 Alpha-olefin-cycloolefin copolymer and preparation method thereof
专利摘要:
The present invention, (1) consisting essentially of 0 to 39 mole% of an α-olefin component represented by the following general formula (1A) and 61 to 100 mole% of a cycloolefin composition represented by the following general formula (1B), and (2) a concentration of 0.5 g / α-olefin-cycloolefin copolymers having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g, measured at 30 ° C., in a toluene solution of dl, hydrogenated copolymers thereof, and methods for their preparation will be : [Formula 1A] [Formula 1B] [Wherein, R 1 and R 2 are hydrogen atoms or C 1-16 saturated aliphatic hydrocarbon groups]. 公开号:KR20000064810A 申请号:KR1019980707757 申请日:1998-01-29 公开日:2000-11-06 发明作者:히데아끼 니따；기요나리 하시주메；마사끼 다께우찌；가오루 이와따 申请人:야스이 쇼사꾸；데이진 가부시키가이샤；빌프리더 하이더；바이엘 악티엔게젤샤프트； IPC主号:
专利说明:
Alpha-olefin-cycloolefin copolymer and preparation method thereof Plastics used in optical materials such as optical disc materials and optical lenses require a number of properties, in addition to transparency, such as optical isotropy (low birefringence), dimensional stability, weather resistance and thermal stability. Conventionally, polycarbonate and polymethyl methacrylate have been mainly used for such optical applications, but polycarbonate has disadvantages such as a large intrinsic birefringence and a tendency to optical anisotropy of the molded body, and polymethyl methacrylate is also due to high water absorption. Disadvantages such as insufficient dimensional stability and low heat resistance. Currently, polycarbonate is mostly used as the optical disc material, and with the recent development of increased capacity magnetic optical disc (MOD) and high recording density represented by the invention of digital video disc (DVD), the birefringence of polycarbonate Issues such as deflection of the disk by degrees and moisture absorption have been of interest. In this situation, developments have been accelerated in the field of cyclic olefin polymers to replace polycarbonates. Methods for producing such polymers can be divided into the following two types. (1) ring-opening-polymerizing cyclic olefins with a metathesis catalyst and hydrogenating the resulting unsaturated double bond on the main chain of the polymer, and (2) A method of copolymerizing an cyclic olefin with an α-olefin such as ethylene using a Ziegler-Natta catalyst or a Kaminsky catalyst without ring opening the cyclic olefin. The advantage of the method (1) is that high chemical homogeneity can be obtained because the primary structure of the polymer is formed uniformly, and when molded, a polymer having high transparency can be obtained, but it is expensive to obtain high heat resistance. Polycyclic olefins must be used. For example, such olefins currently commercially available include amorphous polyolefin resins (ZEONEX (Nihon Zeon), ARTRON (Nihon Synthetic Rubber)), dicyclopentadiene and corresponding dienophiles, used as monomers. Tetracyclo [4.4.0.1 2,5 .1 7,10 .]-3-dodecene obtained according to the Alder adduct [Polymer Preprints, Japan Vol. 44, No. 1, 81-83 (1995)]. There is this. However, the synthesis and purification of these polycyclic monomers is expensive and therefore not economically advantageous. Method (2) is a very economical method since it is possible to obtain a polymer having high heat resistance without using expensive polycyclic olefins. For example, it is known that ethylene-norbornin copolymers having a glass transition temperature of 140 ° C. or higher can be obtained by increasing the composition ratio of norbornein (abbreviated as "NB") [B.L. Goodall et al., Macromol. Symp. 89, 421-423 (1995). However, an inherent problem with this method is that it is difficult to obtain chemical homogeneity of the polymer. For most copolymers, the reactivity of the monomer varies with factors such as the composition ratio and concentration of the monomer, the polymerization temperature and the concentration of the catalyst, thus maintaining a constant composition ratio of the resulting copolymer as the polymerization reaction proceeds. Hard to do A large number of ethylene-cyclic olefin copolymers obtained using ethylene and α-olefins have been proposed, but most have been polymerized while maintaining a constant ethylene pressure during the polymerization reaction and have a chemical ratio ([cyclic olefin] / [ethylene] Since the composition ratio of the monomer represented by) decreases as the polymerization reaction proceeds, the ratio of the cyclic olefins introduced into the copolymer gradually decreases. Changes in the composition ratio of such copolymers affect the density of the polymer, thus increasing the light scattering site leading to low transparency. In addition, since the reactivity of ethylene is usually greater than that of cyclic olefins, there is a tendency to produce copolymers comprising ethylene homopolymers, oligomers and partially crystalline ethylene blocks, resulting in low transparency. One way to solve this drawback is to modify the catalyst to increase the level of alternating arrangement of ethylene and cyclic olefins (Japanese Patent No. 6-339327), and the other to minimize the production of polyethylene and ethylene blocks. (Japanese Patent Nos. 6-271628 and 8-12712). However, there is still a difficulty in obtaining a polymer suitable for use comprising an optical disc material that will meet the stringent demands of optical homogeneity and transparency. In this situation, advances in this field are needed because no method is provided for the production of cyclic olefin polymers suitable for optical applications having optical homogeneity and transparency and high heat resistance without using expensive cyclic olefins. Dicyclopentadiene (abbreviated as "DCPD" below) is used as starting material for the synthesis of many different cyclic olefins and is the least expensive of the cyclic olefins. However, research on this material has been limited because the α-olefin-DCPD copolymer containing the monomer contains unsaturated double bonds from DCPD in the copolymer. The ethylene-DCPD copolymer itself is known. H. Schnecko, et al., Angew. Macromol. Chem., 20, 141-152 (1971), describes the use of a Ziegler-Natta catalyst containing a vanadium compound and an organoaluminum compound in the copolymerization reaction of ethylene and DCPD, and an ethylene having a DCPD composition at a composition ratio of 6-100 mol%. A method of obtaining a DCPD copolymer is described. The document proposes that ethylene and DCPD carry out a random copolymerization reaction with a vanadium catalyst. On the other hand, there are several reports of ethylene-DCPD copolymers using Kaminsky catalysts. Japanese Patent Publication No. 7-13084 discloses a copolymerization reaction of ethylene and DCPD using bis (cyclopentadienyl) zirconium chloride and aluminoxane as catalysts. However, the composition ratio of the DCPD composition of the resulting copolymer is 20 mol% or less. Japanese Patent No. 2504495 and Japanese Patent Laid-Open No. 7-224122 and Japanese Patent Laid-Open No. 7-13084 disclose DCPD as a monomer which can be used, but do not mention in detail. In addition, U.S. Patent 4,948,856 discloses copolymers obtained from monomers of the norbornein class containing ethylene and DCPD, and states that an alternating arrangement of the copolymers is preferred. Copolymers with increased levels of alternating arrangement, however, cannot be obtained by the methods described in this patent, and do not describe specific examples of the use of DCPD among the monomers of the norbornene class disclosed. The present invention relates to an α-olefin-cycloolefin copolymer and a process for producing the same. More specifically, the present invention increases the alternation of structural units derived from α-olefins and structural units derived from cycloolefins, ie, high levels of alternating arrangements and chemical homogeneity. It has an alpha -olefin-cycloolefin copolymer, and its manufacturing method. Hydrogenated α-olefin-cycloolefin copolymers obtained by hydrogenating α-olefin-cycloolefin copolymers as precursors have high optical homogeneity and transparency and are therefore suitable for use in optical disc materials or other optical materials. 1 is a 1 H-NMR (400 MHz) spectrum of a DCPD homopolymer, obtained in Reference Example 1 using VOCl 3 -Et 2 AlCl as catalyst. It was measured using deuterated o-dichlorobenzene at 80 ° C. FIG. 2 is a 1 H-NMR (400 MHz) spectrum of an ethylene-DCPD copolymer containing 39 mol% of the DCPD component obtained in Reference Example 2 using VOCl 3 -Et 2 AlCl as catalyst. It was measured using deuterated o-dichlorobenzene at 80 ° C. Figure 3 is carried out using isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride [ i Pr (Cp) (Flu) ZrCl 2 ] -PMAO (polymethylaluminoxane) as catalyst 1 H-NMR (400 MHz) spectrum of ethylene-DCPD copolymer containing 39 mol% of DCPD component, obtained in Example 2. It was measured using deuterated o-dichlorobenzene at 80 ° C. 4 is a 1 H-NMR (400 MHz) spectrum of an ethylene-DCPD copolymer containing 50 mole% of the DCPD component obtained in Reference Example 4 using i Pr (Cp) (Flu) ZrCl 2 -PMAO as catalyst to be. It was measured using deuterated o-dichlorobenzene at 80 ° C. 5 is a 1 H-NMR (270 MHz) spectrum of an ethylene-DCPD copolymer containing 28 mol% of the DCPD component obtained in Reference Example 5 using i Pr (Cp) (Flu) ZrCl 2 -PMAO as catalyst to be. It was measured using deuterated o-dichlorobenzene at 80 ° C. (Indenyl) bis zirconium dichloride [Et (Ind) 2 ZrCl 2 ] - - Figure 6 is an ethylene, as a catalyst [(C 6 H 5) 3 C] + [B (C 6 F 5) 4] - using a 1 H-NMR (270 MHz) spectrum of an ethylene-DCPD copolymer containing 45 mol% of the DCPD component obtained in Example 21. It was measured using deuterated o-dichlorobenzene at 80 ° C. 7 is i Pr (Cp) as a catalyst (Flu) ZrCl 2 - [( C 6 H 5) 3 C] + [B (C 6 F 5) 4] - one, DCPD component obtained by using in Example 22 1 H-NMR (270 MHz) spectrum of a hydrogenated copolymer derived from ethylene-DCPD copolymer containing 43 mol%. It was measured using deuterated o-dichlorobenzene at 80 ° C. 8 is i Pr (Cp) as a catalyst (Flu) ZrCl 2 - [( C 6 H 5) 3 C] + [B (C 6 F 5) 4] - one, DCPD component obtained by using in Example 23 1 H-NMR (270 MHz) spectrum of a hydrogenated copolymer derived from ethylene-DCPD copolymer containing 42 mol%. It was measured using deuterated o-dichlorobenzene at 80 ° C. 9 is a 1 H-NMR (400 MHz) spectrum of a hydrogenated homopolymer derived from a DCPD homopolymer, obtained in Reference Example 1 using VOCl 3 -Et 2 AlCl as catalyst. It was measured using deuterated o-dichlorobenzene at 80 ° C. 10 is a 1 H-NMR (400 MHz) spectrum of a hydrogenated copolymer derived from an ethylene-DCPD copolymer containing 39 mol% of the DCPD component obtained in Reference Example 2 using VOCl 3 -Et 2 AlCl as catalyst to be. It was measured using deuterated o-dichlorobenzene at 80 ° C. 11 shows the relationship between the ratio of the packed monomers of the copolymerization reaction and the composition ratio of the polymer product, measured in Reference Examples 5 and 6. FIG. A: The curve shows the mole fraction [DCPD / (ethylene + DCPD)] and DCPD component of filled DCPD of the polymer product when copolymerizing ethylene and DCPD using i Pr (Cp) (Flu) ZrCl 2 as metallocene The relationship between mole fractions is shown. B: The curve shows the mole fraction of filled NB [NB / (ethylene + NB)] and NB component of the polymer product when copolymerizing ethylene and NB using i Pr (Cp) (Flu) ZrCl 2 as metallocene The relationship between mole fractions is shown. FIG. 12 shows the relationship between the pressure of ethylene measured at 40 ° C. and the solubility (mole fraction) of ethylene in toluene and DCPD for Reference Examples 7 and 8. FIG. C: The curve shows the relationship between the ethylene pressure at 40 ° C. and the solubility of ethylene in toluene (mole fraction, ethylene / (ethylene + toluene)), and the D: curve shows the ethylene pressure at 40 ° C. and solubility of ethylene in DCPD (mole fraction). , Ethylene / (ethylene + DCPD)). FIG. 13 shows the relationship between the mole fraction of the DCPD mole fraction and the DCPD component packed in the polymerization product of the copolymerization reaction of ethylene and DCPD measured for Reference Examples 9, 10 and 11. FIG. E: The curve is the DCPD mole fraction [DCPD / (ethylene + DCPD)] (%) filled when copolymerizing ethylene and DCPD using i Pr (Cp) (Flu) ZrCl 2 as metallocene and DCPD in the polymerization product. The relationship of the mole fraction (%) of a component is shown. F: The curve shows the mole fraction of the DCPD mole fraction [DCPD / (ethylene + DCPD)] (%) charged when ethylene and DCPD were copolymerized using Et (Ind) 2 ZrCl 2 as metallocene and the polymerization product. The relationship of (%) is shown. G: The curve shows the ratio of the monomer [DCPD / (ethylene + DCPD)] (%) and the DCPD component in the polymerization product when ethylene and DCPD were copolymerized using Me 2 Si (Ind) 2 ZrCl 2 as metallocene. The relationship of the composition ratio (%) is shown. FIG. 14 shows F ′ 2 / f ′ and F ′ (f′-1) / f ′ measured by the Fineman-Roth method for Reference Examples 9, 10, and 11, wherein F ′ = [ethylene] / [DCPD], f '= ethylene component in the copolymer / DCPD component in the copolymer. H: The curve shows the relationship between F ' 2 / f' and F '(f'-1) / f' when ethylene and DCPD were copolymerized using i Pr (Cp) (Flu) ZrCl 2 as metallocene. Indicates. I: The curve shows the relationship between F ' 2 / f' and F '(f'-1) / f' when ethylene and DCPD were copolymerized using Et (Ind) 2 ZrCl 2 as the metallocene. J: The curve shows the relationship between F ' 2 / f' and F '(f'-1) / f' when copolymerization of ethylene and DCPD using Me 2 Si (Ind) 2 ZrCl 2 as metallocene. . Best Mode for Carrying Out the Invention The present invention is explained in more detail below. Copolymer (X) Copolymer (X) according to the present invention consists essentially of 0 to 39 mol% of an α-olefin component represented by the following formula (1A) and 61 to 100 mol% of cycloolefin component represented by the following formula (1B): [Formula 1A] [Formula 1B] [Wherein, R 1 and R 2 are hydrogen atoms or saturated C 1-16 aliphatic hydrocarbon groups, which may be referred to as saturated aliphatic hydrocarbon groups include C 1-16 alkyl groups such as methyl, ethyl, propyl and butyl ]. The repeating unit represented by the formula (1A) constitutes 0 to 39 mol%, preferably 1 to 38 mol%, more preferably 5 to 35 mol% of all repeating units. The repeating unit represented by the formula (1B) constitutes 61 to 100 mol%, preferably 62 to 99 mol%, more preferably 65 to 95 mol% of all repeating units. Copolymer (X) has a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g, preferably 0.2 to 3 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. Copolymer (Y) Copolymer (Y) according to the invention consists essentially of repeating units represented by the following formulas (1A), (1B), (1C) and (1D): [Formula 1A] [Formula 1B] [Formula 1C] [Formula 1D] [Wherein R 1 and R 2 are hydrogen atoms or saturated C 1-16 aliphatic hydrocarbon groups, and what may be referred to as saturated aliphatic hydrocarbon groups are C 1-16 alkyl groups such as methyl, ethyl, propyl and butyl, n is 0 or 1; m is 0 or a positive integer of 1 to 3, preferably 0 or 1; p is 0 or 1; R 3 -R 22 are the same or different and are each a hydrogen atom, a halogen atom, a C 6-10 aromatic hydrocarbon group or a saturated or C 1-12 unsaturated aliphatic hydrocarbon group; One that may be referred to as a C 6-10 aromatic hydrocarbon group is an aryl group such as phenyl and naphthyl, which may be substituted with a C 1-3 alkyl group such as methyl; C 1-12 saturated aliphatic hydrocarbon groups which may be mentioned include alkyl groups such as methyl and ethyl and cycloalkyl groups such as cyclopentyl and cyclohexyl groups; What may be mentioned as C 1-12 unsaturated aromatic hydrocarbon groups are alkenyl groups such as vinyl and propenyl; Alternatively R 19 and R 20 or R 21 and R 22 form an alkylidene group such as methylidene or ethylidene, or R 19 or R 20 and R 21 or R 22 together with the two carbon atoms to which they are attached Forming a ring comprising a double bond or forming a ring which may be an aromatic ring, q is an integer from 2 to 8, preferably 2, 3 or 4]. [1A], [1B], [1C] and [1D] composition ratios representing the mole% of the repeating units (1A), (1B), (1C) and (1D) of the copolymer (Y), respectively: ([1A] + [1B]) / ([1C] + [1D]) = 95-99.9 / 0.1-5, preferably 95-98 / 2-5, [1A] / [1B] = 0-39 / 61-100, preferably 1-38 / 62-99, [1D] / [1C] = 0-95 / 5-100, preferably 0-80 / 20-100. Copolymer (Y) has a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g, preferably 0.2 to 3 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. Manufacturing method As may be mentioned as α-olefins which may be used in the polymerization reaction system for the process of the invention C 2-18 α-olefins, in particular ethylene, propylene, 1-butene, 1-hexene, 4-methyl-1-pentene , 1-octene, 1-decene, 1-dodecene, 1-tetradecene, 1-hexadecene and 1-octadecene. Ethylene and propylene are preferred among them in terms of polymerization reactivity and the molecular weight of the polymer, and ethylene is particularly preferable in view of molecular weight. These may be used alone or in combination of two or more. The cyclic olefins used according to the present invention are DCPD, but depending on the necessity of the properties of the polymer, small amounts of cyclic olefins represented by the following formulas (III) and / or (IV) do not impair the object of the present invention. It may be added to the polymerization reaction system, an amount of 10 mol% or less, preferably 5 mol% or less with respect to DCPD is preferred: [Wherein n, m, p and R 3 -R 22 are the same as defined in the general formula (1C), and q is the same as defined in the general formula (1D). According to the invention, Kaminsky catalysts are used. As is known, Kaminsky catalysts contain metallocenes and cocatalysts. The metallocenes used are preferably represented by the formula (V): [Wherein, M is a metal selected from the group consisting of titanium, zirconium and hafnium, R 26 and R 27 are the same or different and each hydrogen atom, halogen atom, saturated or unsaturated C 1-12 hydrocarbon group, C 1- 12 alkoxy group or C 6-12 aryloxy group; R 24 and R 25 are the same or different and are monocyclic or polycyclic hydrocarbon groups capable of forming a sandwiched structure with the central metal M, respectively; R <23> is the following bridge | crosslinking R <24> and R <25> . (R 28 -R 31 may be the same or different and each is a hydrogen atom, a halogen atom, a saturated or unsaturated C 1-12 hydrocarbon group, a C 1-12 alkoxy group, or a C 6-12 aryloxy group, or