Source: https://patents.google.com/patent/JP6039906B2/en
Timestamp: 2019-11-17 08:39:40
Document Index: 779358307

Matched Legal Cases: ['Application No. 545403', 'Application No. 547718', 'Application No. 702475', 'Application No. 87268', 'Application No. 8003', 'Application No. 593756', 'Application No. 07', 'Application No. 304314', 'application No. 07', 'application No. 08']

JP6039906B2 - Shear thinning ethylene / α-olefin interpolymers and methods for their production - Google Patents
Shear thinning ethylene / α-olefin interpolymers and methods for their production Download PDF
JP6039906B2
JP6039906B2 JP2012031987A JP2012031987A JP6039906B2 JP 6039906 B2 JP6039906 B2 JP 6039906B2 JP 2012031987 A JP2012031987 A JP 2012031987A JP 2012031987 A JP2012031987 A JP 2012031987A JP 6039906 B2 JP6039906 B2 JP 6039906B2
JP2012031987A
JP2012136706A (en
ドウェイン キャディー ラリー
マーク ヒューズ モーガン
ケネス ラフナー マイケル
アラン マイスク ラリー
ラジクラル パリクー ディーパク
1998-11-02 Priority to US10656998P priority Critical
1998-11-02 Priority to US60/106,569 priority
2012-02-16 Application filed by ダウ グローバル テクノロジーズ エルエルシー, ダウ グローバル テクノロジーズ エルエルシー filed Critical ダウ グローバル テクノロジーズ エルエルシー
2012-07-19 Publication of JP2012136706A publication Critical patent/JP2012136706A/en
2016-12-07 Publication of JP6039906B2 publication Critical patent/JP6039906B2/en
The present invention relates to shear thinning ethylene / α-olefin (EAO) interpolymers. This interpolymer has a processing rheological ratio (PRR) of at least 4 and has been shown to have long chain branching (LCB). This interpolymer achieves such PRR without the usual LCB monomer such as norbornadiene (NBD). The alpha-olefin (α-olefin) suitably contains 3 to 20 carbon atoms (C 3 -C 20 ), preferably propylene (C 3 ), 1-butene, 1-hexene or 1-hexene. Octene (C 8 ). The interpolymer desirably comprises a diene (diolefin) monomer, preferably a non-conjugated diene monomer such as 5-ethylenediene-2-norbornene (ENB). EAO interpolymers containing this diene are commonly referred to as “EAODM interpolymers”. EAO and EAODM interpolymers are collectively referred to as “EAO (D) M interpolymers”. The present invention also relates to a method for producing such an interpolymer, a composition comprising such an interpolymer, and an article of manufacture comprising at least one part or portion formed from such an interpolymer or composition.
A first aspect of the invention is a shear thinning EAO (D) M interpolymer, wherein the interpolymer is polymerized ethylene, at least one α-olefin monomer, and optionally at least one diene monomer. And PRR is at least 4. The interpolymer has an ethylene (C 2 ) content of 20 to 95 weight percent (wt%), an α-olefin content of 80 to 5 wt%, the α-olefin is a C 3-20 α-olefin, optionally Desirably, the diene monomer content ranges from greater than 0 to 25 wt%, all percentages being based on the interpolymer weight and totaling 100 wt%. This EAO (D) M interpolymer achieves such a PRR without NBD or other conventional LCB monomers.
The interpolymer viscosity is typically 190 ° C. in the range of 0.1-100 radians per second (rad / sec) under a nitrogen atmosphere, typically using a dynamic mechanical spectrometer such as RMS-800 or ARES from Rheometrics under a nitrogen atmosphere. In poise (dyne-second / square centimeter (d-sec / cm 2 )). The viscosities at 0.1 rad / sec and 100 rad / sec can be expressed as V 0.1 and V 100 , respectively, the ratio of the two being referred to as RR and expressed as V 0.1 / V 100 . RRR = RR + [3.82-Interpolymer Mooney viscosity (ML 1 + 4 at 125 ° C.) × 0.3.
