Production of a catalyst component for producing crystalline polymers

Abstract: A process for the production of a supported type titanium catalyst component for producing olefin polymers comprises subjecting a solid product (I) obtained by contacting a liquefied magnesium compound with a depositing agent, a halogen compound, an electron donor and a titanium compound (T₁) to a multi-stage polymerization treatment once or more each with (1) a linear olefin and (2) a non-linear olefin in the presence of an organoaluminum compound to form a linear olefin/non-linear olefin block copolymer as a solid product (II); and reacting a halogenated titanium compound (T₂) with the solid product (II); the content of the olefin polymer block in the supported type titanium catalyst component being from 0.1 to 49.5% by weight, that of the non-olefin polymer block being from 0.01 to 49.5% by weight, and the weight ratio of the linear olefin polymer block to the non-linear olefin polymer block being 2/98 to 98/2.

Description: This invention relates to a catalyst component which may be used for producing highly crystalline olefin polymers and to a process for producing the catalyst. More particularly, the invention relates to a catalyst component suitable for producing highly crystalline olefin polymers from which a film having improved transparency and very few voids is afforded. it is well known that crystalline olefin polymers, such as crystalline polypropylene, may be obtained by polymerizing olefins by means of so-called Ziegler-Natta catalysts comprising a compound of a transition metal of Groups IV to VI of the Periodic Table and an organometal compound of a metal of Groups I to III of the Table. As the transition metal compound, various titanium trichloride compositions have been particularly widely used. Among these titanium trichloride compositions, those of the type obtained by reducing TiCℓ 4 with an organoaluminum compound, followed by heat treatment, afford a polymer having a good form; and thus many processes for producing the above type compositions have been suggested. For example, a process of reducing TiCℓ 4 with an organoaluminium compound, followed by treating the resulting titanium trichloride with an electron donor and TiCℓ 4 to thereby enhance the catalyst activity and reduce the quantity of amorphous polymers formed (see Japanese Patent Publication No. Sho 53-3,356/1978) and like processes have been proposed. We have already proposed a number of processes in this field. Of these, the following processes have led to improvements in the storage stability of titanium trichloride compositions, the polymerization activity and the crystallinity of the resulting olefin polymers, a process of producing olefin polymers using a titanium trichloride composition obtained by reacting TiCℓ 4 with a reaction product of an organoaluminum compound with an electron donor, followed by reacting the resulting solid with an electron donor and an electron acceptor (Japanese Patent Publication No. Sho 59-28,573/1984), and a process of producing olefin polymers using a titanium trichloride composition obtained by reacting TiCℓ 4 with a reaction product of an organoaluminum compound with an electron donor, followed by subjecting the resulting solids to polymerization treatment with an olefin and reacting the resulting material with an electron donor and an electron acceptor (JP-A-58-17,104/1983). Further, in recent years, there has been widely investigated a process for producing olefin polymers which comprises using a titanium-containing solid catalyst component containing Ti, Mg, a halogen an electron donor, which component exhibits a very high polymerization activity while retaining a high stereoregularity, and polymerizing olefins in the presence of a catalyst obtained by combining the above solid catalyst component, an organoaluminum compound and an electron donor together (See, for example, JP-A-58-83,006/1983). We have also already proposed a number of processes in this field. For example, we have disclosed processes for producing olefin polymers having a high stereoregularity and a good particle form with a high polymerization activity (see, for example JP-A-61-209,207/1986, JP-A-62-104,810/1987, JP-A-62-104,811/1987, JP-A-62-104,812/1987, and JP-A-62-104,813/1987). However, while these improved processes have the above-mentioned advantages, films prepared the resulting polyolefins are translucent so that the commodity value is often damaged depending on the intended fields of use. Thus, an improvement in the transparency would be desirable. Various proposals have been made for improving the transparency of films prepared from olefin polymers. For example, processes of adding a nucleating agent, such as an aluminum salt of an aromatic carboxylic acid (Japanese patent publication No. SHo. 40-1,652/1965), benzylidene sorbitol derivatives (JP-A-51-22,740/1976) to polypropylene have been proposed. However, when aluminium salts of aromatic carboxylic acids are used, their dispersibility in the resulting polymer is not only inferior, but also the effectiveness of improvement in the transparency of the resulting film is insufficient, while when benzylidene sorbitol derivatives are used, a definite improvement in the transparency is observed, but there are the problems that their smell at the time of processing is strong and a bleeding phenomenon (exudation) occurs. For solving the above-mentioned problem at the time of addition of nucleating agents, there have been proposed processes of polymerizing propylene using a catalyst obtained by polymerizing a small quantity of vinylcyclohexane, p-t-butylstyrene, allyltrimethylsilane or 4,4-dimethylpentene-1, followed by preactivation treatment (see JP-A-60-139,710/1985, JP-A-63-15,803/1988, JP-A-63-15,804/1988, JP-A-63-218,709/1988). We have produced polypropylene according to the proposed processes, and as a result found that in any of the processes, not only is the polymerization activity to propylene lowered, but also there occurred operational problems such as formation of bulk polymer, scale adhesion onto the wall of polymerization vessels and inferior controllability of polymerization reaction. Thus these processes could not be employed for commercial, long term, continuous polymerization, particularly in the case of gas phase polymerization process wherein olefin polymerization was carried out. Further, when the resulting polypropylene was processed into film, a definite improvement in the transparency was observed, but a large number of voids occurred in the film to thereby damage its value. Further, as a similar technique, there has been proposed a process of polymerizing propylene using a transition metal catalyst component having vinylcyclohexane polymer or allyltrimethylsilane polymer added midway during the preparation of the component (see JP-A-63-69,809/1988). However, since the proposed process requires a separate step for preparing the vinylcyclohexane polymer or allyltrimethylsilane polymer, not only are there commercial disadvantages but also there has been raised the above-mentioned problem that voids occur in the resulting film, as observed in the prior art. We have now found, in accordance with the present invention, that a titanium trichloride composition or a supported type titanium catalyst component, each having a linear olefin/non-linear olefin block copolymer as hereinafter described may be used to provide improved crystalline polyolefins. The invention provides a process for producing a supported type titanium catalyst component for producing olefin polymers, which process comprises subjecting a solid product (I) obtained by contacting a liquefied magnesium compound with a depositing agent, a halogen compound, an electron donor and a titanium compound (T 1 ) to a multi-stage polymerization treatment once or more each with (1) a linear olefin and (2) a non-linear olefin in the presence of an organo- aluminium compound to form a linear olefin/non-linear olefin block copolymer as a solid product (II); and reacting a halogenated titanium compound (T 2 ) with said solid product (II), the content of said linear olefin polymer block in the supported type titanium catalyst component being 0.1 to 49.5% by weight, that of said non-linear olefin polymer block being 0.01 to 49.5% by weight, and the weight ratio of the linear olefin polymer block to the non-linear olefin polymer block being 2/98 to 98/2. In the above process the organoaluminium compound is preferably one of the formula: A1R 8 ℓ R 9 ℓ' X 3 - (ℓ+ℓ') in which R 8 and R 9 each represent a hydrocarbon radical selected from the group consisting of alkyl groups, a cycloalkyl groups and aryl groups, or an alkoxy group; X is a halogen atom and ℓ and ℓ' are each numbers together satisfying the relationship. 