107 disclose a catalyst solid in which a transition metal compound is supported on an inorganic oxide such as silica for the purpose of producing a spherical polymer.

Further, since a low molecular weight component having an adhesive property is produced and the fluidity of the polymer particles is deteriorated, a lump of the polymer may be produced or the reaction tube may be clogged. In addition, if the randomness of the α-olefin in the copolymer is poor, that is, if the distribution of the α-olefin units is biased, a tacky copolymer is produced and the same problems as described above occur. Therefore, a stable copolymerization reaction for a long period of time cannot be performed.

Generally, in the case of a copolymer of ethylene and α-olefin, it is possible to produce a lower density copolymer by increasing the content of α-olefin. However, a low molecular weight component is generated in the polymerization reaction, or the composition distribution of α-olefin in the copolymer becomes wide, that is, if the composition between polymer chains is nonuniform, the surface of the molded film has tackiness. There is a problem.

In the copolymerization of ethylene and α-olefin, in order to solve the above problems, in particular, to narrow the composition distribution and suppress the formation of low molecular weight components, Zr
System catalysts (Japanese Patent Laid-Open Nos. 62-121707 and 62-121)
709, JP-A-3-234712, and JP-A-3-2233.
No. 06, No. 3-217404), or the use of an electron donor in a magnesium compound-supported catalyst (JP-A-61-61).
-271309, 61-217310, 63-
159411, 63-14008, 63-1
17019, Japanese Patent Publication No. 1-49296) and the like. However, the conventional techniques are not always satisfactory in terms of production and physical properties of the above-mentioned copolymer, and further improvement is desired.

[0008]

DISCLOSURE OF THE INVENTION The present invention improves the problems in the process for producing a copolymer of ethylene and an α-olefin, and particularly in the case of producing by a fluidized bed gas phase polymerization, a long-term stable polymerization reaction. And a method for producing a copolymer having excellent physical properties.

[0009]

[Technical Means for Solving Problems] In the present invention, a porous inorganic oxide is prepared from (1) aluminum halide and formula R ¹
_m Si (OR ² ) _4-m (In the formula, R ¹ represents an alkyl group having 1 to 8 carbon atoms or a phenyl group, and R ² has 1 to 8 carbon atoms.
An alkyl group of 8 and m is 0, 1, 2 or 3),
(2) A Grignard compound represented by the formula R ³ MgX ¹ (wherein R ³ represents an alkyl group having 1 to 8 carbon atoms, and X ¹ represents a halogen atom), and (3) the formula Ti (OR ⁴ ) _n
X ² _4-n (In the formula, R ⁴ represents an alkyl group having 1 to 8 carbon atoms or a phenyl group, X ² represents a halogen atom, n 2
Is a titanium compound represented by 0, 1, 2, 3 or 4), and (4) an organometallic compound, which is a solid catalyst component (A) obtained by sequentially contact-treating, and an organoaluminum compound component. It relates to a method for producing an ethylene copolymer, which comprises copolymerizing ethylene and an α-olefin in the presence of a catalyst obtained from (B).

Hereinafter, each component used in the preparation of the catalyst of the present invention and its conditions will be described in detail. In the present invention, the preparation and polymerization of the catalyst component are all carried out under an atmosphere of an inert gas such as nitrogen or argon. Further, it is desirable that the raw material for preparing the catalyst component is substantially anhydrous.

Examples of the porous inorganic oxide in the present invention include silica, alumina, magnesium oxide, titanium oxide, zirconium oxide and the like. Particularly, silica is preferable. The particle size of the porous inorganic oxide is 10 to 10
A spherical one having a diameter of 0 μm is preferable, and its BET is
Those having a surface area of 10 to 600 m ² / g are preferable. It is preferable that the porous inorganic oxide is substantially anhydrous, and therefore, it can usually be used after heat treatment at 200 to 800 ° C. in an inert gas such as nitrogen gas or under vacuum.

In the present invention, first, the above porous inorganic oxide is subjected to contact treatment with a reaction product of an aluminum halide and an organic silicon compound. Specific examples of the aluminum halide include aluminum chloride, aluminum bromide and aluminum iodide, and aluminum chloride is preferably used.

