JP5172522B2 - Method for synthesizing alkoxymagnesium, method for producing solid catalyst component for olefin polymerization, and method for producing catalyst - Google Patents

Description

  The present invention relates to a method for synthesizing alkoxymagnesium, in particular, a method for synthesizing alkoxymagnesium suitable as a carrier material for a solid catalyst component for olefin polymerization, and a solid catalyst component for olefin polymerization using the alkoxymagnesium and a catalyst. is there.

  The main production method of the solid catalyst component for polymerizing highly active olefins known as Ziegler-Natta catalyst is on the surface of the magnesium chloride support activated by mechanical grinding such as a vibration ball mill or dissolution reprecipitation using alcohol etc. A method of obtaining a solid catalyst component by supporting a titanium compound, a method of halogenating alkoxymagnesium with a chloride such as titanium tetrachloride, and then obtaining a solid catalyst component by supporting a titanium compound are known.

  Since the particle characteristics of the polymer produced using these catalysts are greatly influenced by the properties of the carrier, a technique for producing alkoxymagnesium according to the use of the polymer is extremely important. Specifically, there is a need for a carrier having high activity, high bulk density, and few fine particles in order to improve productivity. Currently, the following methods are known as methods for producing alkoxymagnesium.

For example, Patent Document 1 (Japanese Patent Laid-Open No. 3-74341) discloses a method in which metal magnesium and alcohol are added intermittently or continuously at an alcohol reflux temperature in the presence of iodine or magnesium chloride. Yes. Patent Document 2 (Japanese Patent Laid-Open No. 4-130107) discloses a method of reacting magnesium chloride or magnesium iodide containing 0.0001 gram atoms or more of halogen with respect to 1 mole of magnesium metal, alcohol and magnesium. Is disclosed. Patent Document 3 (Japanese Patent Laid-Open No. 2001-233878) discloses a method of reacting iodine in an amount of 0.0005 gram atom or more with metal magnesium, alcohol and 1 mol of magnesium in the presence of a saturated hydrocarbon compound. Has been. In Patent Document 4 (Japanese Patent Application Laid-Open No. 4-368391), a stirring blade diameter and a rotational speed in a method of reacting a specific halogen-containing compound of 0.0001 gram atom or more with respect to 1 mol of metal magnesium, alcohol and magnesium. The method of making it react under the specific stirring conditions prescribed | regulated by this is disclosed.
JP-A-3-74341 Japanese Patent Laid-Open No. 4-130107 JP 2001-233878 A JP-A-4-368391

  In recent years, production of polyolefins has been aimed at improving productivity, and improvement of bulk density and low pulverization of polyolefin powder have become the most important issues. As means for solving this problem, there is a demand for higher solid density and lower pulverization of solid catalyst components used in production than ever. However, the above-mentioned conventional technology cannot realize sufficiently high bulk density and low pulverization, which are related problems.

  Therefore, the object of the present invention is suitable for producing a polymer with a high bulk density and a low fineness without deteriorating the performances such as stereoregularity and polymerization activity. An object of the present invention is to provide a method for synthesizing alkoxymagnesium capable of obtaining a solid catalyst component, and a solid catalyst component and a catalyst for olefin polymerization using the alkoxymagnesium.

  In such a situation, the present inventor has intensively studied to solve the problems remaining in the prior art, and as a result, changed the stirring condition to a condition for lowering the stirring energy level during the alkoxymagnesium preparation process. It was found that by using the alkoxymagnesium used as the carrier of the solid catalyst component, a polymer having a high bulk density and a low fineness can be produced without reducing the performance such as stereoregularity and polymerization activity. It came to be completed.

That is, the present invention provides a method for synthesizing solid alkoxymagnesium by reacting metallic magnesium and alcohol in a stirring vessel with stirring in the presence of a halogen or a halogen-containing compound, and the stirring is performed in the following (I): To (III);
(I) Stir with a stirring blade attached to a stirring shaft provided at the center of the stirring tank;
(II) During the reaction, the stirring is changed from the following strong stirring condition to the following weak stirring condition at a stage where the reaction rate of metal magnesium becomes 20% or more;
1.9 × 10 ⁴ ≦ n _S ³ d ² (strong stirring condition) ≦ 1.9 × 10 ⁶
4.0 × 10 ³ ≦ n _W ³ d ² (weak stirring conditions) ≦ 1.7 × 10 ⁵
(In the formula, d is the stirring blade diameter (m), and n _S and n _W are the number of rotations per minute.)
(III) A method for synthesizing alkoxymagnesium, which is carried out under the conditions (n) in the above (II): n _S ³ d ² > n _W ³ d ² and n _S > 1.4 n _W.

In the present invention, metal magnesium and alcohol are reacted in a stirring vessel with stirring under the following stirring conditions (I) to (III) in the presence of a halogen or a halogen-containing compound. The present invention provides a method for producing a solid catalyst component for olefin polymerization , which comprises synthesizing and contacting the synthesized alkoxymagnesium (a) with a halogen-containing titanium compound (b).
(I) Stir with a stirring blade attached to a stirring shaft provided at the center of the stirring tank;
(II) During the reaction, the stirring is changed from the following strong stirring condition to the following weak stirring condition at a stage where the reaction rate of metal magnesium becomes 20% or more;
1.9 × 10 ⁴ ≦ n _S ³ d ² (strong stirring condition) ≦ 1.9 × 10 ⁶
4.0 × 10 ³ ≦ n _W ³ d ² (weak stirring conditions) ≦ 1.7 × 10 ⁵
(In the formula, d is the stirring blade diameter (m), and n _S and n _W are the number of rotations per minute.)
(III) In the above (II), n _S ³ d ² > n _W ³ d ² and n _S > 1.4 n _W ;

In the present invention, metal magnesium and alcohol are reacted in a stirring vessel with stirring under the following stirring conditions (I) to (III) in the presence of a halogen or a halogen-containing compound. And the synthesized alkoxymagnesium (a) and the halogen-containing titanium compound (b) are contacted to obtain a solid catalyst component for olefin polymerization, and (A) the solid catalyst component for olefin polymerization and (B) The following general formula (1);
R ¹ _p AlQ _3-p (1)
(In the formula, R ¹ represents an alkyl group having 1 to 4 carbon atoms, Q is a hydrogen atom or a halogen atom, p is 0 <a real number p ≦ 3.) Contacting an organoaluminum compound represented by The present invention provides a method for producing an olefin polymerization catalyst.
(I) Stir with a stirring blade attached to a stirring shaft provided at the center of the stirring tank;
(II) During the reaction, the stirring is changed from the following strong stirring condition to the following weak stirring condition at a stage where the reaction rate of metal magnesium becomes 20% or more;
1.9 × 10 ⁴ ≦ n _S ³ d ² (strong stirring condition) ≦ 1.9 × 10 ⁶
4.0 × 10 ³ ≦ n _W ³ d ² (weak stirring conditions) ≦ 1.7 × 10 ⁵
(In the formula, d is the stirring blade diameter (m), and n _S and n _W are the number of rotations per minute.)
(III) In the above (II), n _S ³ d ² > n _W ³ d ² and n _S > 1.4 n _W ;

  According to the synthesis method of the present invention, alkoxymagnesium useful as a solid catalyst component for olefin polymerization can be produced by a simple method. Further, if the alkoxymagnesium is used as one component of a solid catalyst component for olefin polymerization, an olefin polymer having a high bulk density, a low fine powder, and a good particle size distribution can be obtained without reducing the performance such as stereoregularity and polymerization activity. can get.

(Description of synthesis method of alkoxymagnesium)
In the synthesis method of the present invention, the shape of the metallic magnesium is not particularly limited, and any shape of metallic magnesium can be used. For example, granular, ribbon-like, powdery, etc. metallic magnesium is used. Among these, powdered metal magnesium is preferable, and the average particle diameter is preferably 1 to 1000 μm, more preferably 10 to 500 μm. Further, the surface state of the metallic magnesium is not particularly limited, but it is not preferable that the surface is formed with a film such as magnesium oxide, so it is desirable to remove it beforehand.