0 < ℓ + ℓ' ≤ 3. The non-linear olefin is preferably one of the formula:- or in which R 2 , R 3 , R 4 , R 5 , R 6 , R 7 , n and m have the meanings defined below. BRIEF DESCRIPTION OF THE DRAWING Fig. 1 shows a chart of production steps (flowsheet) of the catalyst component, for illustrating the process of the present invention. Next, the constitutions of the present invention will be described in more detail. The titanium catalyst component for olefin polymerization of the present invention is directed to a supported type titanium catalyst component comprising a linear olefin-non-linear olefin block copolymer (hereinafter often abbreviated to a specified block copolymer) containing at least one linear olefin polymer block and at least one non-linear olefin polymer block and titanium, magnesium, a halogen and an electron donor as indispensable components, and a process for producing the supported type titanium catalyst component will be described below. Further, the "liquefaction" of magnesium compound referred to herein includes not only a case where the compound itself forms a liquid, but also a case where the compound itself is soluble in a solvent to form a solution and a case where the compound reacts with another compound or forms a complex therewith so that the resulting material is solubilized in a solvent to form a solution. Further, the solution may be that in a state where a colloid form or semi-dissolved form substance is contained, besides that in a state where the compound is completely dissolved. As the magnesium compound to be liquefied, it may be any of those which form the above-mentioned "liquefied" state. Examples of such compounds are magnesium dihalides, alkoxymagnesium halides, aryloxymagnesium halides, dialkoxymagnesiums, diaryloxymagnesiums, magnesium oxyhalides, magnesium oxide, magnesium hydroxide, magnesium carboxylates, dialkylmagnesiums and alkylmagnesium halides, and besides, metal magnesium may also be used. Further, besides these magnesium compounds or metal magnesium, reaction products thereof with an electron donor, a silicon compound or an aluminum compound may also be used. As a process for liquefying magnesium compounds, known processes may be employed. Examples thereof are a process of liquefying magnesium compounds with an alcohol, an aldehyde, an amine or a carboxylic acid (Japanese patent application laid-open No. Sho 56-811/1981), a process of liquefying with an o-titanic acid ester (Japanese patent application laid-open No. Sho 54-40,293/1979), a process of liquefying with a phosphorus compound (Japanese patent application laid-open No. Sho 58-19,307/1983), and combinations of these processes. Further, as to organomagnesium compounds having a C-Mg bond which cannot be applied to the above processes, since the compounds are soluble in ether, dioxane, pyridine, etc., they may be used in the form of solution thereof in such solvents, or they may be reacted with an organometal compound to form a complex compound expressed by the formula M p Mg q R 10 r R 11 s (wherein M represents Aℓ, Zn, B or Be atom, R 10 and R 11 each represent a hydrocarbon radical, p, q, r and s each are larger than 0 and when the valency of M is denoted by v, then r, s, v, p and q have a relationship of r+s=vp+2q) (Japanese patent application laid-open No. Sho 50-139,885/1975), followed by dissolving the compelx compound in a hydrocarbon solvent to effect liquefaction. Further, in the case where metal magnesium is used, liquefaction may be carried out according to a process of liquefying it with an alcohol and an o-titanic acid ester (Japanese patent application laid-open No. Sho 51-51,587/1975) or a process of reacting it with a halogenated alkyl in ether to form the so-called Grignard reagent. Among the above-mentioned processes of liquefying a magnesium compound, for example, a case where magnesium chloride is dissolved in an inert hydrocarbon solvent (D 1 ) using a titanic acid ester and an alcohol will be illustrated. 0.1 to 2 Mols of a titanic acid ester, 0.1 to 5 mols of an alcohol and 0.1 to 5 ℓ of a solvent (D 1 ) each per mol of magnesium chloride are mixed in an optional addition order, followed by heating the resulting suspension with stirring to 40° to 200°C, preferably 50° to 150°C. The time required for the reaction and dissolution is 5 minutes to 7 hours, preferably 10 minutes to 5 hours. The titanic acid ester refers to an o-titanic acid ester expressed by Ti(OR 12 ) 4 and a polytitanic acid ester expressed by wherein R 12 , R 13 , R 14 , R 15 and R 16 each represent an alkyl group of 1 to 20 carbon atoms or a cycloalkyl group of 3 to 20 carbon atoms and t represents an integer of 2 to 20. Concrete examples thereof are o-titanic acid esters such as methyl o-titanate, ethyl o-titanate, n-propyl o-titanate, i-propyl o-titanate, n-butyl o-titanate, i-butyl o-titanate, n-amyl o-titanate, 2-ethylhexyl o-titanate, n-octyl o-titanate, phenyl o-titanate and cyclohexyl o-titanate, and polytitanic acid esters such as methyl polytitanate, ethyl polytitanate, n-propyl polytitanate, i-propyl polytitanate, n-butyl polytitanate, i-butyl polytitanate, n-amyl polytitanate, 2-ethylhexyl polytitanate, n-octyl polytitanate, phenyl polytitanate and cyclohexyl polytitanate. The quantity of the polytitanic acid ester used may be that corresponding to the o-titanic acid ester as calculated in terms of o-titanic acid ester units. As the alcohol, aliphatic saturated or unsaturated alcohols may be used. Concrete examples are monohydric alcohols such as methanol, ethanol, n-propanol, i-propanol, n-butanol, n-amyl alcohol, i-amyl alcohol, n-hexanol, n-octanol, 2-ethylhexanol or allyl alcohol and polyhydric alcohols such as ethylene glycol, trimethylene glycol or glycerine. Among these, aliphatic saturated alcohols of 4 to 10 carbon atoms are preferred. Examples of the inert hydrocarbon solvent (D 1 ) are aliphatic hydrocarbons such as pentane, hexane, heptane, nonane, decane or kerosine, aromatic hydrocarbons such as benzene, toluene or xylene, halogenated hydrocarbons such as carbon tetrachloride, 1,2-dichloroethane, 1,1,2-trichloroethane, chlorobenzene or o-dichlorobenzene. Among these, aliphatic hydrocarbons are preferred. The solid product (I) is obtained by contacting the above liquefied magnesium compound with a depositing agent (X 1 ), a halogenated compound (X 2 ), an electron donor (B 1 ) and a titanium compound (T 1 ). Examples of the depositing agent (X 1 ) are halogenating agents such as halogens, halogenated hydrocarbons, halogen-containing silicon compounds, halogen-containing aluminum compounds, halogen-containing titanium compounds, halogen-containing zirconium compounds or halogen-containing vanadium compounds. Further, in the case where the liquefied magnesium compounds are the above-mentioned organomagnesium compounds, it is also possible to use active hydrogen-containing compounds such as alcohols or Si-H bond-containing polysiloxanes. The quantity of these depositing agents (X 1 ) used is 0.1 to 50 mols per mol of magnesium compounds. Further, examples of the halogen compound (X 2 ) are halogens and halogen-containing compounds, and compounds similar to the halogenating agents illustrated as examples of the depositing agent are usable, and in the case where halogenating agents are used as the depositing agent, it is not always necessary to newly use the halogen compound (X 2 ). The quantity of the halogen compound (X 2 ) used is 0.1 to 50 mols per mol of the magnesium compound. Examples of the electron donor (B 1 ) are oxygen-containing electron donors such as alcohols, phenols, ketones, aldehydes, carboxylic acids, organic or inorganic acid esters, ethers, acid amides or acid anhydrides, nitrogen-containing electron donors such as ammonia, amines, nitriles or isocyanates, and phosphorus-containing electron donors such as phosphines, phosphites or phosphinites. Concrete examples are alcohols such as methanol, ethanol, n-propanol, i-propanol, n-butanol, pentanol, hexanol, octanol, 2-ethylhexanol, allyl alcohol, benzyl alcohol, ethylene glycol or glycerine, phenols such as phenol, cresol, xylenol or ethylphenol, ketones such as acetone, methyl ethyl ketone, methyl isobutyl ketone, acetophenone or benzophenone, aldehydes such as acetaldehyde, propionaldehyde or benzaldehyde, carboxylic acids such as formic acid, acetic acid, propionic acid, butyric acid or valeic acid, aliphatic carboxylic acid esters such as methyl formate, methyl acetate, methyl butyrate, ethyl acetate, vinyl acetate, n-propyl acetate, i-propyl acetate, n-butyl acetate, octyl acetate, phenyl acetate or ethyl propionate, aromatic monocarboxylic acid esters such as methyl benzoate, ethyl benzoate, methyl toluylate, ethyl toluylate, methyl anisate, ethyl anisate or phenyl anisate, aromatic polybasic carboxylic acid esters such as monomethyl phthalate, dimethyl phthalate, diethyl phthalate, di-n-propyl pthalate, mono-n-butyl phthalate, di-n-butyl phthalate, di-i-butyl phthalate, di-n-heptyl phthalate, di-2-ethylhexyl phthalate, di-n-octyl phthalate, diethyl isophthalate, dipropyl isophthalate, dibutyl isophthalate, di-2-ethylhexyl isophthalate, diethyl terephthalate, dipropyl