Specific examples of the organosilicon compound include tetramethoxysilane, tetraethoxysilane and tetra-n.
-Propoxysilane, tetra-n-butoxysilane, tetraisopentoxysilane, tetra-n-hexoxysilane, methyltrimethoxysilane, methyltriethoxysilane, methyltri-n-butoxysilane, methyltriisopentoxysilane, methyltri-n -Hexoxysilane, ethyltriethoxysilane, ethyltriisopropoxysilane, ethyltriisopentoxysilane, n-
Butyltriethoxysilane, isobutyltriethoxysilane, isopentyltriethoxysilane, isopentyltri-n-butoxysilane, dimethyldiethoxysilane, dimethyldi-n-butoxysilane, dimethyldiisopentoxysilane, diethyldiethoxysilane, diethyl Diisopentoxysilane, diisobutyldiisopentoxysilane, di-n-butyldiethoxysilane, diisobutyldiisopentoxysilane, trimethylmethoxysilane, trimethylethoxysilane, trimethylisobutoxysilane, triethylisopropoxysilane, tri-
n-propylethoxysilane, tri-n-butylethoxysilane, triisopentylethoxysilane, phenyltriethoxysilane, phenyltriisobutoxysilane, phenyltriisopentoxysilane, diphenyldiethoxysilane, diphenyldiisopentoxysilane,
Examples thereof include diphenyldioctoxysilane, triphenylmethoxysilane, triphenylethoxysilane, triphenylisopentoxysilane, benzyltriethoxysilane, benzyltributoxysilane and dibenzyldiethoxysilane. Of these, alkylalkoxysilanes such as methyltriethoxysilane are preferably used.

The proportion of aluminum halide used in the reaction between the aluminum halide and the organosilicon compound is
It is preferably 0.1 to 10 mol, and particularly preferably 0.1 to 2 mol, per mol of the organosilicon compound. The reaction is usually carried out by stirring both compounds in an inert organic solvent at a temperature in the range of -50 to 100 ° C for 0.1 to 2 hours. The reaction proceeds exothermically and the reaction product is obtained as a solution in an inert organic solvent.

Examples of the inert organic solvent include aliphatic hydrocarbons such as propane, butane, pentane, hexane, heptane, octane, decane and dodecane, and alicyclic compounds such as cyclopentane, cyclohexane and methylcyclohexane. Hydrocarbons or aromatic hydrocarbons such as toluene, benzene, xylene, etc. may be mentioned. These inert organic solvents can be similarly used in the following steps of preparing the solid catalyst component (A) or the polymerization step.

The reaction product is an inert organic solvent solution,
Subsequently, it is subjected to a contact treatment with the above-mentioned porous inorganic oxide. The temperature of the contact treatment is usually -50 to 100 ° C, preferably -20 to 80 ° C. The treatment time is not particularly limited, but is usually 5 minutes or longer. The solid thus obtained can be subjected to the next treatment as an insoluble organic solvent slurry, but the solid can be separated in advance, washed with an inert organic solvent, dried, and then subjected to the contact treatment with the next Grignard compound. ..

The Grignard compound represented by the formula R ³ MgX ¹ is preferably an alkylmagnesium chloride in which X ¹ is a chlorine atom, and specific examples thereof include methylmagnesium chloride, ethylmagnesium chloride and n-butylmagnesium. Examples thereof include chloride and n-hexyl magnesium chloride. The amount of the Grignard compound used is usually 0.1 to 100 mmol, and particularly preferably 1 to 20 mmol, per gram of the porous inorganic oxide used for the contact treatment. With the Grignard compound, there is no particular limitation on the method of contacting the porous inorganic oxide, for example, in an inert organic solvent slurry or ether solvent slurry of the porous inorganic oxide,
Gradually adding an ether solution of a Grignard compound, or to an ether solution of a Grignard compound,
Porous inorganic oxides can be added. The temperature of the contact treatment is usually −50 to 100 ° C., preferably −20 to 20 ° C.
It is 80 ° C. There is no particular restriction on the processing time,
Usually, it is 5 minutes or more. Specific examples of ethers include diethyl ether, diisopropyl ether, di-n-butyl ether, diisoamyl ether, and cyclic ethers such as tetrahydrofuran.