alternatively R 28 and R 29 or R 30 and R 31 may form a ring). The central metal M of the metallocene represented by the formula (V) is most preferably zirconium in view of the activity of the catalyst. R 26 and R 27 may be the same or different and are each C 1-6 alkyl group or halogen atom (especially chlorine). As may be mentioned as preferred cyclic hydrocarbon groups of R 24 and R 25 are cyclopentadienyl, indenyl and fluorenyl. These may be substituted with hydrogen atoms, alkyl groups such as methyl, ethyl, isopropyl or tert-butyl, and phenyl or benzyl groups. R 28 -R 31 preferably has a hydrogen atom, a C 1-6 alkyl group or a phenyl group, suitable as R 23 are lower alkylene groups such as methylene, ethylene and propylene, alkylidene groups such as isopropylidene, substituted Alkylene groups such as diphenylmethylene, silylene groups and substituted silylene groups such as dimethylsilylene and diphenylsilylene may be mentioned. Compounds that may be referred to as metallocenes with zirconium as the central metal include dimethylsilylene-bis (l-indenyl) zirconium dichloride, diphenylsilylene-bis (l-indenyl) zirconium dichloride, Dibenzylsilylene-bis (l-indenyl) zirconium dichloride, methylene-bis (l-indenyl) zirconium dichloride, ethylenebis (l-indenyl) zirconium dichloride, diphenylmethylenebis (l -Indenyl) zirconium dichloride, isopropylidene-bis (l-indenyl) zirconium dichloride, phenylmethylsilylene-bis (l-indenyl) zirconium dichloride, dimethylsilylene-bis [l- (2,4,7-trimethyl) indenyl) zirconium dichloride, diphenylsilylene-bis [l- (2,4,7-trimethyl) indenyl] zirconium dichloride, dibenzylsilylene-bis [ l- (2,4,7-trimethyl) indenyl] zirconium dichloride, methylene-bis [l- (2,4,7-trimethyl) indenyl] zirconium dichloride, ethylenebis [l- (2,4,7-trimethyl) indenyl] zirconium dichloride, diphenylmethylene-bis [l- (2,4,7-trimethyl) indenyl] zirconium dichloride, isopropylidene-bis [l- (2,4,7-trimethyl) indenyl] zirconium dichloride, phenylmethylsilylene-bis [l- (2,4,7-trimethyl) indenyl] zirconium dichloride, dimethylsilylene-bis [l -, (2,4-dimethyl) indenyl] zirconium dichloride, diphenylsilylene-bis [l- (2,4-dimethyl) indenyl] zirconium dichloride, dibenzylsilylene-bis [l- (2,4-dimethyl) indenyl] zirconium dichloride, methylene-bis [l- (2,4-dimethyl) indenyl] zirconium dichloride, ethylene-bis [l- (2,4-dimethyl) Nil] zirconium dichloride, diphenylmethylene-bis [l- (2,4-dimethyl) indenyl] zirconium dichloride, isopropylidene-bis [l- (2,4-dimethyl) indenyl] zirconium di Chloride, phenylmethylsilylene-bis [l- (2,4-dimethyl) indenyl] zirconium dichloride, di Tylsilylene-bis [l- (4,5,6,7-tetrahydro) indenyl) zirconium dichloride, diphenylsilylene-bis [l- (4,5,6,7-tetrahydro) Nil] zirconium dichloride, dibenzylsilylene-bis [l- (4,5,6,7-tetrahydro) indenyl] zirconium dichloride, methylene-bis [l- (4,5,6,7 -Tetrahydro) indenyl] zirconium dichloride, ethylene-bis [l- (4,5,6,7-tetrahydro) indenyl] zirconium dichloride, diphenylmethylene-bis [l- (4,5 , 6,7-tetrahydro) indenyl] zirconium dichloride, isopropylidene-bis [l- (4,5,6,7-tetrahydro) indenyl] zirconium dichloride, phenylmethylsilylene-bis [l- (4,5,6,7-tetrahydro) indenyl] zirconium dichloride, dimethylsilylene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, diphenylsilylene- (9-Fluorenyl) (cyclopentadienyl) zirconium dichloride, dibenzylsilylene- (9-fluorenyl) (cyclophene Tadienyl) zirconium dichloride, methylene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, ethylene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, di Phenylmethylene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, phenylmethylsilylene- (9 -Fluorenyl) (cyclopentadienyl) zirconium dichloride, dimethylsilylene- (9-fluorenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, diphenylsilyl Lene- (9-fluorenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, dibenzylsilylene- (9-fluorenyl) [l- (3-tert-butyl ) Cyclopentadienyl] zirconium dichloride, methylene- (9-fluorenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, ethylene- (9-fluorenyl) [ l- (3-tert-butyl) cycle Pentadienyl] zirconium dichloride, diphenylmethylene- (9-fluorenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, isopropylidene- (9-fluorenyl ) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, phenylmethylsilylene- (9-fluorenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium di Chloride, Dimethylsilylene- (9-fluorenyl) [l- (3-methyl) cyclopentadienyl] zirconium dichloride, diphenylsilylene- (9-fluorenyl) [l- (3- Methyl) cyclopentadienyl] zirconium dichloride, dibenzylsilylene- (9-fluorenyl) [l- (3-methyl) cyclopentadienyl] zirconium dichloride, methylene- (9-fluorenyl ) [l- (3-methyl) cyclopentadienyl] zirconium dichloride, ethylene- (9-fluorenyl) [l- (3-methyl) cyclopentadienyl] zirconium dichloride, diphenylmethylene- (9-fluorenyl) [l- (3-methyl) cyclopentadienyl] zirconium di Chloride, isopropylidene- (9-fluorenyl) [l- (3-methyl) cyclopentadienyl] zirconium dichloride, phenylmethylsilylene- (9-fluorenyl) [l- (3- Methyl) cyclopentadienyl] zirconium dichloride, dimethylsilylene- [9- (2,7-di-tert-butyl) fluorenyl] (cyclopentadienyl) zirconium dichloride, diphenylsilylene- [9- (2,7-di-tert-butyl) fluorenyl] (cyclopentadienyl) zirconium dichloride, dibenzylsilylene- [9- (2,7-di-tert-butyl) fluore Nyl] (cyclopentadienyl) zirconium dichloride, methylene- [9- (2,7-di-tert-butyl) fluorenyl] (cyclopentadienyl) zirconium dichloride, ethylene- [9- ( 2,7-di-tert-butyl) fluorenyl] (cyclopentadienyl) zirconium dichloride, diphenylmethylene- [9- (2,7-di-tert-butyl) fluorenyl] (cyclopenta Dienyl) zirconium dichloride, isopropylidene- [9- (2,7-di-tert-butyl) fluorenyl] (cyclopentadienyl) Zirconium dichloride, phenylmethylsilylene- [9- (2,7-di-tert-butyl) fluorenyl) (cyclopentadienyl) zirconium dichloride, dimethylsilylene- (l-indenyl) ( Cyclopentadienyl) zirconium dichloride, diphenylsilylene- (l-indenyl) (cyclopentadienyl) zirconium dichloride, dibenzylsilylene- (l-indenyl) (cyclopentadienyl) zirconium Dichloride, methylene- (l-indenyl) (cyclopentadienyl) zirconium dichloride, ethylene- (l-indenyl) (cyclopentadienyl) zirconium dichloride, diphenylmethylene- (l-de Nyl) (cyclopentadienyl) zirconium dichloride, isopropylidene- (l-indenyl) (cyclopentadienyl) zirconium dichloride, phenylmethylsilylene- (l-indenyl) (cyclopentadienyl ) Zirconium Dichloride, Dimethylsilylene-bis (cyclopentadienyl) Zirconium Dichloride, Diphenylsilylene-bis (cyclopentadienyl) Zirconium Di Chloride, Dibenzylsilylene-bis (cyclopentadienyl) zirconium dichloride, methylene-bis (cyclopentadienyl) zirconium dichloride, ethylene-bis (cyclopentadienyl) zirconium dichloride, diphenyl Methylene-bis (cyclopentadienyl) zirconium dichloride, isopropylidene-bis (cyclopentadienyl) zirconium dichloride, phenylmethylsilylene-bis (cyclopentadienyl) zirconium dichloride, isopropylidene -(l-indenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, isopropylidene- (9-fluorenyl) [l- (3-isopropyl) cyclopentadier Nil] zirconium dichloride, isopropylidene- [l- (2,4,7-trimethyl) indenyl] (cyclopentadienyl) zirconium dichloride, ethylene- (cyclopentadienyl) [l- (3 -tert-butyl) cyclopentadienyl] zirconium dichloride, ethylene- (cyclopentadienyl) [l- (3-phenyl) cycle Pentadienyl] zirconium dichloride, isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dibromide, dimethylsilylene-bis (l-indenyl) zirconium dibromide, ethylene-bis (l -Indenyl) methyl zirconium monochloride. Particularly preferred metallocenes according to the invention may be mentioned isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, diphenylmethylene- (9-fluorenyl) ( Cyclopentadienyl) zirconium dichloride, isopropylidene- (9-fluorenyl) [l- (3-methyl) cyclopentadienyl) zirconium dichloride, isopropylidene- (9-fluorenyl) [l- (3-tert-butyl) cyclopentadienyl] zirconium dichloride, isopropylidene- (l-indenyl) (cyclopentadienyl) zirconium dichloride, dimethylsilylene-bis (l-inde Nil) zirconium dichloride, ethylene-bis (l-indenyl) zirconium dichloride and isopropylidene-bis (l-indenyl) zirconium dichloride. The concentration of metallocene typically be determined according to their polymerization activity but with the -2 to 10 -6 to 10 with respect to 1 mol based on DCPD DCPD added to the polymerization reaction system by mole, preferably 10 -5 to 10- Preference is given to using at a concentration of 3 moles. Preference is given to using organoaluminum oxide aluminoxanes as cocatalysts. Examples of the aluminoxanes include those represented by the following general formula (VI) as the straight chain structure and the general formula (VII) as the cyclic structure. In formula (VI) and formula (VIII), R 32 -R 37 can be the same or different, each being a C 1-6 alkyl group such as methyl, ethyl, propyl, or butyl, phenyl or benzyl group, methyl Or ethyl is preferred, especially methyl. m represents an integer of 2 or more, Preferably it is an integer of 5-100. Aluminoxanes are commonly known methods such as reacting a compound containing absorbed water or a salt containing crystal (such as copper sulfate hydrate) water with an organoaluminum compound such as trialkylaluminum in an inert solvent (such as toluene). It can be prepared according to. Aluminoxanes may contain small amounts of organoaluminum compounds resulting from the manufacturing process. Aluminoxanes can be used to activate metallocenes for polymerization activity. The metallocene can be activated in a solution, preferably by dissolving the metallocene in an aluminoxane solution. The solvent used for such activation is preferably an aliphatic hydrocarbon group or an aromatic hydrocarbon group, with toluene being particularly preferred. The activation of the metallocene with aluminoxane is carried out before it is used in the polymerization reaction, and the time taken for activation is from 1 minute to 10 hours, preferably from 3 minutes to 1 hour. Activation is carried out in a temperature range of -40 to 110 ° C, preferably 0 to 80 ° C. The concentration of the aluminoxane solution is not particularly limited in the range from 1% by weight to the concentration limit, but 5 to 30% by weight is preferred. The ratio of aluminoxane to metallocene is 30 to 20,000 moles, preferably 100 to 5,000 moles, relative to 1 mole metallocene. Too small amounts of aluminoxane relative to metallocene are not preferred because sufficient polymerization activity cannot be obtained. Conversely, too large amounts of aluminoxanes are also undesirable because expensive aluminoxanes are used more in spite of their high polymerization activity and make purification more difficult after the polymerization reaction. Ionic boron compounds may be mentioned as suitable promoters which are further used in the aluminoxanes. In particular, the ionic boron compound is represented by the formulas (VII) to (XI): [R 38 3 C] + [BR 39 4 ] - [R 38 x NH 4-X ] + [BR 39 4 ] - [R 38 x PH 4-X ] + [BR 39 4 ] - Li + [BR 39 4 ] - Each of R 38 in formulas (VII) to (XI) is the same or different and represents a C 1-8 aliphatic hydrocarbon group or a C 6-18 aromatic hydrocarbon group. Each R 39 is the same or different and represents a C 6-18 aromatic hydrocarbon group. x is 1, 2, 3 or 4. As may be referred to as R 38 of the ionic boron compounds represented by the formulas (i) to (XI) above, there are alkyl groups such as methyl, ethyl, propyl and butyl and aryl groups such as phenyl. Preferred R 39 is a fluorinated aromatic hydrocarbon group and a partially fluorinated aromatic hydrocarbon group, of which pentafluorophenyl is particularly preferred. It is preferable that x is three. Specific compounds that may be mentioned include N, N-dimethylanilinium-tetrakis (pentafluorophenyl) borate, trityl-tetrakis (pentafluorophenyl) borate and lithium-tetrakis (pentafluorophenyl) There is a borate. The ionic boron compound stabilizes the metallocene converted to the cation, and therefore it is preferable to use an appropriate alkylation reagent for the initial cationization of the metallocene from the viewpoint of smoothly promoting the polymerization reaction. Preferred alkylating reagents may be mentioned alkyllithium compounds and alkylaluminum compounds, in particular methyllithium, butyllithium, trimethylaluminum, triethylaluminum, triisobutylaluminum and tri-n-butylaluminum. The ratio of the ionic boron compound to the metallocene is 0.5 to 10 moles, preferably 0.8 to 3 moles, more preferably 0.9 to 1.5 moles with respect to 1 mole of metallocene. Alkylating reagents are used from 2 to 500 moles per mole of metallocene. The required amount of ionic boron compound for metallocene was greatly reduced than that of using aluminoxane as a promoter and tends to have high catalytic activity. It is therefore possible to minimize the amount of metallocene and cocatalyst and provide a major advantage in terms of cost and purification after polymerization. These promoters are typically used directly or in the form of a solution in a hydrocarbon solvent (such as toluene), and as described above, they can be used supported on a carrier. Suitable carriers include inorganic compounds such as silica gel and alumina and fine polyolefin powders such as polyethylene and polypropylene. According to the invention, the polymerization reaction is usually carried out using a hydrocarbon solvent. Hydrocarbon solvents dissolve not only DCPD and α-olefins but also the resulting polymer. Hydrocarbon solvents dissolve the catalyst used and do not deactivate the catalyst. Specific examples include aliphatic hydrocarbons such as pentane, hexane, octane and decane, alicyclic hydrocarbons such as cyclopentane, cyclohexane and cyclooctane, and aromatic hydrocarbons such as benzene, toluene and xylene. From the standpoint of solubility of these raw materials, resulting polymers and catalysts, among these hydrocarbon solvents, aromatic hydrocarbons are particularly preferred for use with toluene. However, cyclohexane is also preferably used depending on the catalyst. 1 H-NMR spectral analysis showed that the ethylene-DCPD copolymer obtained using the Kaminsky catalyst is substantially free of chains of the DCPD component. As mentioned above, vanadium catalysts can be used to obtain ethylene-DCPD copolymers of any desired DCPD component ratios; 1 and 2 are 1 H-NMR spectra of an ethylene-DCPD copolymer containing 39 mol% of a DCPD homopolymer and a DCPD component obtained using a vanadium catalyst. 3 and 4 are 1 H-NMR spectra of an ethylene-DCPD copolymer containing 39 mol% of a DCPD component and an ethylene-DCPD copolymer containing 50 mol% of a DCPD component obtained using a Kaminsky catalyst. From the spectrum of the homopolymer of FIG. 1, a broad alkyl group signal is observed around 0.6 to 3.4 ppm when DCPD component crosslinking is produced. The spectrum of the copolymer of FIG. 2 shows that the DCPD component mole fraction is 39 mol%, ie much smaller than 50 mol%, but overlaps with the sharp signal and the broad signal continues to appear. In contrast, as can be seen from the deep valleys (spacing) of the signal near 1.85 ppm, there is virtually no signal in the case of copolymers having the same compositional ratio obtained using the Kaminsky catalyst (FIG. 3). The same result was obtained for the copolymer containing up to 50 mol% of the DCPD component (FIG. 4). On the other hand, it is apparent that the copolymers of the present invention contain crosslinks of two or more consecutive ethylene component units, unless they are fully alternating polymers. In general, decreasing the mole fraction of the DCPD component inevitably results in crosslinking of two ethylene units as well as three or more ethylene units. If the ethylene units increase during crosslinking, undesirable crystalline components are formed. This can be understood from the 1 H-NMR spectrum as in FIG. 5 of a copolymer containing 28 mol% DCPD component, ie, a copolymer containing 72 mol% ethylene component. This spectrum has sharp and strong peaks that can be interpreted as crosslinking of multiple continuous ethylene units around δ 1.3 ppm. In contrast, the copolymer obtained in Reference Example 2 does not have a peak that can be interpreted as crosslinking in the form of an ethylene component block as shown in FIG. 3 even though the polymer contains 61 mol% of the ethylene component. As is apparent from the above, as a method for measuring the increased level of alternating arrangement of the copolymer of the present invention, a method corresponding to crosslinking between DCPD component units and a method corresponding to crosslinking in which ethylene component units are crosslinked as a block form are introduced. Can be. As the former method, the method of the ratio (H 1.85 / H 3.05 ) of the intensity (H 1.85 ) of the bone intensity (H 1.85 ) of δ 1.85 ppm to the intensity (H 3.05 ) of the δ 3.05 ppm peak of the 1 H-NMR spectrum is preferably used. do. This could not be obtained by the method of the present invention, but one of the highest peaks of the copolymer consisting only of DCPD-DCPD crosslinking, which can be obtained using a Ziegler-Natta catalyst, appears in the bone at δ 1.85 ppm as shown in FIG. Because. Of course, it is affected by them because they are sandwiched between two nearby strong peaks. Thus, the H 1.85 / H 3.05 ratio cannot be zero and can constitute a good measurement. The H 1.85 / H 3.05 ratio obtained in the present invention is 0.15 or less, preferably 0.1 or less. For example, a copolymer comprising DCPD crosslinks obtained in Reference Example 2 has a ratio of H 1.85 / H 3.05 of 0.28, which is much greater than 0.15 (FIG. 2). On the contrary, the copolymer containing no DCPD-DCPD crosslinking obtained in Reference Example 4 had a H 1.85 // H 3.05 value of 0.06, and the copolymer containing no DCPD-DCPD crosslinking obtained in Example 2 had H 1.85. // 3.03 value is 0.03, which is much less than 0.15. On the other hand, as a method of indicating ethylene block crosslinking, a peak area of δ 1.3 ppm which can be interpreted as polyethylene and / or ethylene component blocks for a peak area of δ 3.05 ppm (I 3.05 ) in the 1 H-NMR spectrum of the copolymer. the mention may be made of non-(I 1.3 / I 3.05) of (I 1.3). In the present invention, 1/4 x (I 1.3 / I 3.05 ) is 0.05 or less, preferably 0.03 or less. The 1/4 is a correction factor corresponding to four protons contained in one ethylene component and δ 3.05 corresponding to both methine protons in the DCPD component. That is, the ethylene-DCPD copolymer obtained using the Kaminsky catalyst is substantially free of the DCPD component chain, and thus obtained using the vanadium catalyst in that a high mole fraction of the DCPD component provides a more alternatingly arranged copolymer. It's different from one. In the method of the present invention, the ratio (F) of the monomers of the copolymerization reaction system is controlled. As a means for assessing monomer activity in the copolymerization reaction is to use a copolymerization reaction curve which shows the correlation between