terephthalate, dibutyl terephthalate or di-i-butyl naphthalenecarboxylate, ethers such as methyl ether, ethyl ether, isopropyl ether, butyl ether, amyl ether, tetrahydrofuran, anisole or diphenyl ether, acid amides such as acetic acid amide, benzoic acid amide, toluic acid amide, acid anhydrides such as acetic anhydride, maleic anhydride benzoic anhydride, phthalic anhydride or tetrahydrophthalic anhydride, amines such as ethylamine, tributylamine, aniline, pyridine, picoline or tetramethylethylenediamine, nitriles such as acetonitrile or benzonitrile, phosphines such as ethylphosphine, triethylphosphine, tri-n-butylphosphine or triphenylphosphine, phosphites such as dimethylphosphite, triethylphosphite, triphenylphosphite, phosphinites such as ethyldiethylphosphinite or ethylbutylphosphinite, alkoxysilanes such as tetraethoxysilane or tetrabutoxysilane, and preferably, aromatic monocarboxylic acid esters, aromatic polybasic carboxylic acid esters and alkoxysilanes, and more preferably, aromatic polybasic carboxylic acid esters are used. As to these electron donors (B 1 ), one or more kinds are used and the quantity thereof used is 0.01 to 5 mols per mol of the magnesium compound. As the titanium compound (T 1 ) necessary for preparing the solid product (I), there are used halogenated titanium compounds expressed by the formula Ti(OR 17 ) 4-u X u wherein R 17 represents an alkyl group, a cycloalkyl group or an aryl group, X represents a halogen atom and u represents an optional number satisfying an expression of 0<u≦4, and o-titanic acid esters and polytitanic acid esters illustrated at the time of the above-mentioned liquefaction of magnesium compounds. Concrete examples of the halogenated titanium compounds are TiCℓ 4 , TiBr 4 , methoxytitanium trichloride, ethoxytitanium trichloride, propoxytitanium trichloride, butoxytitanium trichloride, phenoxytitanium trichloride, ethoxytitanium tribromide, butoxytitanium tribromide, dimethoxytitanium dichloride, diethoxytitanium dichloride, dipropoxytitanium dichloride, dibutoxytitanium dichloride, diphenoxytitanium dichloride, diethoxytitanium dibromide, dibutoxytitanium dibromide, trimethoxytitanium chlofide, triethoxytitanium chloride, tributoxytitanium chloride and triphenoxytitanium chloride. As the o-titanic acid esters and polytitanic acid esters, the same as those already mentioned are exemplified. As to these titanium compounds (T 1 ), one or more kinds are used, and in the case where halogenated titanium compounds are used as the titanium compound (T 1 ), since they contain a halogen, the depositing agent (X 1 ) and the halogenated compound (X 2 ) are optionally used. Further, in the case where a titanic acid ester is used at the time of liquefying the magnesium compound, new use of the titanium compound (T 1 ) is also optional. The quantity of the titanium compound (T 1 ) used is 0.1 to 100 mols per mol of the magnesium compound. The above-mentioned liquefied magnesium compound, depositing agent (X 1 ), halogenated compound (X 2 ), electron donor (B 1 ) and titanium compound (T 1 ) are contacted with stirring to obtain the solid product (I). At the time of the contact, an inert hydrocarbon (D 2 ) may be used and the respective components may be diluted in advance and used. As the inert hydrocarbon solvent (D 2 ), those similar to the above (D 1 ) may be illustrated. The quantity thereof used is 0 to 5,000 mℓ per mol of the magnesium compound. The process of the contact includes various ones such as 1 ○ a process of adding (X 1 ) to a liquefied magnesium compound to deposit solids and contacting (X 2 ), (B 1 ) and (T 1 ) with the solids in an optional order; 2 ○ a process of adding (X 1 ) to a solution obtained by contacting a liquefied magnesium compound with (B 1 ) to deposit solids and contacting (X 2 ) and (T 1 ) with the solids in an optional order, 3 ○ a process of contacting a liquefied magnesium compound with (T 1 ), followed by adding (X 1 ) and further contacting (B 1 ) and (X 2 ) with the mixture in an optional order, or the like processes. While the quantities of the respective components used are in the above-mentioned ranges, these components may be used at a time or at several separated stages. Further, in the case where one component contains an atom or a group characterizing another component, as already described above, it is not alway necessary to newly use the other component. For example, in the case where a titanic acid ester is used at the time of liquefying a magnesium compound, (T 1 ) constitutes an optional component to be used, and similarly, in the case where a halogen-containing titanium compound is used as the depositing agent (X 1 ), (X 2 ) and (Ti) constitute optional components to be used, and in the case where a halogenating agent is used as the depositing agent (X 1 ), (X 2 ) constitutes an optional component to be used. The contact temperature of the respective components is -40° to +180°C, preferably -20° to +150°C, and the contact time thereof is 5 minutes to 8 hours, preferably 10 minutes to 6 hours at each stage, under the atmospheric pressure (0.1 MPa) to 10 Kg/cm 2 G (1.08 MPa). A solid product (I) is obtained in the above contact reaction. The solid product (I) may be successively subjected to the subsequent stage, but it is preferred to wash the product with an inert solvent as already mentioned, in advance. The solid product (I) obtained according to the above process is then subjected to a multi-stage polymerization treatment with 1 ○ a linear olefin and 2 ○ a non-linear olefin in the presence of an organoaluminum compound (AL 1 ) to obtain a solid product (II). As to this multi-stage polymerization treatment, either one of the linear olefin or the non-linear olefin may be used in in advance, but it is preferred to subject the product to the polymerization treatment first with 1 ○ the linear olefin and successively with 2 ○ the non-linear olefin, in the aspect of the polymerization operation properties at the time of use of the resulting final titanium catalyst component as well as in the aspect of the quality of the resulting olefin polymer. A linear olefin-non-linear olefin block copolymer is formed by the multi-stage polymerization treatment, and the solid product (I) results in a state where it is coated with the block copolymer. In order to obtain the titanium catalyst component achieving the object of the present invention, the multi-stage polymerization treatment may be carried out each at least once using each of the linear olefin and the non-linear olefin, as described above, but it is also possible to carry out the polymerization treatment twice or more, for example, by carrying out polymerization treatment with the non-linear olefin, followed by further adding 3 ○ a linear olefin to carry out polymerization treatment. As to the conditions of the multi-stage polymerization treatment, adding 100 to 5,000 mℓ of an inert hydrocarbon solvent (D 3 ) and 0.5 to 5,000 g of an organoaluminum compound (AL 1 ) to 100 g of a solid product (I), under conditions of a reaction temperature of 0° to 90°C, a reaction time of one minute to 10 hours and a reaction pressure of the atmospheric pressure (0.1 MPa, 0 Kgf/cm 2 G) to 10 Kgf/cm 2 G (1.08 MPa) and using 0.1 g to 100 Kg of a linear olefin and 0.01 g to 100 Kg of a non-linear olefin per 100 g of the solid product (II), a multi-stage polymerization treatment is carried out so as to give a content of the linear olefin polymer block in the final solid product (III), i.e. the supported type titanium catalyst component, of 0.1 to 49.5% by weight and a content of the non-linear olefin polymer block therein of 0.01 to 49.5% by weight, and so as to give a ratio by weight of the linear olefin polymer block to the non-linear olefin polymer block, of 2/98 to 98/2. If the content of the linear olefin polymer block is less than 0.1% by weight, improvement in the operation properties at the time of using the resulting titanium catalyst component as well as the effect of inhibiting the resulting olefin polymer from forming voids are both insufficient, while even if it exceeds 49.5% by weight, improvement in the effects is not notable, resulting in operational and economical disadvantages. Further, if the content of the non-linear olefin polymer block is less than 0.01% by weight, the effect of improving the transparency, when the resulting polymer is made into film, is insufficient, while if it exceeds 49.5% by weight, improvement in the effects is not notable, resulting in operational and economical disadvantages. Further, the ratio by weight of the linear olefin polymer block to the non-linear olefin block is preferred to be 2/98 to 98/2, in the aspect of balance between the improvement effect of the operation properties and that of the transparency. In addition, in the above multi-stage polymerization treatment, after the polymerization treatment with the linear olefin or the non-linear olefin at the respective stages has been completed, it is possible