The solid thus obtained can be subjected to the next treatment as an insoluble organic solvent slurry, but the solid is separated in advance, washed with an inert organic solvent, dried and then subjected to the next contact treatment with a titanium compound. be able to.

Specific examples of titanium compounds include methoxytrichlorotitanium, dimethoxydichlorotitanium, trimethoxychlorotitanium, ethoxytrichlorotitanium, diethoxydichlorotitanium, propoxytrichlorotitanium,
Dipropoxydichlorotitanium, butoxytrichlorotitanium, dibutoxydichlorotitanium, phenoxytrichlorotitanium, diphenoxydichlorotitanium, methoxytribromotitanium, phenoxytribromotitanium, methoxytriiodotitanium, phenoxytriiodotitanium, tetrachlorotitanium, Examples thereof include tetrabromotitanium, tetraiodotitanium, tetramethoxytitanium, tetraethoxytitanium, tetrapropoxytitanium and tetrabutoxytitanium. Two or more kinds of these titanium compounds may be used in combination.

Among them, tetrachlorotitanium, methoxytrichlorotitanium, dimethoxydichlorotitanium, ethoxytrichlorotitanium, diethoxydichlorotitanium, propoxytrichlorotitanium, dipropoxydichlorotitanium,
Butoxytrichlorotitanium, dibutoxydichlorotitanium and tetrabutoxytitanium are preferably used.

The titanium compound is used in an amount of 1 mmol or more, preferably 10 to 100, per gram of the porous inorganic oxide.
It is preferably millimole. The contact treatment between the solid and the titanium compound can be performed by the following method. The solid is treated with 20 to 20% in the presence or absence of an inert organic solvent.
0.5 at a temperature of 200 ° C, preferably 60-140 ° C.
Contact with the titanium compound for ~ 3 hours.

From the mixture containing the treated solid thus obtained, solids are separated by filtration, decantation, etc., dried, or washed with an inert organic solvent as required. As the inert organic solvent, the same one used in the treatment with the titanium compound can be used. The contact treatment with the titanium compound can be continuously performed a plurality of times.

The thus obtained contact-treated solid of the carrier and the titanium compound can be subjected to the following contact treatment with the organometallic compound.

Examples of the organic metal compound include organic aluminum compounds, organic magnesium compounds, organic boron compounds, organic lithium compounds, organic zinc compounds, organic phosphorus compounds and organic gallium compounds.
Among them, organoaluminum compounds can be preferably used.

Specific examples of the organic aluminum compound include trimethyl aluminum, triethyl aluminum, triisobutyl aluminum, tri-n-hexyl aluminum, diethyl aluminum chloride, dibutyl aluminum chloride, diethyl aluminum bromide, ethyl aluminum sesquichloride, ethyl aluminum sesquibromide. , Ethyl aluminum dichloride, propyl aluminum dichloride, butyl aluminum dichloride, ethyl aluminum dibromide, propyl aluminum dibromide, butyl aluminum dibromide, diethyl aluminum hydride, dibutyl aluminum hydride, ethyl aluminum dihydride, propyl aluminum dihydride, butyl aluminum dihydride , Ethyl aluminum Um ethoxy chloride, ethyl aluminum butoxide cycloalkyl chloride, and ethyl aluminum ethoxy bromide and the like. Alkyl lithium, dialkyl magnesium, alkyl magnesium halide, dialkyl zinc, trialkyl aluminum,
Although dialkyl or monoalkyl aluminum halides can be used, trialkyl aluminum is preferable, and specific examples thereof include trimethyl aluminum, triethyl aluminum, triisobutyl aluminum, trihexyl aluminum, trioctyl aluminum and the like. Any of the above organometallic compounds can be used as a mixture. Also,
Polyaluminoxane obtained by the reaction of alkylaluminum and water can be used as well.

Two or more kinds of these organometallic compounds may be used in combination. Further, the titanium compound-treated carrier may be contact-treated by using the organometallic compound stepwise twice or more.