the packed monomer ratio and the composition ratio of the polymer product. FIG. 11 shows ethylene-DCPD copolymers and ethylene-NB copolymers obtained using typical metallocenes and isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichlorides with mirror symmetry. The copolymerization curve for Substantially no DCPD component crosslinking was produced so the mole fraction of the DCPD component of the resulting copolymer is higher but never increases above 50 mol%, regardless of how large the F value is (see Reference Example 4). Thus, a polymerization reaction with DCPD, which is always present in excess of ethylene in the polymerization reaction system, is carried out, i.e., maintaining F above a given value to increase the alternating arrangement of ethylene and DCPD components in the copolymer, and thus a high level of alternating arrangement. Ethylene-DCPD copolymers having high performance and high chemical homogeneity can be obtained. According to FIG. 11, it is theoretically possible to carry out a polymerization reaction as a ratio of a range of monomers to obtain not only ethylene-NB copolymer but also a high level of alternating arrangement, but in practice a fixed range of fixed maximum and minimum values It is rather difficult to maintain the monomer ratio of. However, according to embodiments of the invention only the minimum ratio (F) of the monomers is fixed so that the reaction is much easier to control. A more advantageous embodiment is that the production of copolymers containing crystalline polyethylene or partially crystalline ethylene blocks is drastically reduced. For example, ethylene-bis (1-indenyl) zirconium dichloride, a typical metallocene with C 2 symmetry, is known to produce copolymers containing polyethylene and ethylene blocks during the copolymerization reaction of ethylene and NB, but this metal When Rosene is used in the present invention, the production of the crystalline polymer is drastically reduced. This is because, as one embodiment of the present invention, the polymerization reaction is carried out using a minimum amount of ethylene with respect to the cyclic olefin. The ratio (F) of the monomer of the first step according to the present invention is 4 or more, preferably 5.5 or more. It is not preferable that F is less than 4 because it increases the ratio of the ethylene component in the copolymer to lower chemical homogeneity and lower heat resistance (glass transition temperature). According to the first process of the present invention, F must be maintained at a value in the above range from the start of the polymerization reaction until the reaction rate of DCPD added to the polymerization reaction system reaches 60%. In addition, as described above, a copolymerization curve showing the correlation between the ratio of the packed monomer and the component ratio of the polymer product is used to evaluate the activity of the monomer in the copolymerization reaction. This can be obtained by carrying out the polymerization reaction with various different monomer compositions and determining the components of the copolymer produced (in% conversion) in the initial stages of the polymerization reaction. For the copolymerization reaction between monomers M 1 and M 2 , F (= [M 1 ] / [M 2 ]) representing the ratio of monomer concentration in the polymerization reaction system and f (= d [M 1 ] representing the composition ratio of the copolymerized product / d [M 2 ]) is known to exist in the relationship represented by the following formula (XII) (Shohei Inoue, Seizo Miyada, "Polymer Material Chemistry", Applied Chemistry Series 4, p. 113). f = F (r 1 F + 1) / (F + r 2 ) In the above formula, r 1 is the ratio of the reaction rate of M 1 to M 2 when the proliferation terminus of the copolymer is the M 1 component, is known as the monomer reactivity ratio, and is a value representing the relative reactivity of the monomer. Similarly, r 2 represents the ratio of the reaction rate of M 2 to M 1 when the proliferating end of the copolymer is the M 2 component. r 1 and r 2 can be calculated from the copolymer composition curve, in particular r 1 and r 2 can be calculated from the slope of the line shown for F 2 / f and F (f-1) / f and from their intercepts, respectively. (Fineman-Roths method). Using this concept in the copolymerization reaction of α-olefin and DCPD, monomer M 1 is DCPD and monomer M 2 is α-olefin. As mentioned above, the inventors have found that substantially no DCPD component crosslinking is produced when the α-olefin and DCPD are copolymerized using a Kaminsky catalyst. Therefore, when r α is the reaction rate of the α -olefin monomer and r D is the reaction rate of the DCPD monomer, it can be estimated that r D = 0, and Equation (XII) is briefly expressed as Equation (XIII) below. Can be represented. f = F / (F + r α ) The value of r α changes depending on the polymerization conditions, in particular depending on the kind of metallocene used. Metallocenes can be classified into ligands R 22 and R 23 and those having a C s symmetry (mirror phase) and a C 2 symmetry with respect to the central metal M which binds them in the formula (V). FIG. 13 shows isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, which is a typical metallocene with C s symmetry, and ethylene-bis (1), which is a typical metallocene with C 2 symmetry. The copolymer composition curve of the copolymerization reaction of ethylene and DCPD using -indenyl) zirconium dichloride and dimethylsilylene-bis (1-indenyl) zirconium dichloride is shown. Since almost no crosslinking of the DCPD component occurs, no matter how large the value of F (= [DCPD] / [ethylene]), the mole fraction of the DCPD component in the copolymer is higher but never increases above 50 mol%. In addition, for metallocenes with C 2 symmetry, DCPD components bind less readily than for metallocenes with C s symmetry. That is, r α is greater. As a result, in order to obtain a copolymer having the same DCPD component composition, it is necessary to carry out the polymerization reaction under conditions of large F value. According to the method of the present invention, the monomer molar ratio (F) of the polymerization reaction system is controlled, but according to the second method of the present invention, the value of f (= DCPD component / α-olefin component in the copolymer) of formula (XIII) is set within a predetermined range. When adjusting the F value to maintain the difference in the reactivity of the monomers with the catalyst is taken into account. In order to obtain a high chemical homogeneous copolymer, it is desirable to minimize the change in composition ratio in addition to increasing the alternating arrangement of the copolymerization reaction, f is 38/62 <f <48/52, more preferably 38 / 62 <f <46/54. The value of f is preferably 38/62 or more because it tends to produce copolymers containing polyethylene and ethylene blocks due to insufficient heat resistance due to low DCPD component content and high ethylene component content. The value of f is preferably less than 48/52, because it is too far from the minimum limit of f despite the alternating arrangement of higher copolymerization reactions. For metallocenes with C s symmetry, such as isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride, the molecular weight tends to decrease as f approaches 1, thus This is not preferable in view of molecular weight distribution. The deviation of the copolymerization reaction composition ratio of the α-olefin-DCPD copolymer of the present invention can be measured by DSC curve by DSC measurement near the glass transition temperature. The glass transition temperature of the polymer is generally measured as the bending point of the DSC curve and focuses on the temperature difference between the falling and rising points of the curve, ie the change in heat capacity due to the glass transition (abbreviated ΔTg). In addition, polymers having a large variation in the compositional ratios exhibit a wide range of changes and have a large ΔTg, whereas polymers having a uniform compositional ratio exhibit sharp changes and a small ΔTg. (DELTA) Tg, when measured at the temperature increase rate of 20 degree-C / min, Preferably it is less than 15 degreeC, More preferably, it is less than 10 degreeC. According to the second method of the present invention, F is maintained at a value in the range shown in equation (II) for a time from the start of the polymerization reaction until the reaction rate of DCPD added to the polymerization reaction system reaches 60%. "Reaction rate of DCPD added to the polymerization reaction system" indicates the total reaction rate (polymerization ratio) of DCPD present in the polymerization reaction system at the beginning of the polymerization reaction and DCPD added to the polymerization reaction system during the polymerization reaction. This period is preferably until the reaction rate reaches 70%. The desired copolymer can of course also be obtained by terminating the polymerization reaction before the reaction rate reaches 60%, but this is not preferable in view of the production cost. When ethylene is used as α-olefin, the amount of ethylene present in the polymerization reaction system depends on the pressure (or partial pressure when the gas used is a mixture of inert gases such as nitrogen). Therefore, in order to maintain the F value during the polymerization reaction, the following three methods can be introduced. (1) After introducing a predetermined amount of DCPD into the reaction system, additional DCPD is supplied to the reaction system while ethylene is added during the polymerization reaction to maintain a constant pressure of ethylene in the reaction vessel. (2) After introducing a predetermined amount of DCPD into the reaction system, the pressure of ethylene is gradually lowered as the polymerization reaction proceeds. (3) After all DCPD is introduced into the reaction system, ethylene is introduced into the reaction system under a constant pressure. In the above method (1), the operation of the process is easy, but there is a limit to increasing the final reaction rate of DCPD. On the other hand, in the method (2), the concentration of each monomer is gradually lowered, and thus the rate of reaction is also slowed down, but the polymerization reaction can be carried out with a reaction rate of high DCPD. However, even in the method (1), it is possible to keep the concentration of ethylene in the reaction system at a low level when the supply pressure or partial pressure of ethylene is lowered. Therefore, even when the concentration of DCPD decreases as the reaction proceeds, it is possible to maintain the value of F during the polymerization reaction within a range satisfying the formula (I) until the high reaction rate of DCPD is achieved. In this method, DCPD can be added in portions, but the following two successive methods may be referred to as more precise addition methods. (1a) DCPD is first introduced into the reaction system in an amount greater than four times the available molar concentration corresponding to the pressure or partial pressure of ethylene, and then DCPD is continuously introduced into the reaction system at a constant additional rate (V D ). (1b) DCPD is first introduced into the reaction system in an amount greater than four times the available molar concentration corresponding to ethylene pressure or partial pressure, and then DCPD is further added to a constant rate of mole consumption rate (V E ) of ethylene to be consumed in the reaction system. The molar feed rate (V D ) of the DCPD is introduced to satisfy V D / V E = 38/62-48/52 (mol / mol). The method of (1a) is easier than the method of (1b) from a process operation viewpoint. However, if the DCPD addition rate (V D ) is too high, the method (1a) and the method (3) do not have a difference in terms of ease of process operation, and thus no advantage can be found to introduce the control method of (1a) do. On the other hand, if the addition rate is too low, it becomes difficult to maintain the value of F in the range above 4 as the polymerization reaction proceeds. Therefore, it is necessary to adjust V D so that the value of F exceeds 4 until the response rate of DCPD reaches 60%. On the contrary, in the method (1b), since DCPD was added in combination with the ethylene consumption rate (V E ), the molar ratio (F) of the monomers present in the reaction system can be kept constant until the addition of DCPD is completed. Do. Therefore, method (1b) is preferred to obtain a copolymer having a uniform composition. This control can be accomplished without difficulty by observing the rate of consumption of ethylene with the flow system and feeding this rate back to the DCPD feeder. In this control method, the mole fraction of the DCPD component in the formed copolymer can be controlled via the amount of DCPD introduced into the reaction vessel in advance. If the amount of DCPD to the solubility of ethylene is relatively high, the mole fraction of the DCPD component in the copolymer is high, while if it is too low, the mole fraction is low. Therefore, the amount of DCPD is preferably adjusted in consideration of the rate V D / V E corresponding to the desired mole fraction of the DCPD component in the resulting copolymer. This method is also preferable because F can be maintained in a range satisfying the formula (I), and can be kept constant during the polymerization reaction until a high DCPD reaction rate is achieved when the pressure or partial pressure of ethylene is reduced. Method (3) is the easiest to adjust. In this method, the concentration ratio of DCPD to ethylene in the reaction system is maintained in a range exceeding 4 because the concentration of DCPD is satisfactorily high in the initial stage of the reaction, but the concentration ratio gradually decreases as the reaction proceeds. If the ethylene pressure is high, the concentration of DCPD decreases before the reaction rate of DCPD reaches 60%, making it impossible to maintain the concentration ratio of DCPD to ethylene in excess of four. In this case, the pressure or partial pressure of ethylene must be lowered. It is noted that, as opposed to the case where the above-mentioned NB component is used, since no direct crosslinking between two DCPD component units is produced, the above-described adjustment is possible in the present invention. In the copolymerization reaction according to the method of the present invention, the polymerization reaction proceeds as long as the catalyst is not deactivated even after the DCPD is exhausted. Thus, if the reaction continues after DCPD is depleted, the product will inevitably contain polyethylene or copolymers containing very high mole fractions of ethylene components. Therefore, it is desirable to terminate the reaction with the final reaction rate of DCPD in mind. Of course, it is not necessary to adjust the final response rate of DCPD to 60% or 70%. The final reaction rate of DCPD may vary depending on the method of supplying the monomers or the reaction conditions, and may generally be selected in the range of 95% or less, preferably 90% or less, more preferably 85% or less. In order to maintain the homogeneity of the resulting polymer and increase the reaction rate of DCPD, it is usually desirable to lower the pressure of ethylene. 12 also shows the solubility of toluene, which is a preferred solvent, and ethylene in DCPD, which should be considered as a solvent. According to the present invention, the pressure of ethylene in the polymerization reaction system is determined in consideration of the concentration of DCPD in toluene and FIG. 10, but is 10 kg / cm 2 or less, preferably 5 kg / cm 2 or less, more preferably 2 kg / cm 2 . It is not desirable that the pressure of ethylene exceed 10 kg / cm 2 since it makes it difficult to keep F within the scope of the present invention. However, if the pressure of ethylene is too low, the reaction rate is low and F is too high, which is undesirable. Therefore, 0.1 kg / cm 2 or more, in particular 0.25 kg / cm 2 or more, is preferred. In view of the reaction rate and the range of F, it is preferable to carry out the polymerization reaction under 0.5 to 1 atmosphere. As a method used to introduce DCPD into the reaction system, it is usually preferred to perform the addition at a constant rate from a commercial standpoint. The rate of introduction can be determined based on the polymerization activity and the reactivity of the catalyst used, the amount of solvent and the initial concentration of DCPD, but preferably 10 -4 to 10 -1 amol / min (amol is present in the reaction system at the beginning of the polymerization reaction). As present DCPD). If the introduction rate is 10 −4 amol / min or less, it is difficult to maintain F in the range of the present invention. If the rate of introduction is 10 −1 amol / minute or more, the rate of DCPD introduction will exceed the rate at which the polymerization reaction proceeds, making efforts to increase the overall conversion of dicyclopentadiene difficult. Another preferred method for introducing DCPD into the reaction system is to introduce DCPD in a manner corresponding to the consumption rate of ethylene. As with a gas mass flow meter, the rate of consumption of ethylene maintained at a constant pressure during the polymerization reaction can be easily observed. Thus, F can be adjusted to the correct value corresponding to the rate of consumption of ethylene. For example, when the reaction rate is fast in the initial stage of the polymerization reaction, the DCPD introduction rate may be increased, and when the reaction rate is slow in the latter stage of the polymerization reaction, the DCPD introduction rate may be decreased. Since the viscosity of the reaction solution increases as the polymerization reaction proceeds, it is preferable to stir sufficiently so that ethylene can be evenly dispersed in the solution. For example, when sufficient agitation is not performed under high viscosity conditions, such as when the viscosity of the solution exceeds 500 cps, the dispersion of ethylene becomes nonuniform, which is a factor that lowers the chemical homogeneity of the copolymer. According to the invention the DCPD concentration in the initial solution of the polymerization reaction is generally 5 to 70% by weight, preferably 7 to 50% by weight, more preferably 10 to 30% by weight. It is undesirable that the concentration of DCPD is less than 5% by weight, because it is difficult to keep F within the scope of the present invention and reduces economic viability. Concentrations of more than 70% by weight are also undesirable because the viscosity of the solution becomes too high as the polymerization reaction proceeds. The polymerization temperature generally affects not only the molecular weight of the polymer but also the activity of the catalyst, and according to the invention it is also necessary to take into account the