to use the resulting reaction mixture, as it is, for the polymerization treatment at the subsequent stage. Further, it is also possible to remove the coexisting solvent, unreacted linear olefin or non-linear olefin and organoaluminum compound (AL 1 ), by filtering off or decantation, again add a solvent and an organoaluminum compound (AL 1 ) and use the resulting mixture for polymerization treatment with a non-linear olefin or a linear olefin at the succeeding stage. Further, at the stage of the polymerization treatment, it is also possible to make coexistent a carboxylic acid ester such as ethyl benzoate, methyl toluylate or ethyl anisate or an electron donor (B 2 ) represented by phenyltriethoxysilane, diphenyldimethoxysilane or methyltriethoxysilane. The quantity thereof used is 0 to 5,000 g per 100 g of the solid product (I). The organoaluminum compound (AL 1 ) used for the polymerization treatment is expressed by the formula AℓR 8 ℓ R 9 ℓ X 3-(ℓ+ℓ') wherein R 8 and R 9 each represent a hydrocarbon radical such as an alkyl group, a cycloalkyl group, an aryl group, etc., X represents a halogen atom and ℓ and ℓ' each represent an optional number satisfying an expression of 0<ℓ+ℓ'≦3. Concrete examples of the organoaluminum compound are trialkylaluminums such as trimethylaluminum, triethylaluminum, tri-n-propylaluminum, tri-n-butylaluminum, tri-i-butylaluminum, tri-n-hexylaluminum, tri-i-hexylaluminum, tri-2-methylpentylaluminum, tri-n-octylaluminum or tri-n-decylaluminum, dialkylaluminum monohalides such as diethylaluminum monochloride, di-n-propylaluminum monochloride, di-i-butylaluminum monochloride, diethylaluminum monofluoride, diethylaluminum monobromide or diethylaluminum monoiodide, dialkylaluminum hydrides such as diethylaluminum hydride, aluminum sesqui halides such as methylaluminum sesquichloride or ethylaluminum sesquichloride, and monoalkylaluminum dihalides such as ethylaluminum dichloride or i-butylaluminum dichloride, and besides, alkoxyalkylaluminums such as monoethoxydiethylaluminum or diethoxymonoethylaluminum may also be used. These organoaluminum compounds may be used in admixture of two or more kinds. As the solvent (D 3 ), inert hydrocarbon solvents same as the (D 1 ) and (D 2 ) already mentioned may be illustrated. Examples of the linear olefin used for the polymerization treatment of the present invention are those such as ethylene, propylene, butene-l, pentene-1 or hexene-1, and particularly, ethylene and propylene are preferably used. These linear olefins may be used alone or in admixture. The non-linear olefin preferably used for the polymerization treatment in the present invention is as follows: 1 ○ saturated ring-containing hydrocarbon monomers of 3 to 18 carbon atoms expressed by the formula CH 2 =CH-R 1 wherein R 1 represents a saturated ring-containing hydrocarbon monomer which has a saturated ring-containing structure of a hydrocarbon which may contain silicon and may contain silicon; 2 ○ branched olefins expressed by the formula wherein R 2 represents a linear hydrocarbon radical of 1 to 3 carbon atoms which may contain silicon or silicon, R 3 , R 4 and R 5 each represent a linear hydrocarbon radical of 1 to 6 carbon atoms which may contain silicon, but either one of R 3 , R 4 and R 5 may be hydrogen atom; and 3 ○ aromatic monomers expressed by the formula wherein n represents 0 or 1, m represents 1 or 2, R 6 represents a linear hydrocarbon radical of 1 to 6 carbon atoms which may contain silicon and R 7 represents a hydrocarbon radical of 1 to 12 carbon atoms which may contain silicon, hydrogen atom or a halogen atom and when m represents 2, the respective R 7 s may be the same or different. Concrete examples of the saturated ring-containing hydrocarbon monomers 1 ○ are vinylcycloalkanes such as vinylcyclopropane, vinylcyclobutane, vinylcyclopentane, 3-methylvinylcyclopentane, vinylcyclohexane, 2-methylvinylcyclohexane, 3-methylvinylcyclohexane, 4-methylvinylcyclohexane or vinylcycloheptane, allylcycloalkanes such as allylcyclopentane or allylcyclohexane, and besides, saturated ring-containing hydrocarbon monomers having silicon atom in the saturated ring-structure such as cyclotrimethylenevinylsilane, cyclotrimethylenemethylvinylsilane, cyclotetramethylenevinylsilane, cyclotetramethylenemethylvinylsilane, cyclopentamethylenevinylsilane, cyclopentamethyleneethylvinylsilane, cyclohexamethylenevinylsilane, cyclohexamethylenemethylvinylsilane, cyclohexamethyleneethylvinylsilane, cyclotetramethyleneallylsilane, cyclotetramethylenemethylallylsilane, cyclopentamethyleneallylsilane, cyclopentamethylenemethylallylsilane or cyclopentamethyleneethylallylsilane, saturated ring-containing hydrocarbon monomers having silicon atom outside the saturated ring structure such as cyclobutyldimethylvinylsilane, cyclopentyldimethylvinylsilane, cyclopentylethylmethylvinylsilane, cyclopentyldiethylvinylsilane, cyclohexylvinylsilane, cyclohexyldimethylvinylsilane, cyclohexylethylmethylvinylsilane, cyclobutyldimethylallylsilane, cyclopentyldimethylallylsilane, cyclohexylmethylallylsilane, cyclohexyldimethylallylsilane, cyclohexylethylmethylallylsilane, cyclohexyldiethylallylsilane, 4-trimethylsilylvinylcyclohexane or 4-trimethylsilylallylcyclohexane. Concrete examples of the branched olefins 2 ○ are 3-position-branched olefins such as 3-methylbutene-1, 3-methylpentene-1 or 3-ethylpentene-1, 4-position-branched olefins such as 4-ethylhexene-1, 4,4-dimethylpentene-1 or 4,4-dimethylhexene-1, alkenylsilanes such as vinyltrimethylsilane, vinyltriethylsilane, vinyltri-n-butylsilane, allyltrimethylsilane, allylethyldimethylsilane, allyldiethylmethylsilane, allyltriethylsilane, allyl-n-propylsilane, 3-butenyltrimethylsilane or 3-butenyltriethylsilane, diallylsilanes such as dimethyldiallylsilane, ethylmethyldiallylsilane or diethyldiallylsilane. Further, concrete examples of the aromatic monomers 3 ○ are styrene, as its derivatives, alkylstyrenes such as o-methylstyrene, p-t-butylstyrene, dialkylstyrenes such as 2,4-dimethylstyrene, 2,5-dimethylstyrene, 3,4-3,5-dimethylstyrene or 3, 5-dimethylstyrene, halogen-substituted styrenes such as 2-methyl-4-fluorostyrene, 2-ethyl-4-chlorostyrene, o-fluorostyrene or p-fluorostyrene, trialkylsilylstyrenes such as p-trimethylsilylstyrene, m-triethylsilylstyrene or p-ethyldimethylsilylstyrene, allyltoluenes such as o-allyltoluene or p-allyltoluene, allylxylenes such as 2-allyl-p-xylene, 4-allyl-o-xylene or 5-allyl-m-xylene, alkenylphenylsilanes such as vinyldimethylphenylsilane, vinylethylmethylphenylsilane, vinyldiethylphenylsilane, allyldimethylphenylsilane or allylethylmethylphenylsilane, or 4-(o-tolyl)-butene-1, 1-vinylnaphthalene. These non-linear olefins may be used alone or in admixture. As described above, the multi-stage polymerization treatment is carried out with a linear olefin and a non-linear olefin and the resulting material is washed with an inert hydrocarbon solvent as already mentioned to obtain the solid product (II). Successively, a halogenated titanium compound (T 2 ) is reacted with the solid product (II) to obtain a titanium catalyst component containing a specified silicon-containing polymer. As the halogenated titanium compound (T 2 ), there is used a halogenated titanium compound expressed by the formula Ti(OR 17 ) 4-u X u (wherein R 17 represents an alkyl group, a cycloalkyl group or an aryl group, X represents a halogen atom and u represents an optional number satisfying an expression of 0<u≦4), as illustrated above as an example of the titanium compound (T 1 ) necessary for preparing the solid product (I). As its concrete examples, similar compounds may also be illustrated, and TiCℓ 4 is most preferred. The reaction of the solid product (II) with the halogenated titanium compound (T 2 ) is carried out using one mol or more of the halogenated titanium compound (T 2 ) per mol of a magnesium compound in the solid product (II), under conditions of a reaction temperature of 20° to 200°C and a reaction pressure of the atmospheric pressure (0.1 MPa) to 10 Kg/cm 2 G (1.08 MPa) and for 5 minutes to 6 hours, preferably 10 minutes to 5 hours. Further, it is also possible to carry out the reaction in the presence of an inert hydrocarbon solvent (D 4 ) and an electron donor (B 3 ), and concretely, an inert solvent and an electron donor same as in the (D 1 ) to (D 3 ) and (B 1 ) already mentioned are used. The quantities thereof used are preferred to be 0 to 5,000 mℓ of (D 4 ) per 100 g of the solid product (II) and 0 to 2 mols per mol of (B 3 ) per mol of the magnesium compound in the solid product (II). After the reaction of the solid product (II) with the halogenated titanium compound (T 2 ) and if necessary, further with an electron donor, the resulting solids are separated by filtering-off or decantation, followed by washing with an inert hydrocarbon solvent and removing unreacted substances or byproducts to obtain the solid product (III). Thus, there is obtained the solid product (III) i.e. the supported type titanium