The amount of the organometallic compound used is preferably such that the metal / Ti molar ratio is 0.1 to 1000, particularly 0.5 to 500, relative to the titanium atoms in the titanium compound-treated carrier. As a contact treatment method with an organometallic compound,
In an inert organic solvent, the reaction temperature is preferably 0 to 100 ° C., particularly 5 to 60 ° C., and the contact time is not particularly limited, but is usually 5 minutes or longer.

The Ti valence in the titanium compound-supported solid is reduced to less than 4 by the organometallic compound. Therefore,
By using the solid catalyst component (A) treated with an organometallic compound, the polymerization activity does not change significantly at the start of polymerization, the control of the polymerization reaction is facilitated, and an ethylene copolymer can be obtained with high catalyst efficiency. it can.

Specific examples of the organoaluminum compound component (B) include trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, diethylaluminum chloride,
Dibutyl aluminum chloride, diethyl aluminum bromide, ethyl aluminum sesquichloride, ethyl aluminum sesquibromide, ethyl aluminum dichloride, propyl aluminum dichloride, butyl aluminum dichloride, ethyl aluminum dibromide,
Propyl aluminum dibromide, butyl aluminum dibromide, diethyl aluminum hydride, dibutyl aluminum hydride, ethyl aluminum dihydride, propyl aluminum dihydride, butyl aluminum dihydride, ethyl aluminum ethoxy chloride, ethyl aluminum butoxycyclolide, ethyl aluminum ethoxy bromide, etc. Be done. Also, isopropenylaluminum obtained by the reaction of diisobutylaluminum hydride and isoprene can be used. Further, for example, an alkylalumoxane obtained by a reaction of trialkylaluminum with water dispersed in a solvent or a reaction of water of crystallization of an inorganic compound can be used.

Of these, trialkylaluminums such as triethylaluminum and triisobutylaluminum are preferably used. The amount of the organoaluminum compound component (B) used is usually 1 to 1000 mol per 1 gram atom of titanium in the solid catalyst component (A). still,
It is also possible to use two or more kinds of organoaluminum compounds in combination.

In the present invention, ethylene and α-olefin are copolymerized by using a catalyst composed of the components (A) and (B). Specific examples of α-olefins include:
Propylene, butene-1, 4-methylpentene-1, hexene-1, octene-1 and the like can be mentioned.

In the present invention, if necessary, the catalyst comprising the components (A) and (B) may be prepolymerized with ethylene or a mixture of ethylene and α-olefin. When carrying out the prepolymerization, it is preferred to carry out the polymerization until a particulate polymer containing 0.005 to 0.5 mmol of Ti atoms per gram of the prepolymer is obtained. An inert organic solvent may be used as a polymerization solvent, or a liquid α-olefin itself may be used.

As a preferable condition for producing the prepolymer, the polymerization pressure is usually atmospheric pressure to 10 kg / cm.
^{2. The} polymerization temperature is 100 ° C. or lower, usually 20 to 70 ° C. The polymerization time is usually 1 minute to 5 hours, preferably 1
~ 60 minutes. The ratio of the component (A) and the component (B) in the prepolymerization is the molar ratio of Ti and Al, respectively,
Usually, Al / Ti = 0.1 to 1000, preferably 0.
5 to 200. When the component (B) is used in the preliminary polymerization, the copolymer can be produced without additionally using the component (B) in the main polymerization. The prepolymer can be subjected to the main polymerization after evaporating a polymerization solvent with, for example, an inert gas, drying and removing it to obtain a powder.

The main polymerization reaction can be carried out in the same manner as the polymerization reaction of α-olefin with a conventional Ziegler-Natta type catalyst. The main polymerization reaction can be carried out in the liquid phase or the gas phase using the solid catalyst component (A) or the prepolymer. Examples of the gas phase polymerization reaction include a fluidized bed polymerization method and a stirring polymerization method.

In particular, when performing the fluidized bed polymerization method, it is possible to copolymerize gaseous ethylene and α-olefin in a fluidized bed polymerization reactor in the presence of the prepolymer produced as described above. preferable. As the α-olefin in the main polymerization, the same as or different from those used in the preparation of the prepolymer can be used. In the main polymerization, the heat of polymerization is removed by the monomer gas at the same time that the prepolymer is fluidized by the monomer gas and is usually 50
Polymerization is carried out at ˜110 ° C. In the main polymerization, when a prepolymer is used as a catalyst, an organoaluminum compound (B) can be used together.