In the synthesis method of the present invention, the alcohol is not particularly limited, and the following general formula (2); R ² OH (2)
(Wherein R ² is a linear or branched alkyl group having 1 to 12 carbon atoms), preferably a lower alcohol having 1 to 6 carbon atoms, It is preferable to use methanol, ethanol, propanol, or butanol. In particular, by using ethanol, ethoxymagnesium is formed, and alkoxymagnesium that significantly improves the expression of catalyst performance is obtained. The purity and water content of the alcohol are not limited, but the lower the moisture, the better. Specifically, dehydrated alcohol and a dehydrated alcohol having a water content of 200 ppm or less are desirable.

  In the synthesis method of the present invention, the type of halogen is not particularly limited, but chlorine, bromine or iodine, particularly iodine is desirable. The type of halogen-containing compound is not limited, and any compound containing a halogen atom in its chemical formula can be used. Specific examples of the halogen compound include halogenated metals such as titanium tetrachloride, titanium trichloride, magnesium chloride and magnesium iodide, and halogenated alkoxy metals such as ethoxytitanium dichloride, ethoxymagnesium monochloride and ethoxymagnesium monoiodide. Can be used. Of these, titanium tetrachloride, magnesium chloride, and ethoxytitanium dichloride are particularly preferable.

  The state, shape, particle size and the like of the halogen or halogen-containing compound are not particularly limited and may be any, for example, can be used as a solution of an alcohol solvent such as ethanol. Moreover, you may mix and use with another 1 type, or 2 or more types of halogen containing compound.

  The reaction between the magnesium metal and the alcohol includes a main reaction step until generation of hydrogen gas is not recognized, and an aging step performed while maintaining the reaction temperature generally after the generation of hydrogen gas is stopped. The aging step can be omitted. This reaction step can be carried out in the same manner as in a known method. That is, there is usually a method of obtaining alkoxymagnesium by reacting for 10 minutes to 30 hours until generation of hydrogen gas is not recognized. The reaction is preferably performed in an atmosphere of an inert gas such as nitrogen gas or argon gas. The reaction is usually performed at 30 ° C. or higher, preferably 40 ° C. or higher and 80 ° C. or lower, particularly preferably under reflux of alcohol.

  The above reaction may be performed in the presence of a saturated hydrocarbon compound, an aromatic hydrocarbon compound or the like. Examples of the saturated hydrocarbon compound include linear saturated hydrocarbon compounds, branched saturated hydrocarbon compounds, and alicyclic saturated hydrocarbon compounds having a boiling point higher than that of alcohols having 7 to 15 carbon atoms. Specific examples include heptane, decane, cyclohexane, isooctane and the like, but are not particularly limited and may be arbitrary. In addition, examples of the aromatic hydrocarbon compound include toluene, xylene, ethylbenzene, and the like, but this is not particularly limited.

  With respect to the addition of magnesium metal, alcohol, and halogen-containing compound, a method may be used in which all of them are added from the beginning, or each may be divided into several times and reacted. A particularly preferred form is a method in which the whole amount of alcohol is added from the beginning, an appropriate amount of a halogen-containing compound is added, and metal magnesium and the halogen-containing compound are added thereto in several divided or continuously. In the case of this method, high bulk density and low fine powdery alkoxymagnesium are formed, and at the same time, temporary mass generation of hydrogen gas can be prevented, which is very desirable from the viewpoint of safety. Also, the reaction vessel can be downsized. Furthermore, it becomes possible to prevent entrainment of alcohol and halogen compounds caused by temporary large-scale generation of hydrogen gas.

  In the present invention, the reaction is carried out in a stirring vessel while stirring under the stirring conditions (I), (II) and (III). Stirring is performed with a stirring blade attached to a rotating shaft provided at the center of the stirring tank. The stirring blade may be either a single stage blade or a multistage blade. Examples of the multistage wing include a multistage wing such as a lattice wing and a full zone wing. In the case of multi-stage blades, use the same blade diameter for each stage.

  A suitable example of the stirring tank and the stirring blade will be described with reference to FIG. In FIG. 2, 1 is a cylindrical stirring tank having a curved bottom surface, and a rotating shaft 4 is provided at the center thereof. A drive motor or the like (not shown) is connected to the upper side of the rotating shaft 4, and a two-stage stirring blade 5 is attached to the lower side without using a bearing. Further, it is preferable that no partition plate or the like is attached to the inner wall of the stirring tank 1.

  The stirring blade 5 includes a lower blade 2 and an upper blade 3. As the lower blade 2, various known stirring blades such as a single blade such as a paddle and an inclined paddle, a turbine blade such as a turbine and an inclined turbine, a three-recessed blade, and a marine can be used. The lower wing 2 preferably has a shape in which the lower edge is curved along the tank bottom, and the clearance between the lower end and the bottom surface of the lower wing 2 is preferably as small as possible.

  As the upper wing 3, a lattice wing is desirable. The lower wing 2 and the upper wing 3 may be a continuous body or separated by a gap. Moreover, the installation angle (direction in which the blades extend) of the lower blade 2 and the upper blade 3 with respect to the rotation shaft 4 may be shifted. The ratio d / D between the tank diameter D and the blade diameter d is preferably as close to 1 as possible to prevent the slurry from adhering to the wall surface, preferably 0.99> d / D> 0.6, more preferably 0.98> d / D> 0.8.

  Moreover, the said stirring changes the said stirring from a strong stirring condition to a weak stirring condition in the step in which the reaction rate of metal magnesium becomes 20% or more during the said reaction.

When the stirring blade diameter is d (m), the rotation speed under strong stirring conditions is n _S (rpm), and the rotation speed under weak stirring conditions is n _W (rpm), the stirring conditions in the initial stage of the reaction are strong stirring. It is a condition. The strong stirring condition is preferably 1.9 × 10 ⁴ ≦ n _S ³ d ² ≦ 1.9 × 10 ⁶ . If the strong stirring condition n _S ³ d ² exceeds 1.9 × 10 ⁶ , the formed particles are destroyed because the stirring is too strong, resulting in generation of fine powder and deterioration of the particle size distribution. Further, when the strong stirring condition n _S ³ d ² is less than 1.9 × 10 ⁴ , aggregation occurs during the reaction.

The weak stirring conditions are preferably 4.0 × 10 ³ ≦ n _W ³ d ² ≦ 1.7 × 10 ⁵ . If the weak stirring condition n _W ³ d ² exceeds 1.7 × 10 ⁵ , the stirring is too strong, which causes generation of fine powder, deterioration of particle size distribution, formation of particles having a rough surface state, and the like. If it is less than 4.0 × 10 ³ , aggregation and precipitation occur. Within the range of weak stirring conditions, the stirring energy may be reduced several times as necessary.

Which condition is selected within the range of the strong stirring condition (n _S ³ d ² ) and the weak stirring condition (n _W ³ d ² ) depends on the target particle size and bulk density of alkoxymagnesium, but n _S It is essential to select such that ³ d ² > n _W ³ d ² , n _S > 1.4 n _W. Strong stirring conditions are effective in keeping the particle size distribution of alkoxymagnesium produced by preventing aggregation between nuclei in the nucleation stage of alkoxymagnesium. However, if the reaction is terminated under these conditions, strong energy is added to the particles at the end of the reaction, which may cause cracking of the particles and generation of fine powder, or cause the surface state of the particles to become rough and reduce the bulk density. Become. For this reason, it is necessary to stir under weak stirring conditions at the stage where nucleation is completed and the particle diameter is grown. This condition is an effective condition for uniformly reacting alkoxymagnesium grown to a certain particle size without agglomerating and precipitating. The energy is not too strong to prevent the generation of fine powder and the deterioration of the surface condition. it can.