A second aspect of the present invention is a process for preparing the EAO (D) M interpolymer of the first aspect, wherein the process comprises ethylene under conditions sufficient to achieve at least 60 weight percent ethylene conversion. Contacting at least one α-olefin monomer and optionally at least one diene monomer with a catalyst and an activation catalyst, wherein the conditions include a temperature of at least 70 ° C., more preferably at least 80 ° C., and optionally In the presence of an effective amount of hydrogen, which is an amount sufficient to maintain the interpolymer PRR at least at 4 and the catalyst is at least one geometrically constrained It is a metal composite. A C 3-20 α-olefin monomer is suitable for the α-olefin monomer. This method is particularly useful for solution polymerization of EAO (D) M interpolymers in which the diene or polyene is a conjugated diene such as ENB, 1,4-hexadiene or similar non-conjugated diene or 1,3-pentadiene. This diene is preferably ENB or 7-methyl-1,6-octadiene. Similar to the first embodiment, this interpolymer PRR is realized without the usual LCB monomer.
A third aspect of the present invention is a polymer blend composition comprising the interpolymer of the first aspect and an amount of a crystalline polyolefin resin, desirably a propylene polymer or copolymer, preferably polypropylene (PP). The interpolymer is desirably present in an amount less than 50 parts by weight (pbw), and the crystalline polyolefin resin is desirably present in an amount greater than 50 pbw. When the interpolymer is an EAODM interpolymer, the polymer blend is referred to as a thermoplastic elastomer or TPE. When the interpolymer is an EAO interpolymer, the polymer blend is referred to as a thermoplastic polyolefin or TPO.
A fourth aspect of the present invention is a crystalline polyolefin that is desirably at least partially cross-linked (also referred to as cure or vulcanization) of the interpolymer of the first aspect and again a propylene polymer or copolymer, preferably PP. A polymer blend composition comprising a resin. The interpolymer is preferably present in an amount of 40 to 90 pbw, and the crystalline polyolefin resin is preferably present in an amount of 60 to 10 pbw. The interpolymer is preferably sufficiently crosslinked to have a gel content of at least 70% based on the weight of the interpolymer.
In both the third and fourth embodiments, the amount of interpolymer and crystalline polyolefin resin is based on the total weight of the interpolymer and the crystalline polymer, for a total of 100 pbw.
(Description of Preferred Embodiment)
In this specification, everything related to the Periodic Table of Elements is CRC Press, Inc. , 1989, with reference to the periodic table issued with copyright. Also, anything related to a family or family is a family or family that reflects in this periodic table of elements using families numbered in the IUPAC system.
Pure EAO (D) M interpolymers of the present invention have three different properties. The first is at least 4 PRRs. The PRR is desirably in the range of 4 to 350, preferably 4 to 250, and most preferably 8 to 150. Second, the Mooney viscosity or MV (ML 1 + 4 @ 125 ° C., ASTM D 1646-94) is in the range of 0.5 to 200, preferably 5 to 120, more preferably 10 to 85. Third, the molecular weight distribution (MWD or M w / M n ) is in the range of 2 to 5, preferably 2.0 to 3.8, and more preferably 2.2 to 3.2. Given these properties, preferred EAO (D) M interpolymers have an MWD of at least 2.5 and a PRR of at least 8. Preferred EAODM interpolymers have an MWD of at least 2.2, an MV of at least 15 and a PRR of at least 10. When EAO is C 2 / C 8 (EO) copolymers, MWD, at least 2.3, MV is at least 5, PRR is preferably above 4.
In the solution polymerization method, a known and dominant molecular weight control method is a chain termination reaction by thermal termination, hydrogen termination, or both. It is believed that thermal termination results in chain ends having reactive vinyl groups, while hydrogen termination results in non-reactive saturated end groups. In most cases, thermal shutdown competes with hydrogen shutdown. It is also believed that the formation of reactive vinyl end groups under the process conditions detailed above and their subsequent reinsertion into the increased polymer backbone results in a polymer product with LCB generated in situ. . Thus, combinations of reaction conditions that are advantageous for forming reactive vinyl end groups, such as little or no hydrogen and high polymerization temperatures, incorporate this reactive vinyl end group, and then It would be advantageous to cause an increase in LCB concentration as represented by an increase in PRR.