When the polymerization reaction is carried out in the liquid phase, an inert organic solvent may be used as the polymerization solvent, or a liquid α-olefin itself may be used. The concentration of the catalyst in the polymerization solvent is not particularly limited, but generally 1 L of the polymerization solvent is used.
Therefore, the solid catalyst component (A) is 0.001 to 1 milligram atom in terms of titanium metal, and the organoaluminum compound component (B) is 0.01 to 100 mmol. The polymerization reaction is carried out in a state where water and oxygen are substantially removed. The polymerization temperature is usually 30 to 10
The temperature is 0 ° C., and the polymerization pressure is usually 1 to 80 kg / cm ² . Further, hydrogen can be made to coexist as a molecular weight regulator of the produced polymer.

[0037]

In the present invention, in particular, in the fluidized bed gas phase polymerization method, the proportion of low-molecular-weight tacky product is small, and since the block copolymer of α-olefin is little produced by the copolymerization, In the present polymerization method, good fluidity of polymer particles can be maintained, and a polymerization reaction can be stably carried out for a long period of time without formation of lumps of particles or adhesion to a reactor. The final polymer produced also has a relatively large particle size and is easy to handle because it does not form fine particles. Moreover, since the polymerization activity is high, a deashing step of the produced copolymer is unnecessary.
Further, since the produced copolymer has a narrow composition distribution and a narrow molecular weight distribution, even if the α-olefin content is increased to reduce the density, the surface tackiness of the molding film is small, and the mechanical strength of the molding is low. It has excellent physical properties such as being large.

[0038]

EXAMPLES Examples and comparative examples of the present invention will be described below. In the examples, the “polymerization activity” is a copolymer yield (kg) per 1 g of Ti component of the solid catalyst used in the polymerization reaction. "MI" means ASTM D-1
190 under a load of 2.16 kg / cm ² according to 238
It is the melt index of the polymer measured at ° C. The molecular weight distribution is
Polystyrene determined from GPC using as a standard, the ratio of the number average molecular weight M _W and the weight average molecular weight M _n M
_It was evaluated by _W / _Mn . The content of α-olefin is
It was measured by NMR. The titanium content of the solid catalyst component was measured by a colorimetric method. The content of α-olefin was measured by NMR. Density was measured by a density gradient tube. The composition distribution of the copolymer was evaluated by the relationship between the α-olefin content and the density. That is, in general, when the α-olefin content of the copolymer is the same, the density of the copolymer having a higher randomness is smaller, and thus the composition distribution is narrower.

Example 1 (1) Preparation of solid catalyst component Silica (TG-2040 manufactured by Fuji Devison Chemical Co., Ltd.)
2, average particle size 80μ, BET surface area 282m ² / g)
Was fired in a nitrogen stream at 200 ° C. for 2 hours and further at 600 ° C. for 7 hours. A reaction product obtained by adding 15 mmol of methyltriethoxysilane to 40 ml of a toluene slurry of 15 mmol of anhydrous aluminum chloride and reacting at 25 ° C. for 0.5 hours, then heating to 60 ° C. and further reacting for 1 hour. The mixture was added to 30 ml of a toluene slurry of 4 g of the above silica, and contact-treated at 25 ° C. for 6 hours. The treated solid was filtered off, washed with 30 ml of toluene three times and filtered, and 30 ml of toluene was added to obtain a toluene slurry.

Next, the obtained toluene slurry is placed at -5 ° C.
After cooling to 0.degree. C. and adding 18 ml of a solution of 30 mmol of n-butyl magnesium chloride in diisopropyl ether over 0.5 hour, the silica toluene slurry was heated to 30.degree. C. and reacted for 1 hour. The reaction solid obtained was filtered off, washed with 30 ml of toluene three times and filtered. To 30 ml of a toluene slurry containing 4.90 g of the obtained treated solid, 150 mmol of tetrachlorotitanium was added, and contact treatment was performed at 90 ° C. for 1 hour. The contact-treated solid was separated by filtration at 90 ° C., washed with 30 ml of toluene three times and filtered, and 40 mmol of trihexylaluminum was further added to 30 ml of toluene slurry, and contact-treated at 20 ° C. for 1 hour. The contact-treated solid was filtered off at 90 ° C., washed with 30 ml of n-heptane 5 times and filtered to obtain a slurry of 80 ml of n-heptane. The titanium content of the solid catalyst component was 2.70% by weight.