  In addition, the transition from the strong stirring condition to the weak stirring condition may be performed at any timing depending on the target particle size and bulk density of the alkoxy magnesium as long as the reaction rate of metal magnesium reaches 20% or more. That is, the transition from the strong stirring condition to the weak stirring condition may be performed after entering the aging step of the reaction. When metallic magnesium with the same particle size, shape, etc. is used, large-sized alkoxymagnesium is obtained when shifting to weak stirring conditions at a relatively early stage when the reaction rate is 20% or more, and shifting to weak stirring conditions in the second half of the reaction Then, alkoxymagnesium with a small particle size is obtained. When the reaction rate is less than 20%, the agglomerates are generated when the mode is shifted to weak stirring conditions, and the particle size distribution becomes broad. The weak stirring conditions are preferably performed for at least 10 minutes. Here, the reaction rate in this invention is the ratio of the metal magnesium which reacted with alcohol with respect to the metal magnesium whole quantity with which reaction in a batch reaction is provided. That is, when metal magnesium and alcohol are brought into contact and reacted at once, it is a pure reaction rate of the input metal magnesium, and the reaction rate in the case of adding metal magnesium and the alcohol continuously or divided and reacting is This is the reaction ratio of metallic magnesium to the final amount of metallic magnesium. Even if not all of the metallic magnesium has been charged, at some point during the charging, 20% or more of the final amount of metallic magnesium has reacted. Good. As described above, in the reaction of metal magnesium and alcohol, particles that become the core of alkoxymagnesium are formed at the initial stage of the reaction, and final alkoxymagnesium particles are formed around this nucleus. The formation of the final particles from the nuclei is the same phenomenon even if the entire amount of metallic magnesium is present from the beginning in the reaction system or even if additional metallic magnesium is added during the reaction. Therefore, in the present invention, fine powder is formed by reacting under specific strong stirring conditions until the reaction rate reaches 20%, which is the initial stage of the reaction, to form a dense alkoxymagnesium nucleus and then reacting under weak stirring conditions. Alkoxymagnesium particles having a small particle size distribution and a large bulk specific gravity can be formed.

  The reaction rate of metallic magnesium can be accurately measured by integrating the amount of hydrogen gas generation.

  Since the alkoxymagnesium obtained as described above is used for the preparation of the next solid catalyst component (A), it can be used after drying or by washing the alcohol with an inert hydrocarbon compound.

  The alkoxymagnesium obtained as described above is spherical and has a sharp particle size distribution. Furthermore, the variation in sphericity of each particle is small. Specifically, the average particle size of the alkoxymagnesium of the present invention is 1 to 200 μm, preferably 5 to 100 μm, and particularly preferably 10 to 70 μm. The carrier particles are preferably diethoxymagnesium powder.

The particle size distribution of alkoxymagnesium is:
_{SPAN = (D 90 -D 10)} / D 50
Is preferably 4 or less, preferably 2 or less, particularly preferably 1.0 or less. This SPAN value indicates the degree of spread of the particle size distribution, and the smaller the value, the sharper the particle size distribution and the more uniform the particle size.

In the above formula, D ₉₀ is a particle size corresponding to 90% of the cumulative volume fraction in the particle size distribution of the magnesium compound determined by measurement with a laser diffraction particle size distribution measuring device in a state suspended in the hydrocarbon compound. D ₁₀ indicates a particle size corresponding to a cumulative volume fraction of 10%, and D ₅₀ indicates a particle size corresponding to 50%.

Alkoxy magnesium obtained _is less than 1/4 of the particle diameter of _{D 50} is defined as fines, percentage powder occupied by the fine powder, 1.0 wt% or less, preferably less 0.8 wt%. The proportion of fine powder can be obtained by measuring with a laser diffraction particle size distribution analyzer.

  The resulting alkoxymagnesium has a bulk density (bulk specific gravity) of 0.200 to 0.350, preferably 0.280 to 0.330. The bulk specific gravity may be measured according to JIS K6721.

  The resulting alkoxymagnesium is spherical, has a sharp particle size distribution, has a small amount of fine powder, and has a high bulk density. Therefore, if an olefin is polymerized under a catalyst prepared using this, the stereoregularity, polymerization activity, etc. A polymer with a high bulk density and a low fineness can be produced without reducing the performance.

(Method for producing solid catalyst component for olefin polymerization)
In the production method of the present invention, the solid catalyst component for olefin polymerization is an alkoxymagnesium (a) obtained by the above synthesis method (hereinafter sometimes simply referred to as “component (a)”) and a halogen-containing compound (b). ) And an electron donating compound (c) as necessary.

  The halogen-containing titanium compound (b) (hereinafter sometimes referred to as “component (b)”) used for the preparation of the component (A) in the present invention is one type of compound selected from the group consisting of titanium halides and alkoxytitanium halides. Or it is 2 or more types. Specifically, titanium tetrachloride such as titanium tetrachloride, titanium tetrabromide and titanium tetraiodide as titanium halide, methoxytitanium trichloride, ethoxytitanium trichloride, propoxytitanium trichloride, n-butoxytitanium trichloride as alkoxytitanium halide. Examples include chloride, dimethoxy titanium dichloride, diethoxy titanium dichloride, dipropoxy titanium dichloride, di-n-butoxy titanium dichloride, trimethoxy titanium chloride, triethoxy titanium chloride, tripropoxy titanium chloride, tri-n-butoxy titanium chloride. The Of these, titanium tetrahalide is preferable, and titanium tetrachloride is particularly preferable. These titanium compounds can be used alone or in combination of two or more.

  The electron-donating compound (hereinafter sometimes simply referred to as component (c)) used in the preparation of the solid catalyst component (A) in the present invention is an organic compound containing an oxygen atom or a nitrogen atom, such as alcohols. Phenols, ethers, esters, ketones, acid halides, aldehydes, amines, amides, nitriles, isocyanates, organosilicon compounds containing a Si—O—C bond, and the like.

  Specifically, alcohols such as methanol, ethanol, n-propanol and 2-ethylhexanol, phenols such as phenol and cresol, methyl ether, ethyl ether, propyl ether, butyl ether, amyl ether, diphenyl ether, 9,9- Ethers such as bis (methoxymethyl) fluorene and 2-isopropyl-2-isopentyl-1,3-dimethoxypropane, methyl formate, ethyl acetate, vinyl acetate, propyl acetate, octyl acetate, cyclohexyl acetate, ethyl propionate, ethyl butyrate , Methyl benzoate, ethyl benzoate, propyl benzoate, butyl benzoate, octyl benzoate, cyclohexyl benzoate, phenyl benzoate, methyl p-toluate, ethyl p-toluate, methyl anisate, anisic acid Monocarboxylic acid esters such as chill, diethyl malonate, dipropyl malonate, dibutyl malonate, diisobutyl malonate, dipentyl malonate, dineopentyl malonate, diethyl isopropyl bromomalonate, diethyl butyl bromomalonate, diethyl isobutyl bromomalonate , Diethyl diisopropylmalonate, diethyl dibutylmalonate, diethyl diisobutylmalonate, diethyl diisopentylmalonate, diethyl isopropylisobutylmalonate, dimethyl isopropylisopentylmalonate, diethyl (3-chloro-n-propyl) malonate, bis (3-Bromo-n-propyl) diethyl malonate, diethyl maleate, dibutyl maleate, dimethyl adipate, diethyl adipate, dipropyl adipate, adipine Dibutyl esters such as dibutyl, diisodecyl adipate, dioctyl adipate, succinic diester, phthalic diester, phthalic diester derivatives, 1-cyclohexene-1,2-dicarboxylic acid dineopentyl, acetone, methyl ethyl ketone, methyl butyl ketone, acetophenone , Ketones such as benzophenone, acid halides such as phthalic acid dichloride and terephthalic acid dichloride, aldehydes such as acetaldehyde, propionaldehyde, octylaldehyde and benzaldehyde, amines such as methylamine, ethylamine, tributylamine, piperidine, aniline and pyridine Amides such as oleamide and stearamide, nitriles such as acetonitrile, benzonitrile and tolunitrile, isocyanide Mention of organosilicon compounds containing Si—O—C bonds such as isocyanates such as methyl acid and ethyl isocyanate, phenylalkoxysilanes, alkylalkoxysilanes, phenylalkylalkoxysilanes, cycloalkylalkoxysilanes, cycloalkylalkylalkoxysilanes, etc. Can do.