effect that this has on the ratio (F) of the monomers. This is because the solubility of gases such as ethylene, propylene and other α-olefins in the solvent is affected by temperature in addition to their pressure or partial pressure. Increasing temperature reduces their solubility and increases F. The polymerization reaction temperature should be determined with a variety of these conditions in mind, but is usually in the range of 0 to 110 ° C, preferably 10 to 80 ° C, more preferably 15 to 50 ° C. The polymerization reaction temperature is preferably above 0 ° C. so that the activity of the catalyst is not reduced, and below 110 ° C. to prevent deactivation and addition reaction of the catalyst. After the completion of the polymerization reaction, the reaction mixture can be treated according to conventional methods to obtain a copolymer, but care is required for purification since aluminum from the aluminoxane remains in the polymer obtained using a Kaminsky catalyst. Optical materials such as optical discs preferably have an aluminum content of less than 100 ppm, more preferably less than 10 ppm, in particular less than 1 ppm. The α-olefin-DCPD copolymer obtained according to the invention preferably has a DCPD content of 38 to 50 mol%, in particular 38 to 48 mol%. The ethylene-DCPD copolymer using ethylene as the α-olefin preferably has a glass transition temperature (Tg) in the range from 140 to 190 ° C, in particular from 140 to 180 ° C. However, a characteristic aspect of the invention lies in the homogeneity of the polymer composition, and therefore it is difficult to always describe this aspect as the range of Tg. In general, the homogeneity of the polymer is represented by the relationship between Tg and composition and the degree of steepness of Tg. The range of Tg of the ethylene-DCPD copolymer according to the present invention is represented by the following formula: -22.7 + 2.84 m D + 0.0262 m D 2 <Tg <-2.7 + 2.84 m D + 0.0262 m D 2 [Wherein m D represents the mole fraction (%) of the DCPD component in the polymer and is in the range of 38% <m D <50%]. Tg generally increases but does not always increase as m D increases. Even if m D is the same, Tg is different between the case where the distribution of a copolymer composition is wide and narrow. As mentioned above, when using a Ziegler-Natta catalyst, a DCPD-DCPD crosslinking can be produced. Thus, copolymers having a mole fraction of DCPD components well above 50 mol% and air fractions having a mole fraction of ethylene components well above 50 mol%, unless the concentrations of DCPD and ethylene in the reaction system remain precise and constant during the polymerization reaction. The coalescing is formed in combination. In this case, Tg and m D do not satisfy the above formula. Therefore, even when the metallocene catalyst used in the present invention is used, components having a mole fraction of crystalline polyethylene or high ethylene components are simultaneously produced, so that Tg and m D are The above formula is not satisfied. In contrast, the copolymers according to the invention are very homogeneous and therefore exhibit a relationship between Tg and m D in the range of the above formula. In addition, the embodiment of the α-olefin-DCPD copolymer according to the present invention is represented by the sharpness of the glass transition temperature. The copolymer according to the invention has a temperature difference (ΔT g) between the falling point and the rising point of the DSC curve of 15 ° C. or lower, preferably 13 ° C. or lower. Copolymers obtained according to methods or conditions outside the scope of the present invention have broad Tg ranges or peaks corresponding to the melting point of polyethylene, or copolymerized ethylene block components are observed in the DSC curve, all of which are undesirable. The molecular weight of the α-olefin-DCPD copolymer obtained according to the method of the present invention is 0.1 to 10 dl / g, preferably 0.2 to 3 dl / g, in a toluene solution at a concentration of 0.5 g / dl at 30 ° C. η sp has / c This value is preferably at least 0.1 dl / g in order to avoid a decrease in the dynamic properties of the molded article, and is preferably at most 10 dl / g in order to avoid an increase in resin melt viscosity that may inhibit melt molding. The molecular weight of the resulting polymer can be controlled by known methods such as supplying a predetermined amount of hydrogen to the polymerization reaction system, changing the catalyst concentration, or changing the polymerization reaction temperature. The molecular weight of the ethylene-DCPD copolymer can be controlled by adding small amounts of liquid α-olefins such as 1-hexene. The amount of α-olefin added is 0.03 mol or less, preferably 0.02 mol or less with respect to 1 mol of DCPD. Polymer (X H ) The copolymer (X H ) according to the present invention consists essentially of 0 to 39 mol% of an α-olefin component represented by the following formula (1Aa) and 61 to 100 mol% of cycloolefin component represented by the following formula (1Ba): Formula 1Aa] [Formula 1Ba] [Wherein R 1 and R 2 are hydrogen atoms or C 1-16 saturated aliphatic hydrocarbon groups, which may be referred to as saturated aliphatic hydrocarbon groups are C 1-16 alkyl groups such as methyl, ethyl, propyl and butyl] The repeating unit represented by the above formula (1Aa) constitutes 0 to 39 mol%, preferably 1 to 38 mol%, more preferably 5 to 35 mol% of all repeating units. The repeating unit represented by the above formula (1Ba) constitutes 61 to 100 mol%, preferably 62 to 99 mol%, more preferably 65 to 95 mol% of all repeating units. The copolymer (X H ) has a reduced viscosity η sp / C in the range of 0.1 to 10 dl / g, preferably 0.2 to 3 dl / g, as measured at 30 ° C., in a toluene solution with a concentration of 0.5 g / dl. . Copolymer (Y H ) The copolymer (Y H ) according to the invention consists essentially of repeating units represented by the following formulas (1Aa), (1Ba), (1Ca) and (1Da): Formula 1Aa] [Formula 1Ba] Formula 1Ca] Formula 1Da] [Wherein R 1 and R 2 are hydrogen atoms or saturated C 1-16 aliphatic hydrocarbon groups, which may be referred to as saturated aliphatic hydrocarbon groups include C 1-16 alkyl groups such as methyl, ethyl, propyl and butyl; ; n is 0 or 1; m is 0 or a positive integer of 1 to 3, preferably 0 or 1; p is 0 or 1; R 3 -R 22 are the same or different and each is a hydrogen atom, a halogen atom, a C 6-10 aromatic hydrocarbon group or a saturated C 1-12 aliphatic hydrocarbon group; Alternatively R 19 and R 20 or R 21 and R 22 form an alkylidene group such as methylidene or ethylidene, or R 19 or R 20 and R 21 or R 22 together with the two carbon atoms to which they are attached an aromatic ring Forming a ring, q is an integer from 2 to 8, preferably 2, 3 or 4. One that may be referred to as a C 6-10 aromatic hydrocarbon group is an aryl group such as a phenyl group and a naphthyl group, which may be substituted with a C 1-3 alkyl group such as methyl. What may be mentioned as saturated C 1-12 aliphatic hydrocarbon groups are alkyl groups such as methyl and ethyl and cycloalkyl groups such as cyclopentyl and cyclohexyl. [1Aa], [1Ba], [1Ca] and [1Da] composition ratios representing the mole% of the repeating units (1Aa), (1Ba), (1Ca) and (1Da) of the copolymer (Y H ), respectively: ([1Aa] + [1Ba]) / ([1Ca] + [1Da]) = 95-99.9 / 0.1-5, preferably 95-98 / 2-5, [1Aa] / [1Ba] = 0-39 / 61-100, preferably 1-38 / 62-99, [1Da] / [1Ca] = 0-95 / 5-100, preferably 0-80 / 20-100. The copolymer (Y H ) has a reduced viscosity η sp / C in the range of 0.1 to 10 dl / g, preferably 0.2 to 3 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. . The α-olefin-cycloolefin copolymers (X H ) in the hydrogenated form according to the invention exhibit a high level of alternating arrangement and, therefore, high homogeneity. This can be easily understood from the fact that the precursor α-olefin-DCPD copolymer has a high degree of change and high homogeneity. This is apparent even when comparing the 1 H-NMR spectrum of the hydrogenated DCPD homopolymer and the hydrogenated ethylene-DCPD copolymer obtained in Reference Examples 1 and 2 with the spectrum of the hydrogenated ethylene-DCPD copolymer obtained in Examples 21 to 23. Do. As can be seen in FIG. 9, which shows 1 H-NMR of the hydrogenated DCPD homopolymer obtained by hydrogenating the DCPD homopolymer obtained in Reference Example 1 using VOCl 3 -Et 2 AlCl as the catalyst, the hydrogenated DCPD homopolymer is Very broad peaks around 0.7-3.0 ppm. This widening peak is due to crosslinking between tricyclo [4.3.0.1 2.5 ] decane (hereinafter referred to as tricyclodecane) component units. In FIG. 10 showing the 1 H-NMR spectrum of the hydrogenated ethylene-DCPD copolymer by hydrogenating the ethylene-DCPD copolymer obtained in Reference Example 2 using VOCl 3 -Et 2 as a catalyst, the hydrogenated ethylene-DCPD copolymer was δ. Sharp peaks appear around 1.07, 1.3, 1.47, 1.65, 1.8, 2.0 and 2.4 ppm. However, peaks overlapping with broad peaks are observed at δ 0.7 and 3.0 ppm of the spectrum of the hydrogenated DCPD homopolymer. This suggests that even though the copolymer contains tricyclodecane components in amounts much less than 39 mol%, ie 50 mol%, the copolymer includes tricyclodecane component crosslinking. In addition, the valleys observed at δ 2.2 ppm of the spectrum of the hydrogenated ethylene-DCPD copolymer do not have a deep bottom corresponding to the barrier observed at δ 2.2 ppm of the spectrum of the hydrogenated DCPD homopolymer. In contrast, in the 1 H-NMR spectrum of the hydrogenated ethylene-DCPD copolymers obtained in Examples 21-23, the corresponding valleys have a bottom nearly deep enough to touch the bottom line. This means that the peaks of these spectra do not overlap with the broad peaks due to tricyclodecane component crosslinking, or that the hydrogenated ethylene-DCPD copolymer according to the invention does not contain tricyclodecane component crosslinking. Of course, even in the 1 H-NMR spectrum of the hydrogenated ethylene-DCPD copolymer according to the present invention, the peak of δ 1.07 to 1.8 ppm is sharp but the valley between the peaks does not have a deep bottom. However, it is noted that this is not due to the tricyclodecane component crosslinking but due to the presence of many peaks in this region. From the study, 1 H-NMR ratio (H '2.20 / H' 2.40 ) of the 'δ 2.40 intensity of the peak in ppm (H about (2.20, 2.40) spectra bone strength H)' of δ 2.20 ppm measured at the It is a good way to know the presence of tricyclodecane component crosslinking in the hydrogenated ethylene-DCPD copolymer. In the present invention, the H'2.20 / H'2.40 ratio is 0.07 or less, preferably 0.05 or less. For example, the H ' 2.20 / H' 2.40 ratio of the hydrogenated ethylene-DCPD copolymer obtained in Reference Example 2 is 0.13, while the ratios of the copolymers obtained in Examples 21 to 23 are 0.038, 0.031 and 0.024, respectively. The hydrogenated α-olefin-DCPD copolymers obtained according to the invention are characterized by the homogeneity of the polymer composition. As with the corresponding α-olefin-DCPD copolymer, the homogeneity of the hydrogenated α-olefin-DCPD copolymer is indicated by the relationship between Tg and composition and the sharp degree of Tg. The range of Tg of the ethylene-cycloolefin copolymer of the hydrogenated kind according to the invention can be represented by the formula: -32.7 + 2.84 m T + 0.0262 m T 2 <Tg <-7.7 + 2.84 m T + 0.0262 m T 2 [Wherein m T represents the mole fraction (%) of the tricyclodecane component in the polymer and is in the range of 38% <m T <50%]. The temperature difference (ΔT g) between the falling point and the rising point of the DSC curve is 15 ° C. or less, preferably 13 ° C. or less. Manufacturing method (hydrogenation treatment) The α-olefin-DCPD copolymers (copolymer (X) and copolymer (Y)) obtained according to the present invention contain unsaturated double bonds in the polymer and thus lack thermal stability and are not suitable for melt molding. However, by adding hydrogen to these copolymers, hydrogenated unsaturated double bonds can be hydrogenated to rapidly increase thermal stability, and melt molding becomes possible. The hydrogenation ratio (ratio of hydrogenation to unsaturated double bonds) of the hydrogenated α-olefin-DCPD copolymer is at least 99%, preferably at least 99.5%, more preferably at least 99.9%. A hydrogenation ratio of less than 99% is undesirable because it leads to insufficient thermal stability and tends to color during melt molding. In the case of ring-opening polymers having unsaturated double bonds in the main chain, the glass transition temperature is drastically reduced by hydrogenation, but in the case of the α-olefin-DCPD copolymer of the present invention, the unsaturated double bond is located in a branched chain or in a ring structure. The glass transition temperature will change somewhat less before or after hydrogenation. The ends of the polymers obtained using a Kaminsky catalyst usually comprise unsaturated double bonds provided with a molecular weight regulator which does not use hydrogen. Such terminal double bonds are undesirable because they promote crosslinking reactions during melt molding and form gel fish-eyes. The present invention provides a copolymer having no double bond at the terminal by hydrogenation. Hydrogenation can be carried out using a hydrogenation catalyst according to known methods. Hydrogenation may be carried out after the polymer is separated and purified to obtain the α-olefin-DCPD copolymer of the present invention, but from the economic point of view of hydrogenation, it is preferable to carry out hydrogenation after the polymerization reaction in which the polymer is still in solution. desirable. If this is done, unreacted DCPD in the polymerization solution can be hydrogenated to tricyclo [4.3.0.1 2,5 ] decane, but this is not a problem since it can be easily removed by purification after hydrogenation. It is preferable to deactivate the Kaminsky catalyst before adding the hydrogenation catalyst to the polymerization solution in view of the nature of the hydrogenation copolymer and in particular the molecular weight. Kaminsky catalysts can be deactivated without affecting the ongoing hydrogenation reaction by adding small amounts of aliphatic alcohols such as methanol, ethanol, n-propanol or isopropanol to the polymerization solution. The catalyst used for hydrogenation according to the invention is not critical and may be one commonly used for the hydrogenation of olefins. These catalysts are generally divided into heterogeneous catalysts and homogeneous catalysts. Examples of preferred heterogeneous catalysts are solid catalysts containing nickel, palladium and platinum as well as the metals supported on silica, carbon, diatomaceous earth, alumina, titanium oxide and the like. Particular mention may be made of nickel / silica, nickel / diatomaceous earth, palladium / diatomaceous earth, palladium / carbon, palladium / silica, palladium / diatomaceous earth and palladium / alumina. Raney nickel may be preferably used as the nickel catalyst, and platinum oxide and platinum black may be preferably used as the platinum catalyst. What may be mentioned as homogeneous catalysts are catalyst systems containing Group 8 metal compounds, in particular Ni, Co or Fe compounds and organometallic compounds of Group 1 to 3 metals, such as cobalt naphthenate / triethylaluminum, cobalt acetylacetonate / iso Butylaluminum, iron acetylacetonate / isobutylaluminum, cobalt octenoate / n-butyllithium and nickel acetylacetonate / triethylaluminum. Also compounds such as Ru, Rh, such as carbonylchlorohydrido-tris (triphenylphosphine) ruthenium, dihydridocarbonyl-tris (triphenylphosphine) ruthenium, dihydrido-tetrakis (triphenylphosph) Pin) ruthenium, chloro-tris (triphenylphosphine) rhodium and hydridocarbonyl (triphenylphosphine) rhodium. Although the hydrogenation reaction conditions vary depending on the catalyst used, the hydrogenation reaction can usually be carried out at a temperature of 50 to 200 ° C, preferably 80 to 180 ° C under a hydrogen pressure of 1 to 100 atm. The reaction time may depend on the activity of the catalyst but can typically be from 10 minutes to 10 hours, preferably from 30 minutes to 5 hours. Depending on the type of catalyst and the reaction conditions, the solvents used, such as unsaturated solvents such as toluene, are hydrogenated simultaneously, which is economically undesirable. Therefore, it is desirable to select conditions under which such side reactions do not occur. Of course, when a small amount of the solvent is hydrogenated, the hydrogenated solvent can be easily removed. The α-olefin-cycloolefin copolymer of the hydrogenated kind obtained according to the invention can be melt molded according to known methods such as injection molding or extrusion molding. The resin melt temperature for forming is determined based on the required properties of the molded article and the melt viscosity and thermal decomposition temperature of the copolymer used, but is usually in the range of 200 to 380 ° C, preferably 240 to 340 ° C. If the resin melting temperature is lower than the above range, the fluidity of the resin becomes insufficient to obtain a uniform molded product. If the resin melting temperature is higher than the above range, thermal deterioration of the resin occurs to cause coloring. Small amounts of commonly used antioxidants such as Irganox 1010, 1076 (Siba-Geigy Co.) may be added for improved thermal stability of the resin during melt molding. It is an object of the present invention to provide α-olefin-cycloolefin copolymers having high chemical homogeneity and suitable for optical purposes and a process for their preparation. As a result of the steady study on the copolymerization reaction of α-olefin and DCPD with Kaminsky catalyst, we found that the reactivity of DCPD is much higher than that of conventional vanadium catalyst. That is, when a Kaminsky catalyst is used, a DCPD homopolymer cannot be obtained, and when copolymerized with ethylene, the composition of DCPD does not exceed 50 mol% in the copolymer regardless of how high the composition ratio of DCPD to ethylene is. This indicates that there is substantially no crosslinking reaction of the DCPD composition in the presence of a Kaminsky catalyst. This is because homopolymers of NB are obtained when the polymerization of NB is carried out using a Kaminsky catalyst as in many reports published to date [W. Kaminsky et al., Stud. Surf. Sci. Catal. 