EAO of the present invention (D) M interpolymers, C 2 in at least one C 3 to 20 alpha-olefin (ethylene unsaturated) monomers and, optionally, C 4 to 40 diene monomer (other than NBD Or other conventional LCB monomer). The α-olefin can be either aliphatic or aromatic and is styrene, p-methylstyrene, cyclobutene, cyclopentene, and norbornene substituted at the 5 and 6 positions with C 1-20 hydrocarbyl groups. It is possible to include vinylic unsaturated or cyclic compounds such as norbornene containing. The α- olefin is preferably a C 3 to 20 aliphatic compound, more preferably C 3 to 16 aliphatic compound. Preferred ethylenically unsaturated monomers include 4-vinylcyclohexene, vinylcyclohexane, and C 3-10 aliphatic α-olefins (especially ethylene, propylene, isobutylene, 1-butene, 1-pentene, 1-hexene, 3-methyl -1-pentene, 4-methyl-1-pentene, 1-octene, 1-decene and 1-dodecene). More preferred C 3-10 aliphatic α-olefins are selected from the group consisting of propylene, 1-butene, 1-hexene and 1-octene.
The inventive interpolymers, 95 wt% of C 2 content of 20, 93 wt% and more preferably from 30, most preferably 90 wt% from 35. The interpolymers also contain at least one α-olefin other than C 2 80 wt% from 5, more preferably 70 wt% to 7, and most preferably from 10 at a concentration of 65 wt%. Finally, the interpolymer can contain non-conjugated dienes. When the interpolymer includes a non-conjugated diene, the non-conjugated diene content is preferably greater than 0 to 25 wt% or more, more preferably greater than 0 to 15 wt%, and most preferably greater than 0 to 10 wt%. All percentages are based on interpolymer weight. If desired, more than one diene, such as 1,4-hexadiene and ENB, can be incorporated simultaneously such that the total amount of diene incorporation is within the limits specified above.
The C4-40 diolefin or diene monomer is preferably a non-conjugated diolefin that is usually used as a polymerization site for crosslinking. The non-conjugated diolefin can be a C 6-15 straight chain, branched chain or cyclic hydrocarbon diene. Examples of non-conjugated dienes are linear acyclic dienes such as 1,4-hexadiene and 1,5-heptadiene, 5-methyl-1,4-hexadiene, 2-methyl-1,5-hexadiene, 6-methyl-1 , 5-heptadiene, 7-methyl-1,6-octadiene, 3,7-dimethyl-1,6-octadiene, 3,7-dimethyl-1,7-octadiene, 5,7-dimethyl-1,7-octadiene Monocyclic alicyclic dienes such as branched chain acyclic dienes such as 1,9-decadiene and dihydromyrcene isomer mixtures, 1,4-cyclohexadiene, 1,5-cyclooctadiene and 1,5-cyclododecadiene , Tetrahydroindene, methyltetrahydroindene, etc. Polycyclic alicyclic fused ring dienes and linking ring dienes, alkenyl, alkylidene, cycloal Nyl and 5-methylene-2-norbornene (MNB), ENB, 5-vinyl-2-norbornene, 5-propenyl-2-norbornene, 5-isopropylidene-2-norbornene, 5- (4-cyclopentenyl) -2 -Cycloalkylidene norbornene such as norbornene and 5-cyclohexylidene-2-norbornene. The diene is preferably ENB and a non-conjugated diene selected from the group consisting of 1,4-hexadiene and 7-methyl-1,6-octadiene, more preferably ENB. However, the diolefin is from the group consisting of 1,3-pentadiene, 1,3-butadiene, 2-methyl-1,3-butadiene, 4-methyl-1,3-pentadiene, or 1,3-cyclopentadiene. It can be a selected conjugated diene. The EAODM diene monomer content is within the limit range of non-conjugated dienes specified above, whether or not it contains conjugated dienes, non-conjugated dienes, or both.