  Among the above electron donating compounds, esters, particularly aromatic dicarboxylic acid diesters are preferably used, and phthalic acid diesters and phthalic acid diester derivatives are particularly preferable. Specific examples of these phthalic acid diesters include dimethyl phthalate, diethyl phthalate, di-n-propyl phthalate, di-iso-propyl phthalate, di-n-butyl phthalate, and di-iso-butyl phthalate. , Ethyl methyl phthalate, methyl phthalate (iso-propyl), ethyl phthalate (n-propyl), ethyl phthalate (n-butyl), ethyl phthalate (iso-butyl), di-n-pentyl phthalate, Di-iso-pentyl phthalate, di-neo-pentyl phthalate, dihexyl phthalate, di-n-heptyl phthalate, di-n-octyl phthalate, bis (2,2-dimethylhexyl) phthalate, phthalic acid Bis (2-ethylhexyl), di-n-nonyl phthalate, di-iso-decyl phthalate, bis (2,2-dimethylheptyl phthalate) ), N-butyl phthalate (iso-hexyl), n-butyl phthalate (2-ethylhexyl), n-pentylhexyl phthalate, n-pentyl phthalate (iso-hexyl), iso-pentyl phthalate (heptyl) N-pentyl (2-ethylhexyl) phthalate, n-pentyl phthalate (iso-nonyl), iso-pentyl phthalate (n-decyl), n-pentyl undecyl phthalate, iso-pentyl phthalate (iso- Hexyl), n-hexyl phthalate (2,2-dimethylhexyl), n-hexyl phthalate (2-ethylhexyl), n-hexyl phthalate (iso-nonyl), n-hexyl phthalate (n-decyl), N-heptyl phthalate (2-ethylhexyl), n-heptyl phthalate (iso-nonyl), n-phthalate Heptyl (neo-decyl), is phthalate 2-ethylhexyl (an iso-nonyl) is exemplified, these phthalic diester one or two or more kinds are used.

  As the phthalic acid diester derivative, one or two hydrogen atoms of the benzene ring to which the two alkoxycarbonyl groups of the above phthalic acid diester are bonded are an alkyl group having 1 to 5 carbon atoms, a chlorine atom, or a bromine atom. And those substituted with a halogen atom such as a fluorine atom. The solid catalyst component prepared by using the phthalic diester derivative as an electron donating compound can further improve the hydrogen activity or hydrogen response, and the polymer melt flow can be performed even when the amount of hydrogen added during polymerization is the same or small. The rate can be improved. Specifically, dineopentyl 4-methylphthalate, dineopentyl 4-ethylphthalate, dineopentyl 4,5-dimethylphthalate, dineopentyl 4,5-diethylphthalate, diethyl 4-chlorophthalate, di-n-butyl 4-chlorophthalate , Dineopentyl 4-chlorophthalate, di-iso-butyl 4-chlorophthalate, di-iso-hexyl 4-chlorophthalate, di-iso-octyl 4-chlorophthalate, diethyl 4-bromophthalate, di-n 4-bromophthalate -Butyl, dineopentyl 4-bromophthalate, di-iso-butyl 4-bromophthalate, di-iso-hexyl 4-bromophthalate, di-iso-octyl 4-bromophthalate, diethyl 4,5-dichlorophthalate, 4, Di-n-butyl 5-dichlorophthalate, 4, -Di-iso-hexyl dichlorophthalate, di-iso-octyl 4,5-dichlorophthalate, among which dineopentyl 4-bromophthalate, di-n-butyl 4-bromophthalate and di-4-bromophthalate -Iso-butyl is preferred.

  The above esters are preferably used in combination of two or more, and the esters are used so that the total carbon number of the alkyl group of the ester used is 4 or more compared to that of other esters. It is desirable to combine.

  In the present invention, the components (a), (b) and (c) are brought into contact with each other in the presence of the hydrocarbon compound (d) (hereinafter sometimes simply referred to as “component (d)”). The method of preparing (A) is a preferred embodiment of the preparation method. Specifically, the component (d) has a boiling point of 50 to 150, such as n-heptane, n-hexane, cyclohexane, toluene, xylene, and ethylbenzene. A hydrocarbon compound at 0 ° C. is preferably used. Moreover, these may be used independently or may be used in mixture of 2 or more types.

  As a particularly preferred method for preparing the solid catalyst component in the present invention, a suspension is formed from the component (a), the component (c), and the hydrocarbon compound (d) having a boiling point of 50 to 150 ° C., and the component (b) The preparation method by making the mixed solution formed from the component (d) contact this suspension, and making it react after that can be mentioned.

In the preparation of the solid catalyst component (A) of the present invention, in addition to the above components, polysiloxane (hereinafter sometimes simply referred to as “component (e)”) can be used. By using polysiloxane, the stereoregularity or crystallinity of the produced polymer can be improved, and further the fine powder of the produced polymer can be reduced. Polysiloxane is a polymer having a siloxane bond (—Si—O— bond) in the main chain, and is also collectively referred to as silicone oil, and has a viscosity at 25 ° C. of 0.02 to 100 cm ² / s ( ^{2 to} 10,000 centistokes). ), More preferably 0.03 to ⁵ cm ² / s (3 to 500 centistokes), a liquid or viscous chain, partially hydrogenated, cyclic or modified polysiloxane at room temperature.

  As the chain polysiloxane, dimethylpolysiloxane and methylphenylpolysiloxane are used. As the partially hydrogenated polysiloxane, methylhydrogen polysiloxane having a hydrogenation rate of 10 to 80% is used. As the cyclic polysiloxane, hexamethylcyclotrimethyl is used. Siloxane, octamethylcyclotetrasiloxane, decamethylcyclopentasiloxane, 2,4,6-trimethylcyclotrisiloxane, 2,4,6,8-tetramethylcyclotetrasiloxane, and modified polysiloxanes include higher fatty acid groups. Examples thereof include substituted dimethylsiloxane, epoxy group-substituted dimethylsiloxane, and polyoxyalkylene group-substituted dimethylsiloxane. Among these, decamethylcyclopentasiloxane and dimethylpolysiloxane are preferable, and decamethylcyclopentasiloxane is particularly preferable.

  As a preferred method for preparing the solid catalyst component of the present invention, the component (a) is suspended in the component (d), then the component (b) is contacted, and then the component (c) and the component (d) are contacted. A method of preparing a solid catalyst component by reacting, or by suspending component (a) in component (d) and then contacting component (c), then contacting component (b) and reacting The method of preparing a solid catalyst component can be mentioned. Moreover, the performance of the final solid catalyst component can be improved by bringing the component (b) or the component (b) and the component (c) into contact with the solid catalyst component thus prepared again or a plurality of times. At this time, it is desirable to carry out in the presence of the aromatic hydrocarbon compound (d).

  As a preferred method for preparing a solid catalyst component of the present invention containing component (e), component (a) is suspended in component (d) and then contacted with component (b), then component (c), component ( a method of preparing a solid catalyst component by bringing d) and component (e) into contact with each other and reacting them, or, after suspending component (a) in component (d) and then contacting component (c) A method of preparing a solid catalyst component by bringing (b) into contact with each other and further contacting with component (e) to cause a reaction can be mentioned. Further, the performance of the final solid catalyst component is improved by bringing the component (b) or the component (b), the component (c) and the component (e) into contact with the solid catalyst component thus prepared again or multiple times. Can be made. At this time, it is desirable to carry out in the presence of the aromatic hydrocarbon compound (d).

  The contact of each component is performed with stirring in a container equipped with a stirrer in an inert gas atmosphere and in a state where moisture and the like are removed. The contact temperature is a temperature at the time of contact of each component, and may be the same temperature as the reaction temperature or a different temperature. The contact temperature may be a relatively low temperature range around room temperature when the mixture is simply brought into contact with stirring and mixed, or dispersed or suspended for modification, but the product is allowed to react after contact. When obtaining, the temperature range of 40-130 degreeC is preferable. If the temperature during the reaction is less than 40 ° C., the reaction does not proceed sufficiently, resulting in insufficient performance of the prepared solid component, and if it exceeds 130 ° C., the evaporation of the solvent used becomes remarkable. , It becomes difficult to control the reaction. The reaction time is 1 minute or longer, preferably 10 minutes or longer, more preferably 30 minutes or longer.

  The amount of each component used in preparing the solid catalyst component (A) varies depending on the preparation method and cannot be defined unconditionally. For example, the halogen-containing titanium compound (b) is 0 per mole of alkoxymagnesium (a). 0.5 to 100 mol, preferably 0.5 to 50 mol, more preferably 1 to 10 mol, and the electron donating compound (c) is 0.01 to 10 mol, preferably 0.01 to 1 mol, more Preferably it is 0.02-0.6 mol, and hydrocarbon compound (d) is 0.001-500 mol, Preferably it is 0.001-100 mol, More preferably, it is 0.005-10 mol. When using polysiloxane (e), it is 0.01-100g, Preferably it is 0.05-80g, More preferably, it is 1-50g.