56, (Catal. Olefin Polym.), 425-438 (1990) and ethylene-NB copolymers having a mole fraction NB composition of more than 50 mole% were obtained [W. Kaminsky, et al., Macromol. Chem., Macromol. Symp., 47, 83-93 (1991)] is a surprising finding in view of the known fact that the crosslinking reaction of NB compositions is easily carried out on the basis of evidence. The inventors have noted the properties of these DCPDs and catalysts, using Kaminsky catalysts to maintain the composition ratio of DCPD monomers in the reaction system above a certain value relative to the α-olefins and increase the DCPD component, crystalline α-olefin homopolymers, It has been found that the production of oligomers and block copolymers can be minimized to yield α-olefin-DCPD copolymers with high chemical homogeneity. In addition, hydrogenated α-olefin-DCPD copolymers obtained by adding hydrogen to the copolymer to hydrogenate unsaturated double bonds have been found to have excellent optical homogeneity and transparency, and thus are suitable for optical applications including optical disc materials, Based on this, the present invention has been completed. That is, the present invention, (1) consisting essentially of 0 to 39 mol% of an α-olefin component represented by the following formula (1A) and 61 to 100 mol% of cycloolefin component represented by the following formula (1B), [Wherein, R 1 and R 2 are hydrogen atoms or C 1-16 saturated aliphatic hydrocarbon groups] (2) α-olefins having an increased level of alternating arrangement having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g, measured at 30 ° C., in a toluene solution with a concentration of 0.5 g / dl. A cycloolefin copolymer (hereinafter sometimes referred to as copolymer (X)) is provided. Accordingly, the copolymer according to the present invention substantially includes not only copolymers composed of repeating units represented by formula (1A) and formula (1B) but also repeating units represented by formula (1A) in copolymer (X). And therefore comprises a copolymer consisting essentially of repeating units represented by the formula (1B). In addition, the present invention, (1) consisting essentially of repeating units represented by the following formulas (1A), (1B), (1C) and (1D), [Formula 1A] [Formula 1B] [Wherein R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group, n is 0 or 1, m is a positive integer of 0 or 1 to 3, and p is 0 or 1 R 3 to R 22 are the same or different and each is a hydrogen atom, a halogen atom, a C 6-10 aromatic hydrocarbon group or a C 1-12 saturated or unsaturated aliphatic hydrocarbon group, and R 19 and R 20 or R 21 and R 22 are Together may form an alkylidene group, R 19 or R 20 and R 21 or R 22 may form a ring which may be an aromatic ring or a ring which may contain two carbon atoms and one or more double bonds to which they are bonded , q is an integer from 2 to 8] The composition ratio of [1A], [1B], [1C] and [1D], representing the mole% of each repeating unit (1A), (1B), (1C) and (1D) is ([1A] + [1B] ) / ([1C] + [1D]) = 95-99.9 / 0.1-5, [1A] / [1B] = 0-39 / 61-100 and [1D] / [1C] = 0-95 / 5- Is in the range of 100, (2) α-olefins having an increased level of alternating arrangement having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g, measured at 30 ° C., in a toluene solution with a concentration of 0.5 g / dl. A cycloolefin copolymer (hereinafter sometimes referred to as copolymer (Y)) is provided. That is, the copolymer according to the present invention includes a copolymer composed of repeating units (1B) and (1C) such that the composition ratio is in the range of [1B] / [1C] = 95-99.9 / 0.1-5. In addition, the copolymer according to the present invention has a composition ratio of [1B] / ([1C] + [1D]) = 95-99.9 / 0.1-5 and [1D] / [1C] = 1-95 / 5-99 It includes a copolymer composed of repeating units (1B), (1C) and (1D) to the extent. In addition, the copolymer according to the present invention has a composition ratio of ([1A] + [1B]) / [1C] = 95-99.9 / 0.1-5 and [1A] / [1B] = 1-24 / 76-99 It includes a copolymer composed of repeating units (1A), (1B) and (1C) to the extent. In addition, the copolymer according to the present invention has a composition ratio of ([1A] + [1B]) / ([1C] + [1D]) = 95-99.9 / 0.1-5, [1A] / [1B] = 1- Copolymers composed of repeating units (1A), (1B), (1C) and (1D) in the range of 24 / 76-99 and [1D] / [1C] = 1-95 / 5-99. The present invention also relates to α-olefin-cycloolefin copolymers in hydrogenated form with increased levels of alternating arrangement, obtainable by hydrogenating at least 99% of the unsaturated double bonds of copolymer (X) (copolymer (X H ) It may be indicated by). Thus, the α-olefin-cycloolefin copolymer (X H ) is (1) consisting essentially of 0 to 39% of the α-olefin component represented by the following formula (1Aa) and 61 to 100 mol% of the cycloolefin component represented by the following formula (1Ba), [Wherein, R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group] (2) It has a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g when measured at 30 ° C. in a toluene solution having a concentration of 0.5 g / dl. The present invention also relates to an α-olefin-cycloolefin copolymer in hydrogenated form with increased levels of alternating arrangement, obtainable by hydrogenating at least 99% of olefinically unsaturated double bonds in copolymer (Y) (copolymer (Y H ) may be indicated). Thus, the α-olefin-cycloolefin copolymer (Y H ) is (1) consisting essentially of repeating units represented by the following formulas (1Aa), (1Ba), (1Ca) and (1Da), Formula 1Aa] [Formula 1Ba] [Wherein R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group, n is 0 or 1, m is a positive integer of 0 or 1 to 3, and p is 0 or 1 , R 3 to R 22 are the same or different and each is a hydrogen atom, a halogen atom, a C 6-10 aromatic hydrocarbon group or a C 1-12 saturated aliphatic hydrocarbon group, and R 19 and R 20 or R 21 and R 22 together May form an alkylidene group, or R 19 or R 20 and R 21 or R 22 may form a ring which may be an aromatic ring with the two carbon atoms to which they are attached, q is an integer from 2 to 8; The composition ratios of [1Aa], [1Ba], [1Ca] and [1Da] representing the mole% of each repeating unit (1Aa), (1Ba), (1Ca) and (1Da) are ([1Aa] + [1Ba] ) / ([1Ca] + [1Da]) = 95-99.9 / 0.1-5, [1Aa] / [1Ba] = 0-39 / 61-100 and [1Da] / [1Ca] = 0-95 / 5- 100, (2) It has a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g when measured at 30 ° C. in a toluene solution having a concentration of 0.5 g / dl. In the present invention, while the reaction rate of DCPD added to the polymerization reaction system is 60% from the start of the polymerization reaction, while maintaining the molar ratio (F) of the monomer in the reaction system in the range satisfying the following formula (I), the center metal is titanium Α, comprising copolymerizing DCPD with an α-olefin having at least two carbon atoms in the presence of at least one metallocene and a catalyst containing at least one metallocene, which is zirconium or hafnium, followed by or without hydrogenation Provided is a process for preparing an -olefin-cycloolefin copolymer. F = [dicyclopentadiene] / [α-olefin]> 4 Within the scope of the production method, preferred production methods are those wherein the α-olefin used is ethylene. It is preferred that the central metal of the metallocene is zirconium and the promoter is aluminoxane. Equally preferred is that the central metal of the metallocene is zirconium and the promoter is an ionic boron compound. In the period in which the ratio of the monomers is maintained, the molar ratio (F) of the monomers in the reaction system is preferably in a range satisfying the above formula (I) until the reaction rate of the dicyclopentadiene added to the polymerization reaction system reaches 70%. Do. In the above method of the present invention, a more preferable ratio (F) of the monomer is in the range of F> 5.5. As a result of the study of the copolymerization reaction of α-olefin and DCPD including the activity of the catalyst, the inventors found that the reactivity of the monomers varies considerably depending on the type of metallocene used. The present invention provides an α-olefin-cycloolefin copolymer having a narrow range of copolymer composition ranges and a high level of alternating arrangement, i.e., high chemical homogeneity, by controlling the composition ratio of monomers based on the monomers different from each catalyst during the polymerization reaction. Completion is based on the finding that can be obtained. Therefore, in the present invention, while the reaction rate of DCPD added to the polymerization reaction system reaches 60% from the start of the polymerization reaction, the molar ratio (F = [DCPD]) / [α-olefin]) of the monomers in the reaction system is represented by the following formula (II). Copolymerizing DCPD with an α-olefin having at least two carbon atoms in the presence of at least one metallocene catalyst and at least one cocatalyst whose central metal is titanium, zirconium or hafnium Then, there is provided a method for producing an α-olefin-cycloolefin copolymer comprising performing or not performing hydrogenation. 38/62 <F / (F + r α ) <48/52 [Wherein, r α represents the ratio of the reactivity of the monomer of the α-olefin to DCPD, and represents the reaction rate of the α-olefin when the proliferation end of the copolymer is the α-olefin component during the polymerization reaction]. The process of the invention is particularly suitable when the α-olefin is ethylene. It is also preferable that the central atom of the metallocene is zirconium and the promoter is aluminoxane. It is equally preferable that the central metal of the metallocene is zirconium and the promoter is an ionic boron compound. In the period in which the ratio of the monomers is maintained, the molar ratio (F) of the monomers in the reaction system is preferably in a range satisfying the above formula (II) until the reaction rate of DCPD added to the polymerization reaction system reaches 70%. Although this invention is demonstrated in detail as an Example, this invention is not limited to these Examples. Toluene (solvent), DCPD, NB and 5-ethylidene-2-norbornane used were distilled and purified and dried appropriately. Metallocene isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride is described in J. Chem. A. Ewen et al., J. Am. Chem. Soc., 110, 6255-6266 (1998). Dimethylsilylene-bis (1-indenyl) zirconium dichloride is described in W. A. Herrmann et al., Angew. Chem. Int. Ed. Engl., 28, 1511-1512 (1989). Ethylene-bis (1-indenyl) zirconium dichloride was purchased from Aldrich and used. Trityl-tetrakis (pentafluorophenyl) borate was used as an ionic boron compound in the form purchased from Toso Akuzo. The aluminoxane used was polymethylaluminoxane (PMAO) purchased from Tosoh Akujosa and prepared as a 2 M toluene solution. Triisobutylaluminum [( i Bu) 3 Al] was used as a 1 M concentration of n-hexane solution purchased from Kanto Chemical. Vanadium oxytrichloride (VOCl 3 ) was used in the form purchased from Canto Chemicals. Diethylaluminium chloride (Et 2 AlCl) was used in the form of a 1 M concentration of n-hexane purchased from Canto Chemicals. The measurement in an Example was performed by the following method. Glass transition temperature (Tg): It measured using TA 2920 DSC-type measuring device, heating up at the speed of 20 degree-C / min. Molecular weight: The reduced viscosity η sp / c was measured in a toluene solution at 30 ° C. and 0.5 g / dl concentration. Light transmittance: Measured using a Shimanzu UV spectrometer (UV-240). Haze value: It measured using the UDH-20D automatic digital haze meter of Nihon Denshoku Industries. Residual aluminum concentration in the polymer: measured by ICP emission analysis. Reference Example 1 Vanadium catalysts were used for homopolymerization of DCPD. Into a 50 ml Schlenk flask, which was purged with nitrogen, 87 mg of vanadium oxytrichloride (VOCl 3 ) was quantitatively introduced and 2.5 ml of diethylaluminium chloride (Et 2 AlCl) dissolved in a 1 M n-hexane solution. ) Is added and the mixture is activated by stirring at room temperature for 5 minutes. Thereafter, 15 ml of toluene and 6.6 g of DCPD are administered to polymerize at room temperature for 13.5 hours, and treated in a conventional manner to obtain 0.40 g of a polymer. The reduced viscosity η sp / c measured at 30 ° C. in the toluene solution having a concentration of 0.5 g / dl is 0.049 dl / g. 1 H-NMR spectrum of this DCPD homopolymer is shown in FIG. 1. The obtained DCPD homopolymer is hydrogenated by dissolving 5 mg of triisobutylaluminum in 10 ml of toluene as 70 mg of DCPD homopolymer and catalyst in a high pressure reactor. The hydrogenation is carried out at a temperature of 140 ° C. for 6 hours under a hydrogen pressure of 10 atm and then treated in a conventional manner to give 58 mg of hydrogenated polymer. The 1 H-NMR spectrum of the hydrogenated DCPD homopolymer is shown in FIG. 9. Reference Example 2 A vanadium catalyst was used for the copolymerization reaction of ethylene and DCPD. After addition of 15 ml of toluene and 6.6 g of DCPD, the same method as in Reference Example 1 was followed except that ethylene gas was passed through a Schlenk flask system to produce an ethylene pressure atmosphere of 1 kg / cm 2 . The polymerization is carried out at room temperature for 95 hours and conventional treatment gives 1.40 g of polymer. The resulting polymer contains a large amount of toluene-insoluble moieties, and DSC measurements showed a broad signal due to polyethylene or ethylene blocks near the crystal melting temperature of 130 ° C. Extract the toluene-soluble portion with toluene from the polymer to yield 0.62 g of copolymer. The mole fraction of the DCPD component in the copolymer is 39 mol%, and the reduced viscosity η sp / c measured at 30 ° C. in a toluene solution having a concentration of 0.5 g / dl is 0.49 dl / g. 1 H-NMR spectrum of the copolymer is shown in FIG. The obtained ethylene-DCPD copolymer is hydrogenated by dissolving 5 mg of triisobutylaluminum in 10 ml of toluene as a 70 mg of ethylene-DCPD copolymer and a catalyst in a high pressure reactor. The hydrogenation is carried out at a temperature of 140 ° C. for 6 hours under a hydrogen pressure of 10 atm and then treated in a conventional manner to give 58 mg of hydrogenated polymer. The 1 H-NMR spectrum of the hydrogenated ethylene-DCPD copolymer is shown in FIG. 10. Reference Example 3 Isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride (hereinafter abbreviated i Pr (Cp) (Flu) ZrCl 2 ) as metallocene and PMAO as cocatalyst Attempts have been made to obtain DCPD homopolymers. Into a 50 ml Schlenk flask, which was purged with nitrogen, 4.2 mg of i Pr (Cp) (Flu) ZrCl 2 was quantitatively introduced, 5 ml of toluene solution of PMAO adjusted to 2 M concentration was added, and the mixture was 25 ° C. Activate by stirring for 10 minutes at. Thereafter, 10 ml of toluene and 3.3 g of DCPD were administered to polymerize at 40 ° C. for 18 hours, but no polymer was obtained. Reference Example 4 In order to determine the maximum amount of DCPD components that may be present in the copolymer of ethylene and DCPD prepared using a Kaminsky catalyst, the polymerization was carried out as a very large monomer ratio (F), in order to obtain a low yield of the copolymer. The polymerization reaction was carried out for a short time. Into a 50 ml Schlenk flask, which was purged with nitrogen, 4.2 mg of i Pr (Cp) (Flu) ZrCl 2 was quantitatively introduced and 5 ml of toluene solution of PMAO adjusted to 2 M concentration in the same manner as in Reference Example 3 Was added and the mixture was stirred at 25 ° C. for 10 minutes to activate. After adding 17.2 g of DCPD and raising the temperature to 40 ° C., ethylene gas is passed through a Schlenk flask system to produce an ethylene pressure atmosphere of 1 kg / cm 2 . 12, the ratio (F) of the monomer at the beginning of a polymerization reaction was measured at 51. 5 minutes after the start of the ethylene flow, the reaction is terminated and treated to yield 0.16 g of polymer. As measured by 1 H-NMR, the mole fraction of the DCPD component in the polymer was 50 mol%, and the DSC measurement resulted in a glass transition temperature of 189 ° C. The reduced viscosity η sp / c measured at 30 ° C. in the toluene solution having a concentration of 0.5 g / dl is 0.16 dl / g. 1 H-NMR spectrum of the copolymer is shown in FIG. 4. Reference Example 5 In order to measure the copolymerization curve of ethylene and DCPD, a 100 ml volume high pressure reactor at a reaction temperature of 40 ° C. was used for the copolymerization reaction. i Pr (Cp) (Flu) ZrCl 2 and PMAO were used as metallocenes. The copolymerization curve was measured according to a conventional method, and the polymerization reaction was carried out as variously filled monomer ratios, the reaction rate was reduced to 10% or less, the copolymer was separated and the composition ratio was measured. The results are shown in FIG. 11 (A). Reference Example 6 The copolymerization curves of ethylene and NB were measured in the same manner as in Reference Example 5 except that DCPD was replaced with NB. The results are shown in FIG. 11 (B). Reference Example 7 A 100 ml volume high pressure reactor was used to study the solubility of ethylene in toluene at 40 ° C. Add a fixed amount of ethylene to a high pressure reactor containing a fixed amount of toluene, reach equilibrium at 40 ° C., record the pressure and calculate the amount of ethylene dissolved at this pressure. 