catalyst component used for producting olefin polymers, of the present invention, comprising a linear olefin-non-linear olefin block copolymer in a ratio by weight of the linear olefin polymer block to the non-linear olefin polymer block of 2/98 to 98/2 and containing 0.1 to 49.5% by weight of the linear olefin polymer block and 0.01 to 49.5% by weight of the non-linear olefin polymer block and Ti, Mg, a halogen atom and an electron donor as indispensable components. The thus obtained titanium catalyst component containing a specified block copolymer, of the present invention can be used in the same manner as in known titanium catalyst components used for producing olefin polymers. The titanium catalyst component containing a specified block copolymer is combined with an organoaluminum compound (AL 2 ) and an electron donor (B 4 ) to prepare a catalyst, or further a small quantity of an olefin is polymerized on the catalyst to prepare a preactivated catalyst, and the catalysts are then used for olefin polymerization. As the organoaluminum compound (AL 2 ) used for the olefin polymerization, organoaluminum compounds same as (AL 1 ) used for obtaining the above-mentioned titanium catalyst component of the present invention may be used. Further, as the electron donor (B4), organic acid esters, organosilicon compounds containing a Si-O-C bond such as alkoxysilanes or aryloxysilane compounds, ethers, ketones, acid anhydrides or amines are preferably used. Besides the compounds illustrated as electron donors (B 1 ) to (B 3 ) used for producing the above-mentioned titanium catalyst component, the following concrete examples are mentioned: amines having a large steric hindrance such as 2,2,6,6-tetramethylpiperidine, 2,2,5,5-tetramethylpyrrolidine, organosilicon compounds having a Si-O-C bond such as trimethylmethoxysilane, trimethylethoxysilane, dimethyldimethoxysilane, dimethyldiethoxysilane, diphenyldimethoxysilane, methylphenyldimethoxysilane, diphenyldiethoxysilane, ethyltriethoxysilane, methyltrimethoxysilane, vinyltrimethoxysilane, phenyltrimethoxysilane, methyltriethoxysilane, ethyltriethoxysilane, vinyltriethoxysilane, butyltriethoxysilane, phenyltriethoxysilane, ethyltri-i-propoxysilane or vinyltriacetoxysilane. The quantities of the respective catalyst components used are the same as those in the case of conventional olefin polymerization, and are concretely about 0.05 to 500 g of organoaluminum compound (AL 2 ) and about 0.01 to 200 g of electron donor (B 4 ) each per g of the titanium catalyst component. Further, examples of olefins used for the preactivation are linear monoolefins such as ethylene, propylene, butene-1, pentene-1, hexene-1 or heptene-1; or branched monoolefins such as 4-methyl-pentene-1 or 2-methyl-pentene-1, etc. These olefins may be same as or different from those as the object of the polymerization and may be used in admixture of two kinds or more. The form of polymerization using the above catalyst has no particular limitation, but not only liquid phase polymerization such as slurry polymerization and bulk polymerization, but also gas phase polymerization may be preferably carried out. In the case of slurry polymerization or bulk polymerization, even a combined catalyst of the titanium catalyst component with organoaluminum compound (AL 2 ) and electron donor (B4) exhibits a sufficient effectiveness, but in the case of gas phase polymerization, a preactivated catalyst obtained by reacting olefin is preferred. In the case of slurry polymerization or bulk polymerization, followed by gas phase polymerization, even when the initially used catalyst is the former one, since reaction with an olefin has already been carried out at the time of the gas phase polymerization, the resulting catalyst is the same as the latter one to exhibit a superior effectiveness. The preactivation may be carried out in an inert hydrocarbon solvent such as propane, butane, n-pentane, n-hexane, n-heptane, benzene or toluene and also may be carried out in a liquefied olefin such as liquefied propylene or liquefied butene-1, or in gaseous ethylene or propylene, and further, hydrogen gas may be made coexistent in the preactivation. In the preactivation, polymer particles obtained by slurry polymerization, bulk polymerization or gas phase polymerization may be made coexistent. Such a polymer may be the same as or different from the olefin polymer as the object of the polymerization. The quantity of the polymer particles made coexistent is 0 to 5,000 g per g of the titanium catalyst component. The solvent or olefin used at the time of the preactivation may be removed by distilling off under reduced pressure or filtering off midway during the preactivation or after completion of the preactivation, and further in order to suspend the solid product in a solvent in a quantity not exceeding 80 ℓ per g of the product, it is possible to add the solvent to the product. The thus obtained catalyst obtained by combining the titanium catalyst component of the present invention with the organoaluminum compound (AL 2 ) and the electron donor (B4), or the preactivated catalyst with an olefin, may be used for producing olefin polymers. The polymerization form in which an olefin is polymerized includes, as described above, 1 ○ slurry polymerization carried out in a hydrocarbon solvent such as n-pentane, n-hexane, n-heptane, n-octane, benzene or toluene, 2 ○ bulk polymerization carried out in a liquefied olefin monomer such as liquefied propylene or liquefied butene-1, 3 ○ gas phase polymerization in which an olefin such as ethylene or propylene is polymerized in gas phase, and 4 ○ a process wherein two or more of the above 1 ○ to 3 ○ are stepwise combined. Any of the processes are carried out at a polymerization temperature of room temperature (20°C) to 200°C, under a polymerization pressure of the atmospheric pressure (0.1 MPa, 0 Kg/cm 2 G) to 50 Kg/cm 2 G (5 MPa) and usually for about 5 minutes to 20 hours. In the polymerization, addition of a suitable quantity of hydrogen gas for controlling the molecular weight, etc. are carried out in the same manner as in conventional polymerization process. Further, examples of the olefins subjected to polymerization are linear monoolefins such as ethylene, propylene, butene-1, hexene-1 or octene-1, branched monoolefins such as 4-methylpentene-1 or 2-methylpentene-1, diolefins such as butadiene, isoprene or chloroprene, and these olefins may be subjected not only to homopolymerization, but to copolymerization with one another or with another olefin, for example, in combination of propylene with ethylene, butene-1 with ethylene, or propylene with buene-1, or three components of propylene, ethylene and butene-1, and further, block copolymerization may be carried out by varying the kind of the olefin fed at the multi-stage polymerization. ( Function ) The olefin polymer obtained using the titanium catalyst component of the present invention contains a highly stereospecific linear olefin-non-linear olefin block copolymer in an extremely dispersed state; hence when the polymer is made into a film, voids are few and since the non-linear olefin polymer block of the specified block copolymer exhibits a nucleating function at the time of melt-molding, crystallization of the resulting olefin polymer is promoted so that the transparency and crystallinity of the total olefin polymer are enhanced. In particular, in the case where the olefin polymer produced using the titanium catalyst component of the present invention is a liear olefin polymer such as polypropylene, the linear olefin polymer block of the linear olefin-non-linear olefin block copolymer is compatible with the linear olefin polymer such as polypropylene so that occurrence of voids in the film prepared from the olefin polymer is further reduced. Further, the specified block copolymer introduced into the olefin polymer by using the titanium catalyst component of the present invention is a stereoregular high molecular polymer having a high compatibility with the olefin polymer, as described above, so that the copolymer does not bleed onto the surface of the resulting olefin polymer. (Example) The present invention will be described in more detail by way of Examples, but it should not be construed to be limited thereto. The definitions of the terms employed in Examples and Comparative examples and the measurement methods therein are as follows: TY: This indicates polymerization activity and refers to a polymer yield per gram atom of titan (unit: Kg/gram atom). II: This indicates stereoregularity and refers to a residual quantity after extraction with n-hexane at 20°C (unit: % by weight) BD: Bulk desnity (unit: g/mℓ) MFR: Melt flow rate, JIS K 7210, according to the condition 14 in Table 1 (unit: g/l0min.) Inside haze: This refers to a haze inside a film excluding the surface influence; an olefin polymer powder is made into a film of 150 µ thick under conditions of a temperature of 200°C and a pressure of 200 Kg/cm 2 