  Further, the content of titanium, magnesium, a halogen atom and an electron donating compound in the solid catalyst component (A) or (A) in the present invention is not particularly defined, but preferably, titanium is 0.1 to 20% by weight, preferably 1.0 to 10 wt%, magnesium 10 to 25 wt%, more preferably 15 to 25 wt%, particularly preferably 20 to 25 wt%, halogen atoms 20 to 75 wt%, more preferably 30 to 75 wt%. % By weight, particularly preferably 40 to 75% by weight, more preferably 45 to 75% by weight, and when an electron donating compound is used, a total of 0.5 to 30% by weight, more preferably a total of 1 to 25% by weight, especially Preferably it is 2 to 20 weight% in total.

(Description of formation of catalyst for olefin polymerization)
The olefin polymerization catalyst of the present invention includes the above-described solid catalyst component (A) for olefin polymerization, the organoaluminum compound (B) represented by the general formula (1), and, if necessary, an external electron donating compound. (C) is contained.

The organoaluminum compound (B) (hereinafter sometimes simply referred to as “component (B)”) used in forming the olefin polymerization catalyst of the present invention is a compound represented by the above general formula (1). if is not particularly limited, examples of R ^1, an ethyl group, isobutyl group are preferable, as the Q, hydrogen atom, a chlorine atom, preferably a bromine atom, p is preferably 2 or 3, most preferably 3. Specific examples of such an organoaluminum compound (B) include triethylaluminum, diethylaluminum chloride, triisobutylaluminum, diethylaluminum bromide, and diethylaluminum hydride, and one or more can be used. Triethylaluminum and triisobutylaluminum are preferable.

  The external electron donating compound (C) (hereinafter sometimes referred to as “component (C)”) used in forming the olefin polymerization catalyst of the present invention is used for the preparation of the solid catalyst component described above. The same electron donating compounds that can be used are used, and among them, ethers, esters, or organosilicon compounds are preferable. Among the ethers, 1,3 diether is preferable, and 9,9-bis (methoxymethyl) fluorene and 2-isopropyl-2-isopentyl-1,3-dimethoxypropane are particularly preferable. Of the esters, methyl benzoate and ethyl benzoate are preferred.

As said organosilicon compound, following General formula (3)
R ³ _q Si (NR ⁴ R ⁵ ) _r (OR ⁶ ) _{4- (q + r)} (3)
(In the formula, q is an integer of 0, 1 to ⁴ , r is an integer of 0, 1 to ⁴ , provided that q + r is an integer of 0 to 4, R ³ , R ⁴ or R ⁵ is a hydrogen atom, 1 to Any of 12 linear or branched alkyl groups, substituted or unsubstituted cycloalkyl groups, phenyl groups, vinyl groups, allyl groups, aralkyl groups, which may contain heteroatoms, and may be the same or different R ⁶ represents an alkyl group having 1 to 4 carbon atoms, a cycloalkyl group, a phenyl group, a vinyl group, an allyl group, or an aralkyl group, may contain a hetero atom, may be the same or different, and R ⁴ And R ⁵ may combine to form a ring.).

In general formula (3), R ³ is preferably a linear or branched alkyl group having 1 to 10 carbon atoms or a cycloalkyl group having 5 to 8 carbon atoms, and particularly a linear or branched group having 1 to 8 carbon atoms. An alkyl group and a cycloalkyl group having 5 to 8 carbon atoms are preferred. R ⁴ or R ⁵ is preferably a linear or branched alkyl group having 1 to 10 carbon atoms or a cycloalkyl group having 5 to 8 carbon atoms, particularly a linear or branched alkyl group having 1 to 8 carbon atoms. And a cycloalkyl group having 5 to 8 carbon atoms is preferred. In addition, R ⁴ and R ⁵ are combined to form a ring (NR ⁴ R ⁵ ) is preferably a perhydroquinolino group or a perhydroisoquinolino group. R ⁶ is preferably a linear or branched alkyl group having 1 to ⁶ carbon atoms, and particularly preferably a linear or branched alkyl group having 1 to 4 carbon atoms.

  Examples of such organosilicon compounds include phenylalkoxysilane, alkylalkoxysilane, phenylalkylalkoxysilane, cycloalkylalkoxysilane, cycloalkylalkylalkoxysilane, (alkylamino) alkoxysilane, alkyl (alkylamino) alkoxysilane, alkyl ( Alkylamino) silane, alkylaminosilane and the like.

  In the formula, specific examples of the organosilicon compound in which r is 0 include trimethylmethoxysilane, trimethylethoxysilane, tri-n-propylmethoxysilane, tri-n-propylethoxysilane, tri-n-butylmethoxysilane, tri -Iso-butylmethoxysilane, tri-t-butylmethoxysilane, tri-n-butylethoxysilane, tricyclohexylmethoxysilane, tricyclohexylethoxysilane, cyclohexyldimethylmethoxysilane, cyclohexyldiethylmethoxysilane, cyclohexyldiethylethoxysilane, dimethyldimethoxy Silane, dimethyldiethoxysilane, di-n-propyldimethoxysilane, di-iso-propyldimethoxysilane, di-n-propyldiethoxysilane, di-iso-propyldi Toxisilane, di-n-butyldimethoxysilane, di-iso-butyldimethoxysilane, di-t-butyldimethoxysilane, di-n-butyldiethoxysilane, n-butylmethyldimethoxysilane, bis (2-ethylhexyl) dimethoxysilane Bis (2-ethylhexyl) diethoxysilane, dicyclopentyldimethoxysilane, dicyclopentyldiethoxysilane, dicyclohexyldimethoxysilane, dicyclohexyldiethoxysilane, bis (3-methylcyclohexyl) dimethoxysilane, bis (4-methylcyclohexyl) dimethoxysilane Bis (3,5-dimethylcyclohexyl) dimethoxysilane, cyclohexylcyclopentyldimethoxysilane, cyclohexylcyclopentyldiethoxysilane, cyclohexyl Pentyldipropoxysilane, 3-methylcyclohexylcyclopentyldimethoxysilane, 4-methylcyclohexylcyclopentyldimethoxysilane, 3,5-dimethylcyclohexylcyclopentyldimethoxysilane, 3-methylcyclohexylcyclohexyldimethoxysilane, 4-methylcyclohexylcyclohexyldimethoxysilane, 3,5 -Dimethylcyclohexylcyclohexyldimethoxysilane, cyclopentylmethyldimethoxysilane, cyclopentylmethyldiethoxysilane, cyclopentylethyldiethoxysilane, cyclopentyl (iso-propyl) dimethoxysilane, cyclopentyl (iso-butyl) dimethoxysilane, cyclohexylmethyldimethoxysilane, cyclohexylmethyldi Ethoxysilane, cyclo Xylethyldimethoxysilane, cyclohexylethyldiethoxysilane, cyclohexyl (n-propyl) dimethoxysilane, cyclohexyl (iso-propyl) dimethoxysilane, cyclohexyl (n-propyl) diethoxysilane, cyclohexyl (iso-butyl) dimethoxysilane, cyclohexyl ( n-butyl) diethoxysilane, cyclohexyl (n-pentyl) dimethoxysilane, cyclohexyl (n-pentyl) diethoxysilane, diphenyldimethoxysilane, diphenyldiethoxysilane, phenylmethyldimethoxysilane, phenylmethyldiethoxysilane, phenylethyldimethoxy Silane, phenylethyldiethoxysilane, methyltrimethoxysilane, methyltriethoxysilane, ethyltrimethoxysila , Ethyltriethoxysilane, n-propyltrimethoxysilane, iso-propyltrimethoxysilane, n-propyltriethoxysilane, iso-propyltriethoxysilane, n-butyltrimethoxysilane, iso-butyltrimethoxysilane, t -Butyltrimethoxysilane, n-butyltriethoxysilane, 2-ethylhexyltrimethoxysilane, 2-ethylhexyltriethoxysilane, cyclopentyltrimethoxysilane, cyclopentyltriethoxysilane, cyclohexyltrimethoxysilane, cyclohexyltriethoxysilane, vinyltrimethoxy Silane, vinyltriethoxysilane, phenyltrimethoxysilane, phenyltriethoxysilane, tetramethoxysilane, tetraethoxysilane, tetrapropoxy Examples thereof include orchid and tetrabutoxysilane.