12 (C) shows the relationship between the pressure of ethylene and the solubility (molar fraction). Reference Example 8 The solubility of ethylene in DCPD was studied in the same manner as in Reference Example 7 except that toluene was replaced with DCPD. The results are shown in FIG. 12 as (D). Reference Example 9 In order to measure the copolymerization curve of ethylene and DCPD, a copolymerization reaction was carried out at a polymerization reaction temperature of 40 ° C. using a 100 ml volume high pressure reactor. Isopropylidene- (9-fluorenyl) (cyclopentadienyl) zirconium dichloride [hereafter i Pr (Cp) (Flu) ZrCl 2 ] as metallocene was used, and 1000 times PMAO as cocatalyst was used. The amount of mole was used. After cooling the high pressure reactor with liquefied nitrogen, a predetermined amount of ethylene is added to the high pressure reactor, the temperature is raised to 40 ° C., and the initial concentration of ethylene dissolved in toluene solvent is measured from the internal pressure. The copolymerization curve was measured by conventional methods, and the polymerization reaction was measured as various packed monomer ratios, the reaction rate was lowered to 10% or less, and the copolymer was separated, and then the composition ratio was measured. The results are shown in FIG. 13 as (E). Based on the above results, a Fineman-Ross plot is drawn, but F '= [ethylene] / [DCPD] (= 1 / F) and f' = ethylene component of the copolymer / DCPD for a more accurate calculation of r α ' . F ' 2 / f' and F '(f'-1) / f' as components (= 1 / f) are shown to define r α as the slope instead of the intercept. The results are shown as (H) in FIG. Since r D is 0, the value of r α = 1.4 was calculated from the slope of the line passing through the origin. This value was introduced in equation (II) to obtain 2.2 <F <16.8. Reference Example 10 Copolymer composition of ethylene and DCPD according to the same method as in Reference Example 9, except that ethylene-bis (1-indenyl) zirconium dichloride (hereinafter abbreviated as Et (Ind) 2 ZrCl 2 ) was used as the metallocene. The curve was measured. The result is shown as (F) in FIG. F ' 2 / f' and F '(f'-1) / f' are shown in the same manner as in Reference Example 9. The results are shown in FIG. 14 as (I). Since r D is 0, the value of r ( alpha) = 3.3 was computed from the slope of the line through an origin. This value was introduced into equation (II) to obtain a value of 5.2 <F <39.6. Reference Example 11 Ethylene and DCPD in the same manner as in Reference Example 9, except that dimethylsilylene-bis (1-indenyl) zirconium dichloride (abbreviated as Me 2 Si (Ind) 2 ZrCl 2 ) as the metallocene was used. The copolymerization composition curve of was measured. The result is shown as (G) in FIG. F ' 2 / f' and F '(f'-1) / f' are shown in the same manner as in Reference Example 9. The result is shown as (J) in FIG. Since r D is 0, the value of r ( alpha) = 2.7 was computed from the slope of the line through an origin. This value was introduced into equation (II) to obtain a value of 4.3 <F <32.4. Example 1 Copolymerization of ethylene and DCPD was carried out using i Pr (Cp) (Flu) ZrCl 2 as metallocene in the following manner. The blade-mounted stirring shaft is placed in a 500 ml volume three-necked flask and the vessel is purged with nitrogen gas, followed by filling with 90 ml of toluene and 30 g of DCPD. Thereafter, 40 mg of i Pr (Cp) (Flu) ZrCl 2 was dissolved in 46 ml of PMAO toluene solution adjusted to 2 M concentration, and then the metallocene-PMAO solution was added and stirred at 25 ° C. for 10 minutes to activate. . After raising the temperature to 40 ° C., the inside of the vessel is spread with ethylene and the polymerization reaction is started. The ethylene is fed while maintaining the ethylene pressure of the vessel at 1 atmosphere and the amount of ethylene introduced into the gas mass flow meter is observed. DCPD is added to the vessel in an amount of 0.6 mol relative to 1 mol of ethylene introduced during this period at intervals of 5 minutes after the start of the polymerization reaction. One hour after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 39.4 g. The reaction mixture is added dropwise with stirring to a large amount of methanol acidified with hydrochloric acid to precipitate a white solid. This solid is collected by filtration, washed sequentially with acetone, methanol and water and finally dried to give 63.4 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 43 mol% and the glass transition temperature is 162 ° C. Thus, the DCPD response rate is 71%. The molar ratio (F) of the polymerization reaction measured based on FIG. 12 is 12.3 at the beginning of the polymerization reaction and 6.6 at the end of the reaction. The glass transition temperature was measured by DSC measurement, and no crystal melting point corresponding to polyethylene was observed, thus confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.02 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.00, indicating no ethylene component blocks leading to the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.58 dl / g, which is a sufficiently high value. Example 2 The amount of filling in Example 1 was changed from 90 ml to 200 ml toluene, 40 mg to 20 mg i Pr (Cp) (Flu) ZrCl 2 , and 46 ml to 23 ml PMAO toluene solution. Copolymerization of ethylene and DCPD was performed under the same polymerization conditions as in Example 1. 1.5 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the reaction vessel after the start of the polymerization reaction is 42.5 g. The reaction mixture was treated in the same manner as in Example 1 to yield 60.3 g of copolymer. The molar fraction ratio of the DCPD component of the resulting copolymer is 39 mol% and the glass transition temperature is 142 ° C. Therefore, the response rate of DCPD is 62%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 8.1 at the initial stage of the polymerization reaction, and 6.3 at the end. The glass transition temperature was measured by DSC measurement, and no crystal melting point corresponding to polyethylene was observed, thus confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.03 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.02, indicating little formation of ethylene component blocks leading to the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.68 dl / g, which is a sufficiently high value. 1 H-NMR spectrum of the copolymer is shown in FIG. 3. Example 3 Copolymerization of ethylene and DCPD was carried out using a 500 ml stainless steel high pressure reactor equipped with a stirrer as the polymerization apparatus and i Pr (Cp) (Flu) ZrCl 2 as metallocene according to the following method. The high pressure reactor is purged with nitrogen and the reaction vessel is filled with 80 ml of toluene and 60 g of DCPD. Next, metallocene-PMAO solution prepared by dissolving 40 mg of i Pr (Cp) (Flu) ZrCl 2 was added to 46 ml of PMAO toluene solution adjusted to 2 M concentration, and stirred at 25 ° C. for 10 minutes to activate. Let's do it. The temperature is raised to 40 ° C., the inside of the reactor is replaced with ethylene, and the pressure of ethylene is raised to 2 kg / cm 2 to initiate the polymerization reaction. The introduced ethylene is continuously observed with a gas mass flow meter and the pressure of ethylene is continuously lowered to 2.0 → 1.6 → 1.2 → 0.8 → 0.4 → 0.2 kg / cm 2 and 80 mmol of ethylene is introduced each time. The pressure below 1 kg / cm 2 is the partial pressure of ethylene and nitrogen in the mixed gas. 4 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction when the ethylene pressure (partial pressure) is reduced to 0.2 kg / cm 2 . The reaction mixture was treated in the same manner as in Example 1 to give 56.1 g of copolymer. The molar fraction ratio of the DCPD component of the resulting copolymer is 46 mol% and the glass transition temperature is 175 ° C. Therefore, the response rate of DCPD is 75%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 10.8 at the beginning of the polymerization reaction, and 27.5 at the end. DSC measurements were used to determine the exact glass transition temperature, and no crystalline melting point corresponding to polyethylene was observed, confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.06 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.00, indicating that no ethylene component blocks were formed which caused the formation of undesirable crystalline moieties. The reduced viscosity η sp / c is 0.46 dl / g, which is a sufficiently high value. Example 4 Copolymerization of ethylene and DCPD was carried out according to the following method using the same polymerization apparatus and metallocene as in Example 3. The high pressure reactor is purged with nitrogen, and the reaction vessel is filled with 100 ml of toluene and 40 g of DCPD. Next, metallocene-PMAO solution prepared by dissolving 40 mg of i Pr (Cp) (Flu) ZrCl 2 was added to 46 ml of PMAO toluene solution adjusted to 2 M concentration, and stirred at 25 ° C. for 10 minutes to activate. Let's do it. The temperature is raised to 40 ° C., the inside of the reactor is replaced with ethylene, and the pressure of ethylene is raised to 2 kg / cm 2 to initiate the polymerization reaction. The introduced ethylene is continuously observed with a gas mass flow meter and the pressure of ethylene is continuously lowered to 2.0 → 1.7 → 1.4 → 1.1 → 0.8 → 0.5 kg / cm 2 and 80 mmol of ethylene is introduced each time. The pressure below 1 kg / cm 2 is the partial pressure of ethylene and nitrogen in the mixed gas. At the same time, it is added to the container in an amount of 0.4 mole with respect to 1 mole of ethylene introduced in the period at intervals of 5 minutes after the start of the polymerization reaction. Three hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction when the ethylene pressure (partial pressure) is reduced to 0.5 kg / cm 2 . The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 21.2 g. The reaction mixture was treated in the same manner as in Example 1 to give 54.4 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 45 mol% and the glass transition temperature is 171 ° C. Therefore, the response rate of DCPD is 71%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 7.3 at the beginning of the polymerization reaction, and 11.8 at the end. The glass transition temperature was measured by DSC measurement, and no crystal melting point corresponding to polyethylene was observed, thus confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.05 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.00, indicating that no ethylene component blocks were formed which caused the formation of undesirable crystalline moieties. The reduced viscosity η sp / c is 0.50 dl / g, which is a sufficiently high value. Example 5 The same polymerization reaction as in Example 1 except that 38 mg of ethylene-bis (1-indenyl) zirconium dichloride was used as metallocene instead of 40 mg of i Pr (Cp) (Flu) ZrCl 2 of Example 1 Copolymerization of ethylene and DCPD was performed under conditions. 3 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 41.7 g. The reaction mixture is added dropwise with stirring to a large amount of methanol acidified with hydrochloric acid to give a precipitate. This solid is collected by filtration, washed sequentially with acetone, methanol and water and finally dried to give 62.9 g of copolymer. The molar fraction of the DCPD component of the resulting copolymer is 41 mol% and the glass transition temperature is 152 ° C. Therefore, the response rate of DCPD is 67%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 12.3 at the beginning of the polymerization reaction and 7.7 at the end. DSC measurements were used to determine the exact glass transition temperature, and no crystalline melting point corresponding to polyethylene was observed, confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.03 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.02, indicating little formation of ethylene component blocks leading to the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.73 dl / g, which is a sufficiently high value. Example 6 i Pr (Cp) (Flu) ZrCl 2 was used as metallocene and trityl-tetrakis (pentafluorophenyl) borate (below [(C 6 H 5 ) 3 C] + [B (C 6 F) 5) 4 -] to be in a) crude abbreviated as catalyst according to the following method that is directed to example No. 1 was carried out the copolymerization reaction of ethylene and DCPD. The same polymerization reaction equipment as in Example 1 was used. The vessel is purged with nitrogen and filled with 140 ml of toluene and 30 g of DCPD. Next, in 1.5 ml of triisobutylaluminum (1 M concentration n-hexane solution), 10 mg of i Pr (Cp) (Flu) ZrCl 2 and 21.4 mg of [(C 6 H 5 ) 3 C] + [B ( C 6 F 5) 4 - thus] the dissolved was added to the produced catalyst solution, and activating the mixture was stirred for 5 minutes at 25 ℃. The rest of the polymerization reaction was carried out in the same manner as in Example 1. One hour after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 37.4 g. The reaction mixture was treated in the same manner as in Example 1 to yield 62.3 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 44 mol% and the glass transition temperature is 166 ° C. Therefore, the response rate of DCPD is 73%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 12.1 at the beginning of the polymerization reaction and 6.0 at the end. DSC measurements were used to determine the exact glass transition temperature, and no crystalline melting point corresponding to polyethylene was observed, confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.55 dl / g, which is a sufficiently high value. Example 7 i Pr (Cp) (Flu) ZrCl 2 in place of 9.6 mg of ethylene-bis (1-inde carbonyl) was carried out the copolymerization reaction of ethylene and DCPD under the same polymerization conditions as in Example 6, except for using zirconium dichloride . Two hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 40.5 g. The reaction mixture was treated in the same manner as in Example 1 to yield 63.3 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 42 mol% and the glass transition temperature is 158 ° C. Therefore, the response rate of DCPD is 70%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 12.1 at the beginning of the polymerization reaction and 6.9 at the end. DSC measurements were used to determine the exact glass transition temperature, and no crystalline melting point corresponding to polyethylene was observed, confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.03 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.00, indicating that no ethylene component blocks were formed which caused the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.78 dl / g, which is a sufficiently high value. Comparative Example 1 The polymerization reaction was carried out under the same polymerization reaction conditions as those in Example 1 except that DCPD was not added after the polymerization reaction was started. 60 minutes after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The reaction mixture was treated in the same manner as in Example 1 to obtain 34.6 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 36 mole%. Therefore, the response rate of DCPD is 84%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 12.3 at the beginning of the polymerization reaction, and 2.0 at the end. DSC measurements showed that the glass transition temperature was 130 ° C., but a wide change in heat capacity was observed and the glass transition temperature was unclear. However, no crystalline melting point corresponding to polyethylene was observed. The reduced viscosity η sp / c is 0.75 dl / g. Comparative Example 2 The polymerization was carried out under the same polymerization conditions as in Example 3 except that a constant ethylene pressure of 2 kg / cm 2 was maintained during the polymerization. One hour after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The reaction mixture was treated in the same manner as in Example 1 to yield 80.9 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 32 mole%. Therefore, the response rate of DCPD is 93%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 10.8 at the beginning of the polymerization reaction, and 0.76 at the end. DSC measurements showed a broad endothermic peak near 120 ° C. and a crystal melting point corresponding to polyethylene or partially crystalline ethylene blocks was observed. The copolymer was dissolved again in toluene and the insoluble portion was identified. DSC removal after removal of the soluble portion of toluene showed a broad and unclear but glass transition temperature at 114 ° C. The reduced viscosity η sp / c is 0.85 dl / g. Example 8 To a 300 ml high pressure reactor was added the ethylene / DCPD copolymer obtained in Example 1, 90 ml of toluene, 0.08 g of hydrogenation catalyst RuClH (CO) PPh 3 ) 3 and 170 under a hydrogen pressure of 40 kg / cm 2 . The hydrogenation reaction was carried out at 占 폚 for 5 hours. The reaction mixture is precipitated again in methanol, filtered off, washed and dried to give 14.8 g of copolymer. The 1 H-NMR (solvent: deuterated o-dichlorobenzene) spectrum of the resulting copolymer completely lost the signal of 5.5-5.8 ppm due to the unsaturated bond of DCPD, with a hydrogenation ratio of 99.9%. Peaks around 4.8-5.0 ppm, indicating terminal double bonds of the copolymer, were also hydrogenated. The reduced viscosity η sp / c was 0.58 and no decrease in molecular weight with hydrogenation was observed. The glass transition temperature is 160 ° C. and has not changed substantially from before hydrogenation. Example 9 The polymerization reaction was carried out in the same manner as in Example 4, and a small amount of isopropanol was added to terminate the reaction. 