(2) Prepolymerization 800 ml of heptane was added to a 2 L autoclave made of SUS and purged with nitrogen gas, 10.0 mmol of tri-n-octylaluminum and catalyst solid (Ti = 1 mmol) were added.
Was introduced. After pressurizing with 1.5 kg / cm ² of hydrogen,
The temperature was raised to 60 ° C. and ethylene was introduced to initiate polymerization. Maintained at 68 ℃ during polymerization, ethylene flow rate is 0.93L
/ Min. Polymerize for 2 hours as 0.02 per gram
A prepolymer containing 2 mmol of Ti atoms was obtained.

(3) Gas phase copolymerization of ethylene and 1-butene 500 g of polyethylene powder produced in advance was used to obtain a diameter of 2
0 cm, 50 cm in length stirring type gas phase polymerization reactor,
The powder was pretreated at 110 ° C. for 5 hours under a nitrogen atmosphere with stirring at 1000 rpm. Then, from the bottom, 4 of ethylene / butene-1 / hydrogen (3/1 / 0.2 molar ratio)
The mixed gas at 5 ° C. is raised at a speed of 20 cm / sec,
Circulated. The copolymerization was carried out by introducing the prepolymer produced in (2) above at a rate of 10 g / hour, at a polymerization temperature of about 75 to 85 ° C., a polymerization pressure of 2 kg / cm ² , and an Al / Ti atomic ratio of 10,
It went on continuously for hours. During that period, the ethylene / butene-1 copolymer was continuously withdrawn and evaluated for activity and physical properties. The results are shown in Table 1.

Example 2 The molar ratio of the mixed gas in the main polymerization was changed to (ethylene / butene-1).
/Hydrogen=2/1/0.2 molar ratio)
An ethylene / butene-1 copolymer was obtained in the same manner as in. The results are shown in Table 1.

Examples 3, 4 A solid catalyst component was prepared under the same conditions and method as in Example 1 except that trioctylaluminum was used in place of trihexylaluminum, and the titanium content was 2.6.
8% by weight of solid catalyst component (A) was obtained. Then, prepolymerization was carried out in the same manner to obtain 0.021 mmol of Ti per gram of Ti.
A prepolymer containing atoms was obtained. Further, copolymerization was carried out under the same conditions and methods as in Examples 1 and 2 to obtain an ethylene / butene-1 copolymer. The results are shown in Table 1.

In any of Examples 1 to 4, the copolymer particles after copolymerization were not tacky, and neither aggregates nor adhesion to the reactor wall or stirrer was observed.

[Brief description of drawings]

FIG. 1 is a flowchart showing the polymerization method of the present invention and the steps for preparing a solid catalyst component used in the polymerization.

[Table 1]

Claims (1)

[Claims] 1. A porous inorganic oxide comprising the following formula: (1) aluminum halide and formula R ¹ _m Si (OR ² ) _4-m (wherein
R ¹ represents an alkyl group having 1 to 8 carbon atoms or a phenyl group, R ² represents an alkyl group having 1 to 8 carbon atoms, m is 0,
1, 2, or 3), a reaction product with an organosilicon compound, (2) Formula R ³ MgX ¹ (wherein R ³ represents an alkyl group having 1 to 8 carbon atoms, and X ¹ is A Grignard compound represented by a halogen atom), (3) Formula T
_{^{i (OR 4) n X 2}} 4-n ( wherein, ^{R 4} is 1 to 8 carbon atoms
Which is an alkyl group or a phenyl group, X ² represents a halogen atom, and n is 0, 1, 2, 3 or 4), and (4) an organometallic compound,
Ethylene copolymerization characterized by copolymerizing ethylene and α-olefin in the presence of a catalyst obtained from a solid catalyst component (A) obtained by sequential contact treatment and an organoaluminum compound component (B). Manufacturing method of coalescence.