  Among the above, di-n-propyldimethoxysilane, di-iso-propyldimethoxysilane, di-n-butyldimethoxysilane, di-iso-butyldimethoxysilane, di-t-butyldimethoxysilane, di-n-butyldi Ethoxysilane, t-butyltrimethoxysilane, dicyclohexyldimethoxysilane, dicyclohexyldiethoxysilane, cyclohexylmethyldimethoxysilane, cyclohexylmethyldiethoxysilane, cyclohexylethyldimethoxysilane, cyclohexylethyldiethoxysilane, dicyclopentyldimethoxysilane, dicyclopentyldiethoxy Silane, cyclopentylmethyldimethoxysilane, cyclopentylmethyldiethoxysilane, cyclopentylethyldiethoxysilane, cyclohexylsilane B pentyl dimethoxy silane, cyclohexyl cyclopentyl distearate triethoxysilane, 3-methyl-cyclohexyl cyclopentyl dimethoxy silane, 4-methylcyclohexyl cyclopentyl dimethoxysilane, 3,5-dimethyl-cyclohexyl cyclopentyl dimethoxysilane is preferable.

  In the formula, as the organosilicon compound in which r is 1 to 4, (alkylamino) trialkylsilane, (alkylamino) dialkylcycloalkylsilane, (alkylamino) alkyldicycloalkylsilane, (alkylamino) tricycloalkylsilane , (Alkylamino) (dialkylamino) dialkylsilane, (alkylamino) (dialkylamino) dicycloalkylsilane, bis (alkylamino) dialkylsilane, bis (alkylamino) alkylcycloalkylsilane, bis (alkylamino) dicyclo Alkylsilane, bis (alkylamino) (dialkylamino) alkylsilane, bis (alkylamino) (dialkylamino) cycloalkylsilane, di (alkylamino) dialkylsilane, di (alkylamino) al Dicycloalkylsilane, di (alkylamino) dicycloalkylsilane, di (cycloalkylamino) dialkylsilane, di (cycloalkylamino) alkylcycloalkylsilane, di (cycloalkylamino) dicycloalkylsilane, tris (alkylamino) ) Alkylsilane, Tris (alkylamino) cycloalkylsilane, Tri (alkylamino) alkylsilane, Tri (alkylamino) cycloalkylsilane, Tri (cycloalkylamino) alkylsilane, Tri (cycloalkylamino) cycloalkylsilane, Tetrakis (Alkylamino) silane, tris (alkylamino) dialkylaminosilane, tris (cycloalkylamino) dialkylaminosilane, bis (dialkylamino) bis (alkylamino) Lan, dialkylaminotris (alkylamino) silane, bis (per-hydroisoquinolino) bis (alkylamino) silane, bis (perhydroquinolino) bis (alkylamino) silane, bis (cycloalkylamino) bis (alkylamino) ) Silane, tetra (alkylamino) silane, tri (alkylamino) dialkylaminosilane, tri (cycloalkylamino) dialkylaminosilane, di (dialkylamino) di (alkylamino) silane, dialkylaminotri (alkylamino) silane, di ( Alkyl-substituted per-hydroisoquinolino) di (alkylamino) silane, di (alkyl-substituted perhydroquinolino) di (alkylamino) silane, di (cycloalkylamino) di (alkylamino) silane, alkyl (dialkylamino) ) (Alkylamino) alkoxysilane, cycloalkyl (dialkylamino) (alkylamino) alkoxysilane, vinyl (dialkylamino) (alkylamino) alkoxysilane, allyl (dialkylamino) (alkylamino) alkoxysilane, aralkyl (dialkylamino) (Alkylamino) alkoxysilane, dialkyl (alkylamino) alkoxysilane and the like can be mentioned.

  The organosilicon compound (C) can be used alone or in combination of two or more. These external electron donating compounds can be used alone or in combination of two or more.

(Olefin polymer production method)
In the method for producing an olefin polymer of the present invention, olefins are polymerized or copolymerized in the presence of the olefin polymerization catalyst. Examples of olefins include ethylene, propylene, 1-butene, 1-pentene, 4-methyl-1-pentene, vinylcyclohexane, 1-hexene, 3-methyl-butene-1, and the like. It can also be used as a copolymer in combination of two or more species. Examples thereof include copolymerization of ethylene and propylene, 1-butene and 1-hexene, and copolymerization of propylene and ethylene, butene-1 and 1-hexene.

  The amount of each component used is arbitrary as long as it does not affect the effect of the present invention, and is not particularly limited. Usually, the organoaluminum compound (B) is titanium in the solid catalyst component (A). It is used in the range of 1 to 2000 mol, preferably 50 to 1000 mol, per mol of atoms. The organosilicon compound (C) is used in an amount of 0.002 to 10 mol, preferably 0.01 to 2 mol, particularly preferably 0.01 to 0.5 mol, per 1 mol of the component (B).

  The order of contacting the components is arbitrary. For example, the organoaluminum compound (B) is charged, then the external electron donating compound (C) is contacted, and the solid catalyst component (A) for olefin polymerization is further contacted. A method is mentioned.

  The polymerization method in the present invention can be carried out in the presence or absence of an organic solvent, and the olefin monomer such as propylene can be used in any state of gas and liquid. The polymerization temperature is 200 ° C. or lower, preferably 100 ° C. or lower, and the polymerization pressure is 10 MPa or lower, preferably 5 MPa or lower. Moreover, any of a continuous polymerization method and a batch type polymerization method is possible. Furthermore, the polymerization reaction may be performed in one stage or in two or more stages.

  Further, in the present invention, when polymerizing an olefin using a catalyst containing the solid catalyst component (A), the component (B), and the component (C) for olefin polymerization (also referred to as main polymerization), the catalytic activity and the steric properties are determined. In order to further improve the regularity and the particle properties of the polymer to be produced, it is desirable to perform prepolymerization prior to the main polymerization. In the prepolymerization, the same olefins as in the main polymerization or monomers such as styrene can be used.

  In carrying out the prepolymerization, the order of contacting the respective components and monomers is arbitrary, but preferably, the component (B) is first charged into the prepolymerization system set to an inert gas atmosphere or an olefin gas atmosphere, and then the olefin. After contacting the solid catalyst component (A) for homopolymerization, an olefin such as propylene and / or one or more other olefins are contacted. When the prepolymerization is performed by combining the component (C), the component (B) is first charged in the prepolymerization system set to an inert gas atmosphere or an olefin gas atmosphere, and then the component (C) is contacted. A method of contacting an olefin such as propylene and / or one or other two or more olefins after contacting the solid catalyst component (A) for olefin polymerization is desirable.

  EXAMPLES Next, although an Example is given and this invention is demonstrated further more concretely, these are only illustrations and do not restrict | limit this invention.

(Preparation of alkoxymagnesium)
Metallic magnesium with a particle size of 50-320 μm and an average particle size of 140 μm in a cylindrical flask with a capacity of 1 liter, sufficiently substituted with nitrogen gas and equipped with a stirrer, reflux condenser and integrating flow meter (M-1 SLPM manufactured by AS) A suspension was formed by charging 5 g of powder and 100 ml of dehydrated ethanol with a water content of 200 ppm. Next, 0.5 g of iodine was added, and the suspension was heated while stirring at a rotation speed of 450 rpm (n _S ³ d ² = 2.3 × 10 ⁵ ) to start the reaction under reflux of ethanol. . Stirring was performed with a lattice blade type stirring blade 15 attached to a stirring shaft 14 provided at the center of a cylindrical flask 11 having an inner diameter of 8 cm as shown in FIG. The stirring blade 15 was a single stage, and the stirring blade diameter was 5 cm. Further, the distance from the upper end of the stirring blade to the liquid level a of the suspension below it was 6 cm, and the distance from the lower end of the stirring blade to the bottom of the container was 1 cm. Thereafter, 5 g of metallic magnesium suspended in 35 ml of ethanol was added four times at 15 minute intervals. When the metal magnesium was added for the second time (reaction rate 40%), the rotational speed was reduced to 180 rpm (n _W ³ d ² = 1.5 × 10 ⁴ ). After the addition was completed, the mixture was held for 2 hours until hydrogen generation stopped while maintaining low stirring conditions. The temperature during the reaction was in the range of 75-78 ° C. After completion of the reaction, the reaction mixture was cooled to room temperature and then vacuum-dried to obtain about 98 g of spherical diethoxymagnesium. In this reaction, no aging step was performed.

  For diethoxymagnesium after drying, the particle size distribution, particle shape, amount of fine powder and bulk specific gravity were determined by the following measuring method. The results are shown in Table 1. The obtained diethoxymagnesium had a spherical shape and the surface was in the form of fine primary crystals connected in a dendritic shape.