0.2 g of hydrogenation catalyst RuClH (CO) PPh 3 ) 3 was added to carry out hydrogenation at 170 ° C. for 5 hours under a hydrogen pressure of 40 kg / cm 2 . The reaction mixture was treated in the same manner as in Example 1 to yield 54.2 g of hydrogenated ethylene-DCPD copolymer. The 1 H-NMR spectrum of the resulting copolymer shows no signal due to unsaturated bonds and the hydrogenation ratio is 99.9%. The composition ratio of the hydrogenated DCPD component was 45 mol% based on 13 C-NMR measurement, the glass transition temperature was 170 ° C., and the reduced viscosity η sp / c was 0.49 dl / g, which is almost the same as the value obtained in Example 4. . Example 10 The hydrogenated ethylene-DCPD copolymers obtained in Examples 8 and 9 were further purified and the residual aluminum content in each polymer was reduced to less than 10 ppm. 0.5 wt% of Irganox 1010 was added to the copolymer, followed by injection molding at a resin temperature of 300 ° C. to obtain panels of 1.2 mm in thickness. Each panel has very high transparency and the light transmittance and haze values at a wavelength of 550 nm were 91.8% and 1.0% (copolymer of Example 8), and 92.0% and 0.8% (obtained in Example 9, respectively). Copolymer). Comparative Example 3 The ethylene-DCPD copolymers obtained in Comparative Example 1 and Comparative Example 2 were each hydrogenated according to the method of Example 8 to obtain ethylene-DCPD copolymers having a hydrogenation ratio of 99.9% or more. After purifying in the same manner as in Example 10 so that the residual aluminum content in the copolymer was less than 1 ppm, 0.5 wt% of Irganox 1010 was added and injection molded at a resin temperature of 300 ° C., each having a thickness of 1.2 mm. Obtain the plate. Unlike Example 10, the plate obtained has a low transparency and a large haze value. In particular, the copolymer obtained in Comparative Example 2 is very gloomy and opaque. Light transmittance and haze values at a wavelength of 550 nm are 82.3% and 10.6% (copolymer obtained in Comparative Example 1), and 48.6% and 43.9% (copolymer obtained in Comparative Example 2), respectively. Comparative Example 4 Copolymerization of ethylene and NB was carried out under the same polymerization conditions as in Example 1 except that 21 g of NB was used instead of 30 g of DCPD. 30 minutes after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of NB added to the vessel after the initiation of the polymerization reaction is 5.6 g. The reaction mixture was treated in the same manner as in Example 1 to yield 21.7 g of ethylene-NB copolymer. The mole fraction of the NB component of the resulting copolymer is 67 mol% and the glass transition temperature is 208 ° C. Therefore, the reaction rate of NB is 71%. The molar ratio (F) measured assuming that the solubility of ethylene in NB is approximately the same as that of DCPD, is 12.2 at the beginning of the polymerization reaction and 4.3 at the end. Injection molding was attempted after purification until the residual aluminum content was less than 100 ppm, but the viscosity of the resin was very high and a uniform molded body could not be obtained. Example 11 55.8 was carried out in the same manner as in Example 3, except that 2.7 g of 5-ethylidene-2-norbornane corresponding to 5 mol% of DCPD was further charged into 60 g of DCPD of Example 3 g of copolymer was obtained. The molar fractions of the DCPD component and 5-ethylene-2-norbornane component in the resulting copolymer were 43 mol% and 3 mol%, respectively, and the glass transition temperature was 170 ° C. The response rate of DCPD is therefore 70%. The molar ratio (F) measured assuming that the solubility of ethylene in 5-ethylene-2-norbornane is approximately equal to that of DCPD, is 10.7 at the beginning of the polymerization reaction and 32.7 at the end. DSC measurements were used to determine the exact glass transition temperature, and no crystalline melting point corresponding to polyethylene was observed, confirming that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. The reduced viscosity η sp / c is 0.44 dl / g, which is a sufficiently high value. Example 12 I Pr (Cp) (Flu) ZrCl 2 as metallocene and trityl-tetrakis (pentafluorophenyl) borate as cocatalyst (below [(C 6 H 5 ) 3 C] + [B (C 6 F 5 ) 4 ] - ) to copolymerize the ethylene and DCPD according to the following method. The blade-mounted stirring shaft was placed in a 500 ml three-necked flask and the vessel was purged with nitrogen gas, followed by 170 ml of toluene, 30 g of DCPD and 2.3 ml of triisobutylaluminum (1 M concentration n-hexane Solution) into a container. After raising temperature to 40 degreeC, the inside of a container is substituted by ethylene suitably. Later, 42 mg of [(C 6 H 5) 3 C] + [B (C 6 F 5) 4] - was added, and 20 mg of i Pr (Cp) (Flu) ZrCl 2 and initiates the polymerization reaction. During the polymerization reaction, ethylene is continuously fed to keep the pressure of ethylene in the vessel constant at 1 atm, and fresh DCPD is continuously added dropwise to the vessel at a rate of 0.5 g / min. One hour after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 30 g. The reaction mixture is added dropwise with stirring to a large amount of methanol acidified with hydrochloric acid to give a precipitate. This precipitate is collected by filtration, washed sequentially with acetone, methanol and water and finally dried to give 59.1 g of copolymer. The composition ratio of the DCPD component of the resulting copolymer is 42 mol%, and the glass transition temperature is 157 ° C. Therefore, the response rate of DCPD is 76%. The molar ratio (F) of the polymerization reaction measured based on FIG. 12 is 10.2 at the beginning of the polymerization reaction and 4.2 at the end of the reaction. The exact glass transition temperature was measured by DSC measurement, and the ΔTg representing the temperature difference between the falling point and the rising point of the curve was 8.9 ° C. In addition, no crystal melting point corresponding to polyethylene was observed, so that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.52 dl / g, which is a sufficiently high value. Example 13 As the metallocene was performed i Pr (Cp) (Flu) ZrCl 2 instead of Et (Ind) 2 ZrCl ethylene and copolymerization of DCPD in the following manner according to Example 12 using 2. The same polymerization reaction vessel as in Example 12 was charged with 140 ml of toluene, 30 g of DCPD and 2.2 ml of triisobutylaluminum (1 M concentration n-hexane solution). After raising temperature to 40 degreeC, the inside of a container is substituted by ethylene suitably. Later, 42 mg of [(C 6 H 5) 3 C] + [B (C 6 F 5) 4] - was added, and 19 mg of i Pr (Cp) (Flu) ZrCl 2 and initiates the polymerization reaction. During the polymerization reaction, ethylene is continuously supplied to keep the pressure of ethylene in the vessel constant at 1 atm, and fresh DCPD is continuously added dropwise to the vessel at a rate of 0.25 g / min. 2.5 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 37.5 g. The reaction mixture was treated in the same manner as in Example 12 to yield 66.1 g of copolymer. The molar fraction of the DCPD component in the resulting copolymer is 40 mol% and the glass transition temperature is 150 ° C. Therefore, the DCPD response rate is 74%. The molar ratio (F) of the polymerization reaction measured based on FIG. 12 is 11.9 at the beginning of the polymerization reaction and 6.6 at the end of the reaction. The exact glass transition temperature was measured via DSC measurement, and ΔTg was 10.0 ° C. In addition, no crystal melting point corresponding to polyethylene was observed, so that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.75 dl / g, which is a sufficiently high value. Example 14 Copolymerization of ethylene and DCPD was carried out using Me 2 Si (Ind) 2 ZrCl 2 as metallocene and polymethylaluminoxane (PMAO) as cocatalyst according to the following method. The same polymerization reaction equipment as in Example 12 was used. After the vessel is purged with nitrogen gas, the vessel is filled with 130 ml of toluene, 30 g of DCPD and 2 ml of toluene solution of PMAO adjusted to 2 M concentration. The temperature is raised to 40 ° C. and the interior of the reactor is replaced with ethylene. Next, a metallocene-PMAO solution prepared by dissolving 20 mg of Me 2 Si (Ind) 2 ZrCl 2 was added to 22 ml of PMAO toluene solution adjusted to 2 M concentration, and stirred at 25 ° C. for 10 minutes to activate. Start the polymerization reaction. During the polymerization reaction, ethylene is continuously supplied to keep the pressure of ethylene in the vessel constant at 1 atm, and fresh DCPD is continuously added dropwise to the vessel at a rate of 0.2 g / min. 3 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the vessel after the initiation of the polymerization reaction is 36 g. The reaction mixture was treated in the same manner as in Example 12 to yield 61.5 g of copolymer. The molar fraction of the DCPD component in the resulting copolymer is 42 mol% and the glass transition temperature is 158 ° C. Thus, the DCPD response rate is 72%. The molar ratio (F) of the polymerization reaction measured based on FIG. 12 is 11.1 at the beginning of the polymerization reaction and 5.7 at the end of the reaction. The exact glass transition temperature was measured via DSC measurement, and ΔTg was 9.5 ° C. In addition, no crystal melting point corresponding to polyethylene was observed, so that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.71 dl / g, which is a sufficiently high value. Example 15 The same polymerization as in Example 12 except that the DCPD addition rate in Example 12 was changed to 0.8 g / min for the first 20 minutes, to 0.5 g / min for the next 20 minutes, and 0.2 g / min for the last 20 minutes. Copolymerization of ethylene and DCPD was carried out under the reaction conditions. One hour after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The total amount of DCPD added to the reaction vessel after the start of the polymerization reaction is 30 g. The reaction mixture was treated in the same manner as in Example 12 to yield 58.9 g of copolymer. The mole fraction ratio of the DCPD component of the resulting copolymer is 43 mol%, and the glass transition temperature is 161 ° C. Therefore, the response rate of DCPD is 77%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 10.2 at the beginning of the polymerization reaction, and 4.1 at the end. DSC measurements gave the correct glass transition temperature and ΔTg was 8.6 ° C. In addition, no crystal melting point corresponding to polyethylene was observed, so that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.50 dl / g, which is a sufficiently high value. Comparative Example 5 The polymerization reaction was carried out under the same conditions as in Example 13 except that no new DCPD was added after the polymerization reaction was started. 2 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The reaction mixture was treated in the same manner as in Example 12 to yield 35.9 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 35 mole%. Therefore, the response rate of DCPD is 86%. DSC measurements showed that the glass transition temperature was 130 ° C., but a wide change in heat capacity was observed, the glass transition temperature was unclear, and ΔTg was 19.6 ° C. A faint crystal melting point corresponding to polyethylene was observed. The reduced viscosity η sp / c is 0.80 dl / g. Example 16 To a 300 ml volume high pressure reactor was added 15 g of ethylene / DCPD copolymer, 90 ml toluene, 50 mg of hydrogenation catalyst RuClH (CO) PPh 3 ) 3 obtained in Example 12 and 40 kg / cm 2 of hydrogen The hydrogenation reaction was carried out at 170 ° C. for 5 hours under pressure. The reaction mixture is precipitated in methanol, filtered off, washed and dried to give 14.8 g of copolymer. In the 1 H-NMR (solvent: deuterated o-dichlorobenzene) spectrum of the resulting copolymer, the signal of 5.5-5.8 ppm due to unsaturated bonds of DCPD disappeared completely and the hydrogenation ratio was 99.9%. Peaks around 4.8-5.0 ppm, indicating terminal double bonds of the copolymer, were also hydrogenated. The reduced viscosity η sp / c was 0.50 dl / g, and no decrease in molecular weight with hydrogenation was observed. The glass transition temperature is 154 ° C. and has not changed substantially from before the hydrogenation. Example 17 The ethylene-DCPD copolymer obtained in Example 13 was hydrogenated in the same manner as in Example 16 to obtain a hydrogenated ethylene-DCPD copolymer having a degree of hydrogenation of at least 99.9%. The reduced viscosity η sp / c of the polymer was 0.72 dl / g, and no decrease in molecular weight with hydrogenation was observed. The glass transition temperature is 148 ° C. and has not changed substantially from before hydrogenation. Example 18 The hydrogenated ethylene-DCPD copolymers obtained in Examples 16 and 17 were further purified and the residual aluminum content in each polymer was reduced to less than 10 ppm. 0.5 wt% of Irganox 1010 was added to each copolymer, followed by injection molding at a resin temperature of 300 deg. C to obtain plates of 1.2 mm in thickness. Each panel has very high transparency and has a wavelength of 550 nm and of 92.1% and 0.8% (copolymer obtained in Example 16), and 91.7% and 1.0% (copolymer obtained in Example 17), respectively. The light transmittance haze value was shown. Comparative Example 6 The ethylene-DCPD copolymer obtained in Comparative Example 5 was hydrogenated according to the method of Example 16 to obtain a hydrogenated ethylene-DCPD copolymer having a degree of hydrogenation of at least 99.9%. After purifying in the same manner as in Example 18 so that the residual aluminum content in the copolymer was less than 100 ppm, 0.5 wt% of Irganox 1010 was added and injection molded at a resin temperature of 300 ° C., each having a thickness of 1.2 mm. Obtain the plate. Unlike Example 18, this panel has a low transparency and a large haze value. Light transparency and haze values at a wavelength of 550 nm are 74.7% and 18.3%, respectively. Example 19 A 500 ml stainless steel reaction vessel equipped with a stirrer is charged with 200 g toluene, 50 g DCPD, 395 mg 1-hexene and 780 mg triisobutylaluminum under a nitrogen atmosphere. When the nitrogen pressure of the reaction system is 1 atm, the nitrogen outlet is closed. After adjusting the temperature to 30 ℃, the partial pressure of ethylene in the reaction system by the addition of ethylene to the reaction vessel under an ethylene pressure of 1.5 kg / cm 2 and maintained at 0.5 kg / cm 2. Later, 35 mg of [(C 6 H 5) 3 C] + [B (C 6 F 5) 4] - was added, and 16 mg of Et (Ind) 2 ZrCl 2 and initiates the polymerization reaction. The partial pressure of ethylene is maintained at 0.5 kg / cm 2 during the polymerization reaction and the rate of consumption of ethylene is observed with a flow meter attached to the apparatus. 3 hours after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The reaction mixture was treated in the same manner as in Example 12 to yield 51.0 g of copolymer. The molar fraction ratio of the DCPD component of the resulting copolymer is 40 mol%, and the glass transition temperature is 141 ° C. Therefore, the response rate of DCPD is 78%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 21.0 at the beginning of the polymerization reaction, 8.4 when 60% of DCPD is consumed, and 6.2 when 70% of DCPD is consumed. DSC measurements were used to determine the correct glass transition temperature and ΔTg was 11.1 ° C. In addition, no crystal melting point corresponding to polyethylene was observed, so that the resulting copolymer did not contain polyethylene or partially crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.03 by 1 H-NMR, indicating no DCPD component crosslinking. In addition, 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.08, indicating that very little ethylene component blocks were formed, causing the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.58 dl / g, which is a sufficiently high value. Example 20 A 500 ml stainless steel reaction vessel equipped with a stirrer is charged with 200 g toluene, 33 g DCPD, 407 mg 1-hexene and 780 mg triisobutylaluminum under a nitrogen atmosphere. When the nitrogen pressure of the reaction system is 1 atm, the nitrogen outlet is closed. After adjusting the temperature to 30 ℃, the partial pressure of ethylene in the reaction system by the addition of ethylene to the reaction vessel under an ethylene pressure of 1.5 kg / cm 2 and maintained at 0.5 kg / cm 2. Later, 38 mg of [(C 6 H 5) 3 C] + [B (C 6 F 5) 4] - and the addition of Et (Ind) 2 ZrCl 2 in 16 mg to initiate the polymerization reaction. The partial pressure of ethylene is maintained at 0.5 kg / cm 2 during the polymerization reaction and the rate of consumption of ethylene is observed with a flow meter attached to the apparatus. Thereafter, 17 g of DCPD was added while maintaining the ratio (V E / V D ) of the ethylene consumption rate (V E , mol / minute) to the addition rate of DCPD (V D , mol / minute) at 58/42. do. The maintenance is performed by observing the rate of ethylene as a flow meter and feeding this rate back to the DCPD feeder. 102 minutes after the start of the polymerization reaction, a small amount of isopropanol is added to terminate the reaction. The reaction mixture was treated in the same manner as in Example 12 to yield 54.0 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 42 mol% and the glass transition temperature is 148 ° C. The response rate of DCPD is 83%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 15.0 at the beginning of the polymerization reaction, 8.4 when 60% of DCPD is consumed, and 6.2 when 70% of DCPD is consumed. The glass transition temperature was obtained by DSC measurement and ΔTg was 8.6 ° C. In addition, no crystal melting point corresponding to the polyethylene and / or ethylene component blocks was observed, thus confirming that the resulting copolymer did not contain polyethylene or crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.02 by 1 H-NMR, indicating no DCPD component crosslinking. Also 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.02, indicating little formation of ethylene component blocks leading to the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.41 dl / g, which is a sufficiently high value. Example 21 A 2 l reaction vessel is charged with 600 g toluene, 150 g DCPD, 0.50 g 1-hexene and 1.2 g triisobutylaluminum under a nitrogen atmosphere. The reaction vessel is purged with ethylene. After adjusting the temperature to 30 ° C., 0.114 g of [(C 6 H 5 ) 3 C] + [B (C 6 F 5 ) 4 ] − and 51 mg of Et (with ethylene flowing under atmospheric pressure into the reaction vessel) Ind) 2 ZrCl 2 is added to initiate the polymerization reaction. Ethylene continues to flow under atmospheric pressure in the reaction vessel. During the polymerization reaction, the rate of consumption of ethylene is observed with a flow meter attached to the apparatus. When 22.8 l of ethylene flows into the reaction vessel, a small amount of isopropanol is added to terminate the reaction. The reaction mixture was treated in the same manner as in Example 12 to yield 150 g of copolymer. The mole fraction of the DCPD component of the resulting copolymer is 45 mol% and the glass transition temperature is 145 ° C. The response rate of DCPD is 83%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 10.3 at the beginning of the polymerization reaction, and is 4.1 when 60% of DCPD is consumed. The glass transition temperature was obtained by DSC measurement and ΔTg was 6.1 ° C. In addition, no crystal melting point corresponding to the polyethylene and / or ethylene component blocks was observed, thus confirming that the resulting copolymer did not contain polyethylene or crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.04 by 1 H-NMR, indicating no DCPD component crosslinking. In addition, 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.01, indicating that very little ethylene component blocks were formed, causing the formation of undesirable crystalline moieties. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.59 dl / g, which is a sufficiently high value. 3.6 g of the resulting polymer is dissolved in 20.4 g of toluene in a high pressure reactor. To this solution is added 30 mg of cobalt triacetylacetonate [Co (acac) 3 and 50 mg of triisobutylaluminum. The hydrogenation is then carried out at 130 ° C. for 2 hours under hydrogen pressure of 20 atmospheres. After hydrogenation, the reaction mixture is added dropwise with stirring to a large amount of methanol acidified with hydrochloric acid to give a precipitate. This precipitate is collected by filtration, washed sequentially with acetone, methanol and water and finally dried to give 3.4 g of hydrogenated copolymer. In the 1 H-NMR spectrum of FIG. 6, there are no peaks attributable to C = C double bonds in the DCPD components of the initial copolymers of δ 5.54 and 5.64 ppm, meaning that at least 99.9% of C = C double bonds are hydrogenated do. The spectrum shows multiple peaks but very sharp peaks at δ 1.07, 1.3, 1.47, 1.65, 1.8, 2.0 and 2.4 ppm. H ' 2.20 / H' 2.40 was determined to be 0.038, which means a high level of alternating arrangement for the tricyclodecane ring component and the ethylene component. The copolymer obtained exhibited an accurate glass transition temperature Tg of 140 ° C. and ΔTg of 7.8 ° C. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.55 dl / g, which is a sufficiently high value. Example 22 A 500 ml reaction vessel is filled with 80 g toluene, 20 g DCPD and 300 mg triisobutylaluminum under nitrogen atmosphere. The reaction vessel is purged with ethylene. After adjusting the temperature to 30 ℃, the 28 mg and to ethylene flow at atmospheric pressure in a reaction vessel [(C 6 H 5) 3 C] + [B (C 6 F 5) 4] - and 13 mg of i Pr (Cp) (Flu) ZrCl 2 is added to initiate the polymerization reaction. Ethylene continues to flow into the reaction vessel under atmospheric pressure. The rate of consumption of ethylene during the polymerization reaction is monitored by a flow meter attached to the apparatus. Sample a small amount of solution as 22.8 l of ethylene flows into the container. This solution is treated in the same manner as in Example 12 to obtain a copolymer. The mole fraction ratio of the DCPD component of the resulting copolymer is 43 mol% and the glass transition temperature is 155 ° C. The response rate of DCPD is 75%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 10.3 at the beginning of the polymerization reaction, and is 4.1 when 60% of DCPD is consumed. DSC measurements were used to determine the correct glass transition temperature and ΔTg was 6.1 ° C. In addition, no crystal melting point corresponding to the polyethylene and / or ethylene component blocks was observed, thus confirming that the resulting copolymer did not contain polyethylene or crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.03 by 1 H-NMR, indicating no DCPD component crosslinking and 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.01, which is an undesirable crystalline moiety. Almost no ethylene component block is formed which causes the formation of. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.48 dl / g, which is a sufficiently high value. After sampling the polymer solution is transferred to a high pressure reactor and 107 mg of cobalt triacetylacetonate [Co (acac) 3 ] and 300 mg of triisobutylaluminum are added. The hydrogenation is then carried out at 130 ° C. for 2 hours under a hydrogen pressure of 27 atmospheres. After hydrogenation, the reaction mixture is added dropwise with stirring to a large amount of methanol acidified with hydrochloric acid to give a precipitate. This precipitate is collected by filtration, washed sequentially with acetone, methanol and water and finally dried to yield 18.5 g of hydrogenated copolymer. In the 1 H-NMR spectrum of FIG. 7, there are no peaks attributable to C = C double bonds in the DCPD components of the initial copolymers of δ 5.54 and 5.64 ppm, meaning that at least 99.9% of C = C double bonds are hydrogenated. . The spectrum shows multiple peaks but very sharp peaks at δ 1.07, 1.3, 1.47, 1.65, 1.8, 2.0 and 2.4 ppm. H ' 2.20 / H' 2.40 was determined to be 0.031, which means a high level of alternating arrangement for the tricyclodecane ring component and the ethylene component. The obtained copolymer exhibited a glass transition temperature Tg of 149 ° C and ΔTg of 9.2 ° C. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.45 dl / g, which is a sufficiently high value. Example 23 A 3 l stainless steel reaction vessel is charged with 1380 g of toluene, 201 g of DCPD, 3.4 g of triisobutylaluminum under nitrogen atmosphere. When the nitrogen pressure of the reaction system is 1 atm, the nitrogen outlet is closed. After adjusting the temperature to 30 ℃, it maintains a partial pressure of ethylene in the reaction system by the addition of ethylene to the reaction vessel under an ethylene pressure of 2.0 kg / cm 2 to 1.0 kg / cm 2. Then, in 225 mg [(C 6 H 5 ) 3 C] + [B (C 6 F 5) 4] - was added, and divided by the amount of i Pr (Cp) (Flu) ZrCl 2 equivalent of 122 g for five Add once to polymerize. During the polymerization reaction, the partial pressure of ethylene is maintained at 1.0 kg / cm 2 and the rate of consumption of ethylene is observed with a flow meter attached to the reaction apparatus. Thereafter, 139 g of DCPD was added while maintaining the ratio (V E / V D ) of the ethylene consumption rate (V E , mol / minute) to the addition rate of DCPD (V D , mol / minute) at 60/40. do. The maintenance is performed by observing the rate of consumption of ethylene as a flow meter and feeding it back to the DCPD feeder. A small amount of solution is sampled 173 minutes after the start of the polymerization reaction and when 55.4 l of ethylene flows into the vessel. This solution is treated in the same manner as in Example 12 to obtain a copolymer. The mole fraction of the DCPD component of the resulting copolymer is 42 mole%, and the glass transition temperature is 148 ° C. The response rate of DCPD is 70%. The molar ratio (F) of this polymerization reaction measured based on FIG. 12 is 6.6 at the beginning of the polymerization reaction, and is 4.1 when 60% of DCPD is consumed. DSC measurements gave the correct glass transition temperature and ΔTg was 13 ° C. In addition, no crystal melting point corresponding to the polyethylene and / or ethylene component blocks was observed, thus confirming that the resulting copolymer did not contain polyethylene or crystalline ethylene blocks. H 1.85 / H 3.05 was determined to be 0.03 by 1 H-NMR, indicating no DCPD component crosslinking, and 1/4 x (I 1.3 / I 3.05 ) was determined to be 0.00, which is an undesirable crystalline moiety. It indicates that no ethylene component block is formed which causes the formation of. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.56 dl / g, which is a sufficiently high value. After sampling the polymer solution is transferred to a high pressure reactor and 3.0 g of cobalt triacetylacetonate [Co (acac) 3 ] and 5.1 g of triisobutylaluminum are added. After hydrogenation, hydrogenation is carried out at 130 ° C. for 3 hours under hydrogen pressure of 45 atmospheres. After hydrogenation, the reaction mixture is added dropwise with stirring to a large amount of methanol acidified with hydrochloric acid to give a precipitate. This precipitate is collected by filtration, washed sequentially with acetone, methanol and water and finally dried to give 305 g of hydrogenated copolymer. In the 1 H-NMR spectrum of FIG. 8, there are no peaks attributable to C = C double bonds in the DCPD components of the original copolymers of δ 5.54 and 5.64 ppm, meaning that at least 99.9% of C = C double bonds are hydrogenated. . The spectrum shows multiple peaks but very sharp peaks at δ 1.07, 1.3, 1.47, 1.65, 1.8, 2.0 and 2.4 ppm. H '2.20 / H' 2.40 was measured as 0.024, which means that the alternating arrangement of the high level with respect to the tricyclodecane ring component and ethylene component. The copolymer obtained exhibited an accurate glass transition temperature Tg of 143 ° C. and ΔTg of 9.6 ° C. In a toluene solution with a concentration of 0.5 g / dl, the reduced viscosity η sp / c measured at 30 ° C. is 0.53 dl / g, which is a sufficiently high value. According to the invention it is possible to obtain α-olefin-DCPD copolymers having a high level of alternating copolymerization and high chemical homogeneity. Thus, hydrogenated α-olefin-DCPD copolymers obtained by hydrogenation using these α-olefin-DCPD copolymers as precursors have high optical homogeneity and high transparency and are therefore suitable for the use of optical disc materials and other optical materials. According to the present invention, it is possible to provide a cyclic olefin copolymer suitable for optical purposes without using expensive polycyclic olefins.
权利要求:
Claims (28) [1" claim-type="Currently amended] (1) consisting essentially of 0 to 39 mol% of an α-olefin component represented by the following formula (1A) and 61 to 100 mol% of cycloolefin component represented by the following formula (1B), [Formula 1A] [Formula 1B] [Wherein, R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group] (2) α-olefin-cycloolefin copolymer having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. [2" claim-type="Currently amended] (1) consisting essentially of repeating units represented by the following formulas (1A), (1B), (1C) and (1D), [Formula 1A] [Formula 1B] [Formula 1C] [Formula 1D] [Wherein R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group, n is 0 or 1, m is a positive integer of 0 or 1 to 3, and p is 0 or 1 R 3 to R 22 are the same or different and each is a hydrogen atom, a halogen atom, a C 6-10 aromatic hydrocarbon group or a C 1-12 saturated or unsaturated aliphatic hydrocarbon group, or R 19 and R 20 or R 21 and R 22 May together form an alkylidene group, or R 19 or R 20 and R 21 or R 22 may form a ring which may be an aromatic ring or a ring which may contain two carbon atoms to which they are bonded and one or more double bonds; And q is an integer from 2 to 8] The composition ratio of [1A], [1B], [1C] and [1D], representing the mole% of each repeating unit (1A), (1B), (1C) and (1D) is ([1A] + [1B] ) / ([1C] + [1D]) = 95-99.9 / 0.1-5, [1A] / [1B] = 0-39 / 61-100 and [1D] / [1C] = 0-95 / 5- Is in the range of 100, (2) α-olefin-cycloolefin copolymer having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. [3" claim-type="Currently amended] The α-olefin-cycloolefin copolymer according to claim 1, wherein no peak is interpreted in the DSC curve that is interpretable as melting of the polyethylene and / or ethylene component blocks. [4" claim-type="Currently amended] The α-olefin-cycloolefin copolymer according to claim 1, wherein ΔTg, which represents the temperature difference between the falling point and the rising point of the DSC curve, is 15 ° C. or less. [5" claim-type="Currently amended] The α-olefin-cycloolefin copolymer according to claim 1, wherein the glass transition temperature (Tg: ° C) satisfies the following formula, and the α-olefin is ethylene: -22.7 + 2.84 m D + 0.0262 m D 2 <Tg <-2.7 + 2.84 m D + 0.0262 m D 2 [Wherein m D represents the mole fraction (%) of the cyclic olefin component in the polymer and is in the range of 38 to 50%]. [6" claim-type="Currently amended] The ratio (H 1.85 / H 3.05 ) of the bone intensity (H 1.85 ) of δ 1.85 ppm to the intensity (H 3.05 ) of the δ 3.05 ppm peak of the 1 H-NMR spectrum is 0.15 or less, The α-olefin-cycloolefin copolymer, wherein the α-olefin is ethylene. [7" claim-type="Currently amended] Ratio according to claim 1, 1 H-NMR spectra of δ 3.05 ppm in the peak area (I 3.05) of polyethylene and / or δ 1.3 ppm peak area (I 1.3) of can be interpreted as ethylene component block to the (I 1.3 / Α -olefin-cycloolefin copolymer, wherein 1/4 of I 3.05 ) is 0.05 or less and α-olefin is ethylene. [8" claim-type="Currently amended] The central metal is titanium, Α-olefin-cycloolefin copolymers comprising copolymerizing α-olefins having at least two carbon atoms with dicyclopentadiene in the presence of at least one metallocene catalyst and zirconium or hafnium and at least one cocatalyst Method of manufacture: [Formula I] F = [dicyclopentadiene] / [α-olefin]> 4. [9" claim-type="Currently amended] From the start of the polymerization reaction, the molar ratio (F = [dicyclopentadiene] / [α-olefin]) of the monomers in the reaction system while the reaction rate of the dicyclopentadiene added to the polymerization reaction system reaches 60% is expressed by the following formula (II) While maintaining a range satisfying the formula, α-olefin and dicyclopentadiene having two or more carbon atoms in the presence of at least one metallocene catalyst and at least one promoter containing titanium, zirconium or hafnium Process for preparing α-olefin-cycloolefin copolymer comprising copolymerizing: [Formula II] 38/62 <F / (F + r α ) <48/52 [10" claim-type="Currently amended] 10. The process according to claim 8 or 9, wherein the α-olefin is ethylene. [11" claim-type="Currently amended] The method according to claim 8 or 9, wherein the central metal of the metallocene is zirconium and the promoter is aluminoxane. [12" claim-type="Currently amended] 10. The method according to claim 8 or 9, wherein the center metal of the metallocene is zirconium and the promoter is an ionic boron compound. [13" claim-type="Currently amended] The molar ratio (F) of the monomers in the reaction system satisfies the formula (I) or formula (II) until the reaction rate of the dicyclopentadiene added to the polymerization reaction system reaches 70%. Method characterized in that the range. [14" claim-type="Currently amended] 10. The process according to claim 8 or 9, wherein the ratio (F) of the monomers is in the range of F> 5.5. [15" claim-type="Currently amended] (1) consisting essentially of 0 to 39 mol% of an α-olefin component represented by the following formula (1Aa) and 61 to 100 mol% of cycloolefin component represented by the following formula (1Ba), Formula 1Aa] [Formula 1Ba] [Wherein, R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group] (2) α-olefin-cycloolefin copolymer having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. [16" claim-type="Currently amended] (1) consisting essentially of repeating units represented by the following formulas (1Aa), (1Ba), (1Ca) and (1Da), Formula 1Aa] [Formula 1Ba] Formula 1Ca] Formula 1Da] [Wherein R 1 and R 2 are each a hydrogen atom or a C 1-16 saturated aliphatic hydrocarbon group, n is 0 or 1, m is a positive integer of 0 or 1 to 3, and p is 0 or 1 R 3 to R 22 are the same or different and each is a hydrogen atom, a halogen atom, a C 6-10 aromatic hydrocarbon group or a C 1-12 saturated aliphatic hydrocarbon group, or R 19 and R 20 or R 21 and R 22 are Together may form an alkylidene group, or R 19 or R 20 and R 21 or R 22 may form a ring which may be an aromatic ring with the two carbon atoms to which they are attached, q is an integer from 2 to 8; The composition ratios of [1Aa], [1Ba], [1Ca] and [1Da] representing the mole% of each repeating unit (1Aa), (1Ba), (1Ca) and (1Da) are ([1Aa] + [1Ba] ) / ([1Ca] + [1Da]) = 95-99.9 / 0.1-5, [1Aa] / [1Ba] = 0-39 / 61-100 and [1Da] / [1Ca] = 0-95 / 5- Is in the range of 100, (2) α-olefin-cycloolefin copolymer having a reduced viscosity η sp / c in the range of 0.1 to 10 dl / g as measured at 30 ° C. in a toluene solution with a concentration of 0.5 g / dl. [17" claim-type="Currently amended] 16. The α-olefin-cycloolefin copolymer according to claim 15, wherein no peak is interpretable in the DSC curve that is interpretable as melting of the polyethylene and / or ethylene component blocks. [18" claim-type="Currently amended] The α-olefin-cycloolefin copolymer according to claim 15, wherein Tg, which represents the temperature difference between the falling point and the rising point of the DSC curve, is 15 ° C or less. [19" claim-type="Currently amended] The α-olefin-cycloolefin copolymer according to claim 15, wherein the glass transition temperature (Tg: ° C.) satisfies the following formula, and wherein the α-olefin is ethylene. -32.7 + 2.84 m T + 0.0262 m T 2 <Tg <-7.7 + 2.84 m T + 0.0262 m T 2 [Wherein m T represents the mole fraction (%) of the cyclic olefin component in the polymer and is in the range of 38 to 50%]. [20" claim-type="Currently amended] 16. The method of claim 15, 1 H-NMR spectra of δ 2.40 ppm in the ratio (H '2.20 / H' 2.40 ) of 'of δ 2.20 ppm goal for (2.40 strength (H strength of a peak H), 2.20) is It is 0.07 or less and alpha-olefin is an olefin, The alpha-olefin-cycloolefin copolymer characterized by the above-mentioned. [21" claim-type="Currently amended] (1) The central metal while maintaining the molar ratio (F) of the monomer in the reaction system within the range satisfying the following formula (I) while the reaction rate of the dicyclopentadiene added to the polymerization reaction system from the start of the polymerization reaction reaches 60%. In the presence of a catalyst containing at least one metallocene of titanium, zirconium or hafnium and at least one cocatalyst, an α-olefin having at least two carbon atoms and dicyclopentadiene are copolymerized, and (2) the degree of hydrogenation is 99 Process for preparing α-olefin-cycloolefin copolymer comprising hydrogenating the resulting copolymer until at least%: [Formula I] F = [dicyclopentadiene] / [α-olefin]> 4. [22" claim-type="Currently amended] (1) The molar ratio (F = [dicyclopentadiene] / [α-olefin]) of the monomers in the reaction system while the reaction rate of the dicyclopentadiene added to the polymerization reaction system reaches 60% from the start of the polymerization reaction is expressed by the following equation. Α-olefin and dicyclo having two or more carbon atoms in the presence of at least one metallocene and a catalyst containing at least one metallocene whose central metal is titanium, zirconium or hafnium while maintaining in a range satisfying (II) A process for producing an α-olefin-cycloolefin copolymer comprising copolymerizing pentadiene and (2) hydrogenating the resulting copolymer until the degree of hydrogenation is at least 99%: [Formula II] 38/62 <F / (F + r α ) <48/52 [Wherein, r α represents the ratio of the reactivity of the monomer of the α-olefin to DCPD and the α-olefin]. [23" claim-type="Currently amended] 23. The method of claim 21 or 22, wherein the α-olefin is ethylene. [24" claim-type="Currently amended] 23. The method of claim 21 or 22, wherein the central metal of the metallocene is zirconium and the promoter is aluminoxane. [25" claim-type="Currently amended] 23. The method of claim 21 or 22, wherein the center metal of the metallocene is zirconium and the promoter is an ionic boron compound. [26" claim-type="Currently amended] 23. The molar ratio (F) of the monomers in the reaction system satisfies the formula (I) or (II) until the reaction rate of the dicyclopentadiene added to the polymerization reaction system reaches 70%. Method characterized in that the range. [27" claim-type="Currently amended] 23. The method of claim 21 or 22, wherein the ratio (F) of the monomers is in the range of F> 5.5. [28" claim-type="Currently amended] An optical material composed mainly of the α-olefin-cycloolefin copolymer according to any one of claims 15 to 20.
类似技术:
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同族专利:
公开号 | 公开日 CN1134469C|2004-01-14| ES2195312T3|2003-12-01| WO1998033830A1|1998-08-06| EP0891382B1|2003-05-28| CN1280140A|2001-01-17| EP0891382A1|1999-01-20| CN1222920A|1999-07-14| CA2249714A1|1998-07-31| TW440571B|2001-06-16| US6191243B1|2001-02-20| JP2000509754A|2000-08-02| DE69814991T2|2004-02-26| AT241652T|2003-06-15| DE69814991D1|2003-07-03|
引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题
法律状态:
1997-01-31|Priority to JP97-18491 1997-01-31|Priority to JP1849197 1997-03-06|Priority to JP5163897 1997-03-06|Priority to JP97-51638 1998-01-29|Application filed by 야스이 쇼사꾸, 데이진 가부시키가이샤, 빌프리더 하이더, 바이엘 악티엔게젤샤프트 1998-01-29|Priority to PCT/JP1998/000366 2000-11-06|Publication of KR20000064810A
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申请号 | 申请日 | 专利标题 JP97-18491|1997-01-31| JP1849197|1997-01-31| JP5163897|1997-03-06| JP97-51638|1997-03-06| PCT/JP1998/000366|WO1998033830A1|1997-01-31|1998-01-29|Alpha-olefin-cycloolefin copolymers and process for their production| 相关专利
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