G (19.7 MPa) by means of a press, followed by applying liquid paraffin onto both the surfaces of the film and measuring the resulting haze according to JIS K 7105 (unit: °C). Crystallization temperature: Measured using a differential scanning calorimeter at a temperature-lowering rate of 10°C/min. (unit: °C). Flexural elastic modulus: Tetrakis[methylene-3-(3',5'-di-t-butyl-4'-hydroxyphenyl)propionate]methane (0.1 part by weight) and calcium stearate (0.1 part by weight) were blended with an olefin polymer powder (100 parts by weight), followed by granulating the resulting blend by means of an extrusion-granulator having a screw bore diameter of 40 mm, molding the resulting granules by means of an injection-molding machine at a molten resin temperature of 230°C and a mold temperature of 50°C to prepare a JIS type test piece, allowing this test piece to stand for 72 hours in a room at a humidity of 50% and at room temperature (23°C) and measuring the flexural elastic modulus according to JIS K 7203. (unit: MPa, Kgf/cm 2 ) Void: An olefin polymer is granulated in the same manner as in the above item, followed by extruding the resulting granules by means of a T-die type film-making machine at a molten resin temperature of 250°C to prepare a sheet of 1 mm thick by means of a cooling roll at 20°C, heating the sheet by a hot air at 150°C for 70 seconds,and stretching the sheet in both the longitudinal and lateral directions, each to 7 times the respective original lengths to obtain a biaxially stretched film of 20 µm thick. The film is observed by means of an optical microscope, followed by measuring the number of voids having a diameter of 10 µm or larger. A film having 10 voids or less per cm 2 was denoted by o; that having 10 to 30 voids per cm 2 was denoted by A; and that having more than 30 voids per cm 2 was denoted by ×. Example 1 (1) Preparation of titanium catalyst component In a stainless reactor provided with a stirrer, decane (3 ℓ), anhydrous magnesium chloride (480 g), n-butyl o-titanate (1.7 Kg) and 2-ethyl-1-hexanol (1.95 Kg) were mixed, followed by heating and dissolving the mixture with stirring at 130°C for one hour to prepare a uniform solution, making its temperature 70°C, adding diisobutyl phthalate (180 g) with stirring, after lapse of one hour, dropwise adding SiCℓ 4 (5.2 Kg) over 2.5 hours to deposit solids, further heating at 70°C for one hour, separating the solids from the solution and washing with hexane to obtain a solid product (I). The total quantity of the solid product (I) was suspended in hexane (10 ℓ) containing triethylaluminum (450 g) and diphenyldimethoxysilane (145 g), kept at 30°C, followed by adding propylene (630 g), subjecting the mixture to polymerization treatment with stirring at the same temperature for one hour, thereafter removing the supernatant by decantation, twice washing the resulting solids with n-hexane (6 ℓ), successively adding n-hexane (10 ℓ), triethylaluminum (450 g) and diphenyldimethoxysilane (145 g) with stirring, making the temperature 30°C, adding vinylcyclohexane (730 g), subjecting the mixture to polymerization treatment at 30°C for 2 hours, thereafter removing the supernatant and 4 times repeating a procedure of adding n-hexane (6 ℓ) and removing the supernatant to obtain a solid product (II-A) subjected to a multi-stage polymerization treatment with propylene and vinylcyclohexane. The total quantity of the solid product (II-A) was mixed with TiCℓ 4 (5 ℓ) having 1,2-dichloroethane (5 ℓ) dissolved therein, followed by adding diisobutyl phthalate (180 g), reacting the mixture with stirring at 100°C for 2 hours, removing the resulting liquid phase portion by decantation at the same temperature, again adding 1,2-dichloroethane (5 ℓ) and TiCℓ 4 (5 ℓ), agitating the mixture at 100°C for 2 hours, washing with hexane and drying to obtain a solid product (III) as the titanium catalyst component of the present invention. The titanium catalyst component has a particle form close to sphere and the contents of the propylene polymer block, the vinylcyclohexane polymer block and titanium were 30.8% by weight, 30.8% by weight and 1.2% by weight, respectively. (2) Preparation of preactivated catalyst Into a 30 ℓ capacity stainless reactor provided with slant blades and purged with nitrogen gas were added n-hexane (20 ℓ), triethylaluminum (1.5 Kg), diphenyldimethoxysilane (480 g) and the catalyst component (260 g) at room temperature, followed by keeping the reactor at 30°C, feeding ethylene (240 Nℓ) at the same temperature over 2 hours, reacting the mixture (the quantity of ethylene reacted per g of the titanium catalyst component: 1.0 g), and removing unreacted ethylene to obtain a preactivated catalyst. (3) Production of olefin polymer Into a 80 ℓ capacity, horizontal type polymerization vessel (L/D=3) provided with a stirrer and purged with nitrogen gas was fed a polypropylene powder (20 Kg) having an MFR of 2.0, followed by continuously feeding the above-mentioned preactivated catalyst slurry (containing triethylaluminum and diphenyldimethoxysilane besides the titanium catalyst component) at a rate of 0.286 mg atom/hr as calculated from titanium atom. Further, hydrogen gas was fed so as to keep its concentration in gas phase at 0.15% by volume and also propylene was fed so as to keep the total pressure at 23 Kg/cm 2 G (2.36 MPa), followed by continuously carrying out gas phase polymerization of propylene at 70°C over 120 hours. During the polymerization period, the resulting polymer was continuously withdrawn from the polymerization vessel so as to give the level of the polymer retained in the polymerization vessel at 60% by volume, at a rate of 10 Kg/hr. The withdrawn polymer was successively subjected to contact treatment with nitrogen gas containing 0.2% by volume of propylene oxide at 95°C for 15 minutes to obtain a product powder. Comparative example 1 (1) Example 1 (1) was repeated except that a substance corresponding to the solid product (II) was prepared without subjecting the solid product (I) to the multi-stage polymerization treatment with propylene and vinylcyclohexane, to obtain a titanium catalyst component. (2) Example 1 (2) was repeated except that the titanium catalyst component (100 g) obtained in the above item (1) was used as a titanium catalyst component, to prepare a preactivated catalyst. (3) Example 1 (3) was repeated except that the preactivated catalyst obtained in the above item (2) was used as a preactivated catalyst, to carry out propylene polymerization. Comparative example 2 (1) A titanium catalyst component was obtained in the same manner as in Comparative example 1 (1). (2) Into the reactor used in Example 1 (2) were fed n-heptane (20 ℓ), the titanium catalyst component (100 g) obtained in the above item (1), diethylaluminum monochloride (400 g) and diphenyldimethoxysilane (120 g), followed by adding vinylcyclohexane (130 g), reacting the mixture at 40°C for 2 hours (the quantity of vinylcyclohexane reacted per g of the titanium catalyst component: 0.8 g), washing the resulting material with n-heptane and filtering to obtain solids. Further, to the solids were added n-heptane (20 ℓ), diethylaluminum monochloride (400 g) and diphenyldimethoxysilane (55 g), followed by feeding propylene (120 g) and reacting the mixture at 30°C for one hour (the quantity of propylene reacted per g of the titanium catalyst component: 0.8 g). (3) Example 10 (3) was repeated except that the preactivated catalyst slurry was replaced by the catalyst slurry obtained above in the item (2) and further, triethylaluminum was fed at a rate of 1.7 g/hr and diphenyldimethoxysilane was fed at a rate of 0.3 g/hr, through separate feeding ports, respectively, to carry out propylene polymerization. As a result, since the resulting bulk polymer clogged the powder-withdrawing piping, the production had to be stopped 5 hours after the polymerization initiation. Comparative example 3 (1) Comparative example 1 (1) was repeated except that in advance of adding diisobutyl phthalate to a uniform solution of anhydrous magnesium chloride, n-butyl o-titanate, 2-ethyl-l-hexanol and decane, vinylcyclohexane (3.6 Kg) added into n-hexane (100 ℓ) was polymerized at 60°C for 2 hours, using as catalyst, a titanium catalyst component (100 g) separately obtained in the same manner as in Comparative example 1 (1), triethylaluminum (35 g) and diphenyldimethoxysilane (7.5 g), followed by washing with methanol, drying, grinding a portion (440 g) of resulting vinylhexane polymer (3 Kg) in vibrating mill for 5 hours and suspending the resulting material in the above uniform solution, to obtain a titanium catalyst component. (2) Example 1 (2) was repeated except that the titanium catalyst component obtained above in the item (1) was used as a titanium catalyst component, to obtain a preactivated catalyst. (3) Example 1 (3) was repeated except that the preactivated catalyst obtained above in the item (2) was fed as a preactivated catalyst so as to keep the total