(Particle size distribution)
Laser diffraction particle size distribution measuring apparatus (manufactured by MT3000_Nikkiso _Co.), was calculated SPAN measured _{D 50, D 10, D 90} . At the same time, the ratio of the fine powder in all the particles was determined and shown in Table 1 as the fine powder ratio.

(Particle shape)
Observation was performed with a scanning electron microscope (JSM-5310LV, manufactured by JEOL Ltd.) at acceleration voltages of 5 kV, 300 times, 1000 times, and 5000 times.
(Bulk specific gravity)
It measured according to JIS K6721.

Comparative Example 1
About 86 g of spherical diethoxymagnesium was prepared in the same manner as in Example 1 except that the rotation speed was not changed at the time of the second metal magnesium addition (reaction rate 40%). That is, in Comparative Example 1, the reaction was performed under strong stirring conditions from the beginning of the reaction until the generation of hydrogen stopped. The results are shown in Table 1.

A 20-liter stainless steel reaction vessel equipped with a stirrer, reflux condenser, and integrating flow meter (TF-600 manufactured by Tokyo Keiso Co., Ltd.) was sufficiently substituted with nitrogen gas, and had a particle size of 26 to 320 μm and an average particle size of 88 μm. A suspension was formed by charging 80 g of metal magnesium powder and 3 liters of dehydrated ethanol with a water content of 56 ppm. Next, 25 g of iodine was added, and the suspension was heated while stirring at a rotation speed of 300 rpm (n _S ³ d ² = 1.8 × 10 ⁶ ) to start the reaction under reflux of ethanol. Stirring was performed with a lattice blade type stirring blade 15 attached to a stirring shaft 14 provided at the center of a stainless steel reaction vessel 11 having an inner diameter of 27 cm as shown in FIG. The stirring blade 15 was a single stage, and the stirring blade diameter was 26 cm. Further, the distance from the upper end of the stirring blade to the liquid level a of the suspension below it was 19.5 cm, and the distance from the lower end of the stirring blade to the bottom of the container was 1.5 cm. Thereafter, a suspension in which 80 g of metallic magnesium was inserted in 0.8 liter of ethanol was added nine times at 15 minute intervals. At the time of the fourth metal magnesium addition (reaction rate 50%), the rotation speed was changed to 130 rpm. (N _W ³ d ² = 1.5 × 10 ⁵ ) After completion of the addition, the mixture was held for 2 hours until hydrogen generation stopped while maintaining low stirring conditions. The temperature during the reaction was in the range of 75-78 ° C. After completion of the reaction, the reaction mixture was cooled to room temperature and then vacuum-dried to obtain about 3.3 kg of spherical diethoxymagnesium. In this reaction, no aging step was performed. The results are shown in Table 1.

Comparative Example 2
The same procedure as in Example 2 was performed except that the rotation speed of the initial stirring blade was changed to 300 rpm instead of 330 rpm (n _S ³ d ² = 2.4 × 10 ⁶ ). That is, Comparative Example 2 is a case where stirring under strong stirring conditions is too strong. The results are shown in Table 1.

Comparative Example 3
The same procedure as in Example 2 was performed except that 140 rpm (n ³ d ² = 1.85 × 10 ⁵ ) was used instead of the blade rotation speed of 130 rpm after changing the stirring conditions. That is, Comparative Example 3 is a case where stirring under weak stirring conditions is too strong. The results are shown in Table 1.

Metallic magnesium with a particle size of 50-320 μm and an average particle size of 140 μm in a cylindrical flask with a capacity of 1 liter, sufficiently substituted with nitrogen gas and equipped with a stirrer, reflux condenser and integrating flow meter (M-1 SLPM manufactured by AS) A suspension was formed by charging 3 g of powder and 100 ml of dehydrated ethanol with a water content of 200 ppm. Next, 0.5 g of iodine was added, and the suspension was heated with stirring at a rotation speed of 200 rpm (n _S ³ d ² = 2.0 × 10 ⁴ ) to start the reaction under reflux of ethanol. . The shape of the stirring blade and the position of the stirring blade were the same as in Example 1. Thereafter, 3 g of metallic magnesium suspended in 20 ml of ethanol was added nine times at 15 minute intervals. At the time of the eighth metal magnesium addition (reaction rate 80%), the rotational speed was reduced to 120 rpm. (N _W ³ d ² = 4.3 × 10 ³ ) After completion of addition, the mixture was held for 1 hour until hydrogen generation stopped while maintaining low stirring conditions. The temperature during the reaction was in the range of 75-78 ° C. After completion of the reaction, the reaction mixture was cooled to room temperature and then vacuum-dried to obtain about 127 g of spherical diethoxymagnesium. In this reaction, no aging step was performed. The results are shown in Table 1.

Comparative Example 4
The same procedure as in Example 3 was performed except that the rotation speed of the initial stirring blade was changed to 200 rpm instead of 180 rpm (n ³ d ² = 1.5 × 10 ⁴ ). That is, Comparative Example 4 is a case where stirring under strong stirring conditions is too weak. The results are shown in Table 1. Since the particle size distribution became the W peak, the bulk density was not measured.

Comparative Example 5
The same procedure as in Example 3 was performed except that the rotation speed of the blades after changing the stirring conditions was changed to 110 rpm (n ³ d ² = 3.3 × 10 ³ ) instead of 120 rpm. That is, Comparative Example 5 is a case where stirring under weak stirring conditions is too weak. The results are shown in Table 1. Since the particle size distribution became the W peak, the bulk density was not measured.

A 20-liter stainless steel reaction vessel equipped with a stirrer, reflux condenser, and integrating flow meter (TF-600 manufactured by Tokyo Keiso Co., Ltd.) was sufficiently substituted with nitrogen gas, and had a particle size of 26 to 320 μm and an average particle size of 88 μm. A suspension was formed by charging 80 g of metal magnesium powder and 3 liters of dehydrated ethanol with a water content of 56 ppm. Next, 25 g of iodine was added, and the suspension was heated while stirring at a rotation speed of 200 rpm (n _S ³ d ² = 5.4 × 10 ⁵ ) to start the reaction under reflux of ethanol. The shape of the stirring blade and the position of the stirring blade were the same as in Example 2. Thereafter, a suspension in which 80 g of metallic magnesium was inserted in 0.8 liter of ethanol was added nine times at 15 minute intervals. At the time of the second metal magnesium addition (reaction rate 20%), the rotation speed was changed to 96 rpm. (N _W ³ d ² = 6.0 × 10 ⁴ ) After completion of the addition, the mixture was held for 2 hours until hydrogen generation stopped while maintaining low stirring conditions. The temperature during the reaction was in the range of 75-78 ° C. After completion of the reaction, the reaction mixture was cooled to room temperature and then vacuum-dried to obtain about 3.5 kg of spherical diethoxymagnesium. In this reaction, no aging step was performed. The results are shown in Table 1.

Comparative Example 6
The same procedure as in Example 4 was conducted except that the stirring rotation speed was changed at the first addition of metal magnesium (reaction rate: 10%). The results are shown in Table 1.

Metallic magnesium with a particle size of 50-320 μm and an average particle size of 140 μm in a cylindrical flask with a capacity of 1 liter, sufficiently substituted with nitrogen gas and equipped with a stirrer, reflux condenser and integrating flow meter (M-1 SLPM manufactured by AS) A suspension was formed by charging 15 g of powder and 300 ml of dehydrated ethanol with a water content of 200 ppm. Next, 0.5 g of iodine was added and the suspension was heated while stirring at a rotation speed of 350 rpm (n ³ d ² = 1.1 × 10 ⁵ ) to start the reaction under reflux of ethanol. The stirring blade shape and the stirring blade position were the same as in Example 1 except that the distance from the upper end of the stirring blade to the liquid level of the suspension below it was 2 cm, and the distance from the lower end of the stirring blade to the bottom of the container was 1 cm. Met. Thereafter, the rotational speed was reduced to 150 rpm when the integrated gas generation amount was 6.2 liters (reaction rate 90%) with a gas flow meter. (N ³ d ² = 8.4 × 10 ³ ) After changing the number of revolutions, the mixture was held for 1 hour until hydrogen generation stopped while maintaining low stirring conditions. The temperature during the reaction was in the range of 75-78 ° C. After completion of the reaction, the reaction mixture was cooled to room temperature and then vacuum-dried to obtain about 51 g of spherical diethoxymagnesium. In this reaction, no aging step was performed. The results are shown in Table 1.