Preferred interpolymers are generally substantially free of LCB-derived diene monomers, but are cost-acceptable and the desired interpolymer properties such as processability, tensile strength and elongation must be reduced to unacceptable levels. For example, such a monomer can be included. Such diene monomers include dicyclopentadiene, NBD, methylnorbornadiene, vinyl-norbornene, 1,6-octadiene, 1,7-octadiene, and 1,9-decadiene. When such a monomer is added, it is added in an amount in the range of more than 0 to 3 wt%, more preferably more than 0 to 2 wt%, based on the weight of the interpolymer.
The interpolymers of the present invention can be used to produce various articles or products or components or parts thereof. For purposes of illustration only and not for limitation, such articles may include wire and cable components, electrical insulators, belts, hoses, tubes, gaskets, membranes, molded articles, extruded parts, automotive parts, adhesives, tires. And a group consisting of tire sidewalls.
Although the interpolymer of the present invention can be used as it is, it is preferable to find use as a component of a compound. The compound is generally at least selected from the group consisting of fillers, fibers, plasticizers, oils, colorants, stabilizers, blowing agents, set retarders, set accelerators, crosslinkers and other conventional additives. Contains at least one polymer mixed with one additive. The interpolymers of the present invention preferably contain at least part of the polymer content of such compounds.
Interpolymers and compounds containing such interpolymers can be converted to final products by one of several conventional methods and equipment. Examples of methods include extrusion, calendering, injection molding, compression molding, spinning, and other common thermoplastic methods.
The interpolymers of the present invention also serve as the base polymer in making the graft polymer. Unsaturated organic compounds containing at least one ethylenic unsaturation (at least one double bond) and grafted to the interpolymers of the present invention can be used to modify such interpolymers. Exemplary unsaturated compounds include vinyl ethers, vinyl substituted heterocyclic compounds, vinyl oxazolines, vinyl amines, vinyl epoxides, unsaturated epoxy compounds, unsaturated carboxylic acids and anhydrides, ethers, amines, amides, succinimides or the like Acid esters are included. Representative compounds include maleic acid, fumaric acid, acrylic acid, methacrylic acid, itaconic acid, crotonic acid, α-methylcrotonic acid and cinnamic acid and their anhydrides, ester or ether derivatives, vinyl substituted alkylphenols and methacrylic acid. Glycidyl is included. Suitable unsaturated amines include aliphatic and heterocyclic containing at least one double bond and at least one amine group (at least one primary, secondary, or tertiary amine). Includes organic nitrogen compounds. Maleic anhydride is a preferred unsaturated organic compound. Grafted interpolymers can be used for several applications, only one is a component of an oily compound. The use of grafted EPDM interpolymers in oily compositions, and the methods used to prepare such graft interpolymers and various graft moieties are described in WO 97/32946 (US priority document, Mar. 8, 1996). No. 60/013052, and 60/024913, Aug. 30, 1996), the related teachings or corresponding US applications are incorporated herein by reference.
As mentioned in the third and fourth aspects, this interpolymer can be used for the production of TPE, TPO or TPV. There are several references for general operation of TPE production. One such reference is EP751182, published January 2, 1997, the related teachings of which are incorporated herein by reference.
The olefins that can be used in the production of the crystalline polyolefin resin include one or more of ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene, 2-methyl- 1-propene, 3-methyl-1-pentene, and 4-methyl-1-pentene are included. The crystalline polyolefin is preferably a PP homopolymer or copolymer of propylene having an α-olefin such as ethylene, 1-butene, 1-hexene, or 4-methyl-1-pentene, or a blend of a homopolymer and a copolymer. A preferred α-olefin is ethylene. The crystalline polyolefin can be prepared by an appropriate method such as random polymerization or block polymerization. Various forms such as isotactic and syndiotactic can also be used. Commonly available crystalline resins include PP homopolymers and propylene / ethylene (P / E) copolymer resins. Certain olefin copolymer resins, particularly propylene copolymers such as P / E copolymers, can be referred to as “semi-crystalline” resins. “Crystalline” as used to describe polyolefin resins has a broad enough meaning to include such semi-crystalline resins. These crystalline resins can be used alone or in combination.