pressure at 23 Kg/cm 2 G (2.36 MPa), to carry out propylene polymerization. Comparative example 4 and Examples 2 and 3 In Example 1 (1), the respective quantities of propylene and vinylcyclohexane used for the polymerization treatment were varied to obtain titanium catalyst components having the contents thereof as shown in Table listed later. Thereafter, polypropylenes were obtained in the same manner as in Example 1 (2) and (3). Example 4 Anhydrous aluminum trichloride (1.7 Kg) and magnesium hydroxide (0.6 Kg) were reacted at 250°C for 3 hours while grinding them by means of a vibration mill. As a result, reaction occurred along with evolution of hydrogen chloride gas. After completion of the heating, the reaction mixture was cooled in nitrogen gas current to obtain magnesium-containing solids. In a stainless reactor provided with a stirrer, decane (6 ℓ), the above magnesium-containing solids (1.0 kg), n-butyl o-titanate (3.4 Kg) and 2-ethyl-l-hexanol (3.9 Kg) were mixed, followed by heating the mixture with stirring at 130°C for 2 hours and dissolving it together to obtain a uniform solution, making the temperature of the solution 70°C, adding ethyl p-toluylate (0.2 Kg), reacting the mixture for one hour, adding diisobutyl phthalate (0.4 Kg), further reacting the mixture for one hour, dropwise adding SiCℓ 4 (10 Kg) with stirring over 2 hours 30 minutes, depositing solids, further agitating at 70°C for one hour, separating the solids from the solution and washing with purified hexane to obtain a solid product (I). The total quantity of the solid product (I) was suspended in hexane (10 ℓ) containing triethylaluminum (450 g) and methyl p-toluylate (75 g), kept at 25°C, followed by adding propylene (250 g), reacting the mixture with stirring at 25°C for one hour to carry out the first stage polymerization treatment, thereafter removing the supernatant and twice repeating a procedure of adding n-hexane (6 ℓ) and removing the supernatant by decantation. Successively, n-hexane (10 ℓ), triethylaluminum (450 g) and methyl p-toluylate (75 g) were added with stirring, followed by adding allyltrimethylsilane (1.3 Kg), reacting the mixture at 25°C for 2 hours to carry out the second stage polymerization treatment, removing the supernatant and 4 times repeating a procedure of adding n-hexane (6 ℓ) and removing the supernatant by decantation, to obtain a solid product (II) subjected to a multi-stage polymerization treatment with propylene and allyltrimethylsilane. The total quantity of the solid product (II) together with TiCℓ 4 (10 ℓ) diluted with 1,2-dichloroethane (10 ℓ) were added to diisobutyl phthalate (0.4 Kg), followed by reacting the mixture with stirring at 100°C for 2 hours, removing the resulting liquid phase portion by decantation at the same temperature, again adding 1,2-dichloroethane (10 ℓ) and TiCℓ 4 (10 ℓ), reacting the mixture with stirring at 100°C for 2 hours, filtering while hot to obtain solid portion, washing with purified hexane and drying to obtain a solid product (III) as a final titanium catalyst component. The contents of the propylene polymer block, the allyltrimethylsilane polymer block and Ti in the titanium catalyst component were 15.0% by weight, 35.0% by weight and 1.7% by weight, respectively. Successively, Example 1 (2) was repeated except that diphenyldimethoxysilane was replaced by phenyltriethoxysilane (500 g) and also the above solid product (III) was used as a titanium catalyst component, to obtain a preactivated catalyst. Thereafter, gas phase polymerization of propylene was carried out in the same manner as in Example 1 (3). Comparative example 5 Example 4 was repeated except that a substance corresponding to the solid product (II) was prepared without subjecting the solid product (I) to polymerization treatment with propylene and allyltrimethylsilane, to obtain a titanium catalyst component, with which propylene was polymerized. Example 5 In a stainless reactor provided with a stirrer, n-heptane (8 ℓ), anhydrous magnesium chloride (1.0 Kg) and n-butyl o-titanate (7.4 Kg) were mixed, followed by raising the temperature up to 90°C with stirring, heating the mixture for 2 hours for dissolution to obtain a uniform solution, cooling the uniform solution down to 40°C, dropwise adding methylhydrogenpolysiloxane (1,500 mℓ), depositing solids and washing with n-heptane to obtain grey-white solids. The solids (500 g) and n-heptane (7 ℓ) were placed in a stainless reactor provided with a stirrer, followed by adding diisobutyl phthalate (100 g), after elapse of one hour at 30°C, dropwise adding a mixed solution of SiCℓ 4 (11.3 Kg) with TiCℓ 4 (500 g) over one hour, successively reacting the mixture at 30°C for 30 minutes and further at 90°C for one hour, separating the resulting solids from the solution and washing with n-heptane to obtain a solid product (I). The solid product (I) of 2.5 mols calculated in terms of magnesium atom was suspended in n-heptane (5 ℓ) containing triethylaluminum (200 g) and diphenyldimethoxysilane (60 g) kept at 30°C, followed by adding propylene (200 g) and reacting the mixture with stirring at 30°C for one hour, to carry out a first stage polymerization treatment. After lapse of the reaction time, the supernatant was removed, followed by twice repeating a procedure of adding n-heptane (6 ℓ) and removing the supernatant by decantation, successively adding n-heptane (5 ℓ), triethylaluminum (200 g) and diphenyldimethoxysilane (60 g) with stirring, adding 4,4-dimethylpentene-1 (280 g), reacting the mixture at 30°C for 2 hours to carry out a second stage polymerization treatment, thereafter separating the resulting solids from the solution and washing with n-heptane to obtain a solid product (II) subjected to a multi-stage polymerization with propylene and 4,4-dimethylpentene-1. The total quantity of the solid product (II) was mixed with an n-heptane solution (12 ℓ) containing TiCℓ 4 (6 ℓ), followed by adding diheptyl phthalate (100 g), reacting the mixture at 50°C for 2 hours, washing with n-heptane, further adding TiCℓ 4 (150 mℓ) and washing at 90°C to obtain a solid product (III). The contents of the propylene polymer block, 4,4-dimethylpentene-1 polymer block and titanium were 25.0% by weight, 25.0% by weight and 1.5% by weight, respectively. Successively, Example 1 (2) was repeated except that diphenyldimethoxysilane was replaced by t-butyltriethoxysilane (150 g) and also the above solid product (III) (200 g) was used as a titanium catalyst component, to obtain a preactivated catalyst, with which gas phase polymerization of propylene was carried out in the same manner as in Example 1 (3). Comparative example 6 Example 5 was repeated except that a substance corresponding to the solid product (II) was prepared without subjecting the solid product (I) with propylene and 4,4-dimethylpentene-1, to obtain a titanium catalyst component, with which gas phase polymerization of propylene was carried out. Example 6 In a stainless reactor provided with a stirrer, n-decane (2.5 ℓ), anhydrous MgCℓ 2 (480 g) and 2-ethyl-l-hexanol (1.95 Kg) were heated at 130°C for 2 hours for dissolution to obtain a uniform solution, followed by adding phthalic anhydride (111 g) into the solution, and mixing these with stirring at 130°C to dissolve phthalic anhydride in the uniform solution. The thus obtained uniform solution was cooled down to room temperature, followed by dropwise adding the total quantity into TiCℓ 4 (10 ℓ) kept at -20°C,over 1 hr.,raising the temperature of the resulting mixed solution up to 110°C over 4 hours, reacting the resulting material with stirring at the same temperature for 2 hours, separating the resulting solids from the solution and washing with n-hexane to obtain a solid product (I). The total quantity of the solid product (I) was suspended in n-decane (10 ℓ) containing triethylaluminum (450 g) and diphenyldimethoxysilane (145 g), kept at 40°C, followed by adding propylene (470 g), reacting the mixture with stirring at 40°C for one hour to carry out a first stage polymerization treatment, thereafter separating the resulting solids from the solution, washing with n-hexane, successively adding n-decane (10 ℓ), triethylaluminum (450 g) and diphenyldimethoxysilane (145 g) with stirring, adding 3-methylbutene-l (350 g), reacting the mixture at 40°C for 2 hours to carry out a second stage polymerization treatment, separating the resulting solids from the solution and washing with n-hexane, to obtain a solid product (II) subjected to a multi-stage polymerization treatment with propylene and 3-methylbutene-1. The total quantity of the solid product (II) was mixed with TiCℓ 4 (10 ℓ), followed by adding diisobutyl phthalate (350 g), reacting the mixture with stirring at 110°C for 2 hours, removing the resulting liquid phase portion by decantation at the same temperature, and again adding TiCℓ 4 (1,000 mℓ) to carry out heating reaction at 110°C for 2 hours. After completion of the reaction, the resulting liquid phase portion was removed by