  After stopping the generation of hydrogen gas, the same procedure as in Example 1 was performed except that aging was performed for 3 hours while maintaining the reaction temperature and that the rotation speed was changed 30 minutes after stopping the generation of hydrogen gas. That is, in Example 6, the stirring condition was changed at a stage where the reaction rate was 100%. The results are shown in Table 1.

The same procedure as in Example 1 was performed except that 0.075 g of TiCl ₄ was used instead of 0.5 g of iodine as a catalyst. The results are shown in Table 1.

[Preparation of solid catalyst component (A)]
A 500 ml round bottom flask fully substituted with nitrogen gas and equipped with a stirrer was charged with 10 g of diethoxymagnesium produced in Example 1, 3.2 g of di-n-butyl phthalate and 80 ml of toluene. Suspended. Next, 20 ml of titanium tetrachloride was added to the suspension solution, and the temperature was raised to 90 ° C. Thereafter, the reaction was carried out with stirring for 2 hours while maintaining a temperature of 90 ° C. After completion of the reaction, it was washed 4 times with 90 ml of toluene at 90 ° C., 20 ml of titanium tetrachloride and 40 ml of toluene were newly added, the temperature was raised to 110 ° C., and the reaction was carried out with stirring for 2 hours. After the completion of the reaction, it was washed 7 times with 70 ml of n-heptane at 40 ° C. to obtain a solid catalyst component. In addition, when the solid-liquid in this solid catalyst component was isolate | separated and the titanium content rate in solid content was measured, it was 3.1 weight%.

[Formation and polymerization of polymerization catalyst]
Into an autoclave with a stirrer having an internal volume of 2.0 liters completely replaced with nitrogen gas, 1.32 mmol of triethylaluminum, 0.13 mmol of cyclohexylmethyldimethoxysilane and 0.0026 mmol of the solid catalyst component as titanium atoms were charged, A polymerization catalyst was formed. Thereafter, 2.0 liters of hydrogen gas and 1.4 liters of liquefied propylene were charged, preliminarily polymerized at 20 ° C. for 5 minutes, then heated up, and polymerized at 70 ° C. for 1 hour. Polymerization activity per 1 g of the solid catalyst component at this time, ratio of boiling n-heptane insoluble matter in the produced polymer (HI), melt index value (MI) of the produced polymer (a), fine powder in the produced polymer Table 2 shows (105 μm or less), particle size distribution [(D ₉₀ -D ₁₀ ) / D ₅₀ ], and bulk specific gravity (BD).

The polymerization activity per solid catalyst component used here was calculated by the following equation.
Polymerization activity = produced polymer (g) / solid catalyst component (g)
Further, the ratio (HI) of boiling n-heptane insoluble matter in the produced polymer is the ratio (% by weight) of the polymer insoluble in n-heptane when this produced polymer is extracted with boiling n-heptane for 6 hours. ). Further, the melt index value (MI) of the produced polymer (a) was measured according to ASTM D 1238 and JIS K 7210. The bulk specific gravity (BD) of the polymer was measured according to JIS K6721.

Comparative Example 7
A solid catalyst component and a catalyst were prepared and polymerized in the same manner as in Example 8 except that the alkoxymagnesium obtained in Comparative Example 1 was used. The obtained results are shown in Table 2.

Examples 9-14, Comparative Examples 8-12
[Preparation of solid catalyst component (A)]
A solid catalyst component was obtained in the same manner as in Example 8 except that diethoxymagnesium produced in Examples 2-7 and Comparative Examples 1-6 were used. That is, Example 9 uses the diethoxymagnesium of Example 2, Example 3 is Example 10, and Example 4 is Example 11. The same applies hereinafter. Moreover, the thing using the diethoxy magnesium of the comparative example 2 is the comparative example 8, the thing of the comparative example 3 is the comparative example 9, and the thing of the comparative example 4 is the comparative example 10. The same applies hereinafter.

[Formation and polymerization of polymerization catalyst]
Polymerization was carried out in the same manner as in Example 8 to obtain a produced polymer. Table 2 shows the activity, HI, MI, particle size distribution, fine powder amount, and BD.

It is a flowchart figure which shows the process of preparing the polymerization catalyst of this invention. It is an example of the stirring tank and stirring blade used with the synthesis | combining method of this invention. It is a figure of the stirring tank and stirring blade used in the Example.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Stirring tank 2 Lower wing 3 Upper wing 4 Rotating shaft 5 Stirring wing

Claims (6)

In the method of synthesizing solid alkoxymagnesium by reacting metallic magnesium and alcohol with stirring in the presence of halogen or a halogen-containing compound in a stirring vessel, the stirring is performed in the following (I) to (III);
(I) Stir with a stirring blade attached to a stirring shaft provided at the center of the stirring tank;
(II) During the reaction, the stirring is changed from the following strong stirring condition to the following weak stirring condition at a stage where the reaction rate of metal magnesium becomes 20% or more;
1.9 × 10 ⁴ ≦ n _S ³ d ² (strong stirring condition) ≦ 1.9 × 10 ⁶
4.0 × 10 ³ ≦ n _W ³ d ² (weak stirring conditions) ≦ 1.7 × 10 ⁵
(In the formula, d is the stirring blade diameter (m), and n _S and n _W are the number of rotations per minute.)
(III) In the above (II), n _S ³ d ² > n _W ³ d ² and n _S > 1.4 n _W ;
A process for synthesizing alkoxymagnesium, which is carried out under the following conditions:   The method for synthesizing alkoxymagnesium according to claim 1, wherein 0.0003 mol or more of halogen or halogen compound is present per 1 mol of metal magnesium.   The method for synthesizing alkoxymagnesium according to claim 1, wherein the halogen is iodine.   2. The method for synthesizing alkoxymagnesium according to claim 1, wherein the halogen compound is a titanium chloride. Metallic magnesium and alcohol are reacted in the presence of a halogen or a halogen-containing compound in a stirring vessel with stirring under the following stirring conditions (I) to (III) to synthesize a solid alkoxymagnesium. A method for producing a solid catalyst component for olefin polymerization, comprising contacting alkoxymagnesium (a) with a halogen-containing titanium compound (b).
(I) Stir with a stirring blade attached to a stirring shaft provided at the center of the stirring tank;
(II) During the reaction, the stirring is changed from the following strong stirring condition to the following weak stirring condition at a stage where the reaction rate of metal magnesium becomes 20% or more;
1.9 × 10 ⁴ ≦ n _S ³ d ² (strong stirring condition) ≦ 1.9 × 10 ⁶
4.0 × 10 ³ ≦ n _W ³ d ² (weak stirring conditions) ≦ 1.7 × 10 ⁵
(In the formula, d is the stirring blade diameter (m), and n _S and n _W are the number of rotations per minute.)
(III) In the above (II), n _S ³ d ² > n _W ³ d ² and n _S > 1.4 n _W ; Metallic magnesium and alcohol are reacted in the presence of a halogen or a halogen-containing compound in a stirring vessel with stirring under the following stirring conditions (I) to (III) to synthesize a solid alkoxymagnesium. The alkoxymagnesium (a) and the halogen-containing titanium compound (b) are contacted to obtain a solid catalyst component for olefin polymerization, and (A) the solid catalyst component for olefin polymerization and (B) the following general formula (1) ;
R ¹ _p AlQ _3-p (1)
(In the formula, R ¹ represents an alkyl group having 1 to 4 carbon atoms, Q is a hydrogen atom or a halogen atom, p is 0 <a real number p ≦ 3.) Contacting an organoaluminum compound represented by A process for producing a catalyst for olefin polymerization.
(I) Stir with a stirring blade attached to a stirring shaft provided at the center of the stirring tank;
(II) During the reaction, the stirring is changed from the following strong stirring condition to the following weak stirring condition at a stage where the reaction rate of metal magnesium becomes 20% or more;
1.9 × 10 ⁴ ≦ n _S ³ d ² (strong stirring condition) ≦ 1.9 × 10 ⁶
4.0 × 10 ³ ≦ n _W ³ d ² (weak stirring conditions) ≦ 1.7 × 10 ⁵
(In the formula, d is the stirring blade diameter (m), and n _S and n _W are the number of rotations per minute.)
(III) In the above (II), n _S ³ d ² > n _W ³ d ² and n _S > 1.4 n _W ;

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