decantation at the same temperature, followed by washing the resulting solids with n-decane and n-hexane at 80°C and drying to obtain a solid product (III) as a final titanium catalyst component. The contents of the propylene polymer block, the 3-methylbutene-l polymer block and titanium were 30.0% by weight, 20.0% by weight and 1.5% by weight, respectively. In a 200 ℓ capacity polymerization vessel provided with a stirrer having two-stage turbine elements, n-hexane was added to the above titanium catalyst component to prepare a 4.0% by weight n-hexane suspension, followed by continuously feeding the suspension at a rate of 0.39 mg atom/hr calculated in terms of titanium atom, triethylaluminum at a rate of 8.5 g/hr and diphenyldimethoxysilane at a rate of 3.0 g/hr, each through the same piping and n-hexane at a rate of 21 Kg/hr through a separate piping, further feeding hydrogen gas so as to keep its concentration in gas phase at 0.25% by volume and propylene so as to keep the total pressure at 8 Kg/ cm 2 G (0.88 MPa) to continuously carry out slurry polymerization of propylene at 70°C over 120 hours. During the polymerization period, the resulting slurry was continuously withdrawn from the polymerization vessel into a 50 ℓ capacity flash tank so as to give a level of the slurry retained in the polymerization vessel, of 75% by volume. The pressure of the slurry was dropped in the flash tank to remove unreacted propylene, while methanol was fed at a rate of 1 Kg/hr, to subject them to contact treatment at 70°C, followed by removing the solvent from the slurry by means of a centrifuge, and drying the resulting material by a dryer to continuously obtain a product powder at a rate of 10 Kg/hr. Comparative example 7 Example 6 was repeated except that the solid product (I) was made a substance corresponding to the solid product (II) without subjecting it to polymerization treatment with propylene and 3-methylbutene-l to obtain a titanium catalyst component, with which slurry polymerization of propylene was carried out in the same manner as in Example 6 . Example 7 Example 1 (1) was repeated except that anhydrous MgCℓ 2 was replaced by magnesium ethoxide (580 g), the quantity of propylene used was made 85 g and vinylcyclohexane was replaced by p-trimethylsilylstyrene (1.6 Kg) to obtain a solid product (III), and using the solid product (III) as a final titanium catalyst component, gas phase polymerization of propylene was carried out in the same manner as in Example 10 (2) and (3). Comparative example 3 Example 7 was repeated except that the solid product (I) was made into a substance corresponding to the solid product (II) without subjecting it to polymerization treatment with propylene and p-trimethylsilylstyrene, to obtain a titanium catalyst component, with which propylene was polymerized. Example 8 Example 10 (1) was repeated except that n-butyl o-titanate was replaced by n-butyl polytitanate (pentamer) (1.2 Kg), the quantity of propylene used was made 240 g and vinylcyclohexane was replaced by 2-methyl-4-fluorostyrene (2.7 Kg), to obtain a titanium catalyst component. Using the titanium catalyst component, propylene polymerization was carried out in the same manner as in Example 1 (2) and (3). Comparatively example 9 Example 8 was repeated except that the solid product (I) was made into a substance corresponding to the solid product (II) without subjecting it to polymerization treatment with propylene and 2-methyl-4-fluorostyrene, to obtain a titanium catalyst component, with which propylene was polymerized. Example 9 (1) Example 1 (1) was repeated except that ethylene (950 Nℓ) in place of propylene was fed over one hour, followed by subjecting the resulting solid product (I) to a first stage polymerization treatment, removing unreacted ethylene, adding vinylcyclohexane (730 g) without washing the resulting reaction mixture and carrying out a second stage polymerization treatment at 40°C for 2 hours, to obtain a solid product (III) as a titanium catalyst component of the present invention. (2) Example 1 (2) was repeated except that the titanium catalyst component obtained above in the item (1) was used as a titanium catalyst component, to obtain a preactivated catalyst component. (3) Example 1 (3) was repeated except that the preactivated catalyst component obtained above in the item (2) was used as a preactivated catalyst component and ethylene was further fed so as to keep its concentration in the gas phase of the polymerization vessel at 0.2% by volume at the time of gas phase polymerization of propylene, to carry out propylene-ethylene copolymerization and thereby obtain a propylene-ethylene copolymer. Comparative example 10 Example 9 was repeated except that a titanium catalyst component was obtained without carrying out the multi-stage polymerization treatment with ethylene and vinylcyclohexane, of Example 9 (1), and the titanium catalyst component was used, to obtain a propylene-ethylene copolymer. The titanium catalyst component, polymerization results and evaluation results of the above Examples and Comparative examples are shown in Table 2. ( Effectiveness of the Invention ) The main effectiveness of the present invention consists in that when the titanium catalyst composition of the present invention is used as a transition metal compound catalyst component for producing olefin polymers, in olefin polymerization, it is possible to produce a highly crystalline olefin polymer having few occurrence of voids and a superior transparency when made into film, without causing any operational problems and with a high productivity. As apparent from the above Examples, when olefin polymers are produced using the titanium catalyst component composition of the present invention, no problem on production is raised and a long term, stabilized production is possible. Further, films produced from the resulting olefin polymer have an inside haze of 1.2 to 3.1%, that is, a very high transparency, as compared with about 9 to 12 % of films produced using conventional olefin polymers produced using a titanium catalyst component containing no specified block polymer. Further, the crystallization temperature has been raised by about 6° to 12°C to notably improve the crystallinity so that the flexural elastic modulus has also been improved (see Examples 1 - 9 and Comparative examples 1 and 5 to 10). Whereas, according to a conventional process in which a non-linear olefin polymer is introduced in a manner other than that of the present invention, such problems are raised that operational problems occur and when the resulting polymer is made into films, voids very often occur and improvements in the transparency and crystallinity are also insufficient due to inferior dispersibility (see Comparative examples 2 and 3).

Claims: A process for producing a supported type titanium catalyst component for producing olefin polymers, which process comprises subjecting a solid product (I) obtained by contacting a liquefied magnesium compound with a depositing agent, a halogen compound, an electron donor and a titanium compound (T 1 ) to a multi-stage polymerization treatment once or more each with (1) a linear olefin and (2) a non-linear olefin in the presence of an organoaluminum compound to form a linear olefin/non-linear olefin block copolymer as a solid product (II); and reacting a halogenated titanium compound (T 2 ) with the solid product (II); the content of the olefin polymer block in the supported type titanium catalyst component being from 0.1 to 49.5% by weight, that of the non-olefin polymer block being from 0.01 to 49.5% by weight, and the weight ratio of the linear olefin polymer block to the non-linear olefin polymer block being 2/98 to 98/2. A process according to claim 1, in which the organoaluminum compound is one the formula: A1R 8 ℓ R 9 ℓ' X 3 - (ℓ+ℓ') in which R 8 and R 9 each represent a hydrocarbon radical selected from the group consisting of alkyl groups, cycloalkyl groups and aryl groups or an alkoxy group; X is a halogen atom, and ℓ and ℓ' are each a number satisfying the relationship 0 < ℓ + ℓ' ≤ 3). A process according to claim 1, in which the non-linear olefin is one of the formula: or in which n represents 0 or 1; and m represents 1 or 2; R 2 represents a linear hydrocarbon radical of 1 to 3 carbon atoms which may contain silicon or represents silicon, R 3 , R 4 and R 5 each represent a linear hydrocarbon radical of 1 to 6 carbon atoms which may contain silicon, but either one of R 3 , R 4 and R 5 may be hydrogen atom; R 6 represents a linear hydrocarbon radical of 1 to 6 carbon atoms which may contain silicon; R 7 represents a hydrocarbon radical of 1 to 12 carbon atoms which may contain silicon, hydrogen atom or a halogen atom and when m represents 2, the respective R 7 s may be the same or different.

Inventors: SAITO JUN, SANPEI AKIHIKO, SAITO, JUN, SANPEI, AKIHIKO
Applicants: CHISSO CORP, CHISSO CORPORATION
Application year: 1990
Main classification: C08F4
IPC codes: C08F10