Production of PP homopolymers and P / E copolymers also includes the use of Ziegler catalysts such as titanium trichloride in combination with aluminum diethylmonochloride, as described by Cecchin in USP 4177160. The polymerization process used to produce PP includes a slurry process conducted at about 50-90 ° C. and 0.5-1.5 MPa (5-15 atm), and special care to remove amorphous polymer These include both gas phase and liquid monomer methods that must be required. Ethylene can be added to the reaction to form polypropylene with the ethylene block. PP resins can also be prepared by using any of a variety of metallocenes, single site and constrained vaporization catalysts with associated methods.
Some patents and applications disclose geometrically constrained metal composites and methods for their production. Non-exhaustive examples include EP-A-416815 (US Patent Application No. 545403, filed July 3, 1990), EP-A-466651 (US Patent Application No. 547718, filed July 3, 1991). ), EP-A-514828 (US Patent Application No. 702475, filed May 20, 1991), EP-A-520732 (US Patent Application No. 87268, filed May 1, 1992) and WO 93/19104 ( US Patent Application No. 8003, filed January 21, 1993) and US-A-5055538, US-A-5057475, US-A-5096867, US-A-064802, US-A-5132380, US-A-. 5470993, US-A-5556928, US-A-5624878, WO95 / 00526, and US Provisional Application 60-005913 is included. US Patent Application No. 593756, filed Jan. 26, 1996, WO 95/14024, WO 98/27103 (based on US Provisional Application 60/034817, Dec. 19, 1996, 08/949505, Oct. 14, 1997) and PCT / US97 / 07252 (filed April 30, 1997) discloses various substituted indenyl-containing metal composites. All relevant teachings of the aforementioned patents and published or corresponding US patent applications are incorporated herein by reference.
In general, suitable metal complexes for use include additional polymerizing compounds, particularly metals from Groups 3-10 of the Periodic Table of Elements that can be activated to polymerize olefins with the activator of the present invention. A complex is included. Examples include expressions
In which M * is Ni (II) or Pd (II), X ′ is halo, hydrocarbyl or hydrocarbyloxy, Ar * is an aryl group, in particular 2 , 6-diisopropylphenyl or aniline group, CT-CT is 1,2-ethanediyl, 2,3-butanediyl, or the two T groups together form a 1,8-naphthanediyl group. A − is an anion component of the charge separation activator.
Similar complexes as described above are also described in J. Org. Am. Chem. Soc. 118, 267-268 (1996) and J. Am. Am. Chem. Soc. 117, 6414-6415 (1995). Brookhart, et al. And an active polymerization catalyst, particularly for the polymerization of α-olefins, alone or in combination with polar comonomers such as vinyl chloride, alkyl acrylates and alkyl methacrylates.
Additional complexes include group 3, 4 or lanthanide metals containing groups of 1 to 3 π-bonded anionic or neutral ligands, and cyclic or acyclic delocalized π-bonded anionic ligand groups It is possible that The term “π bond” means that the ligand group binds to the transition metal by sharing a partially delocalized π bond electron.
Each atom of the delocalized π bond group is independently hydrogen, halogen, hydrocarbyl, halohydrocarbyl, hydrocarbyloxy, hydrocarbyl sulfide, dihydrocarbylamino, and a hydrocarbyl-substituted metalloid release in which the metalloid is selected from group 14 of the periodic table The hydrocarbyl, halohydrocarbyl, hydrocarbyloxy, hydrocarbyl sulfide, dihydrocarbylamino, and hydrocarbyl substituted metalloid radicals can be further substituted with a radical selected from the group consisting of groups 15 or Substituted with a Group 16 heteroatom. The scope of the term “hydrocarbyl” includes C 1-20 linear, branched and cyclic alkyl radicals, C 6-20 aromatic radicals, C 7-20 alkyl substituted aromatic radicals, and C 7-20 allyl substitutions. Alkyl radicals are included. In addition, two or more such radicals can form together a fused ring system, including a partially or fully hydrogenated fused ring system, or can form a metallocycle with a metal. Is possible. Suitable hydrocarbyl substituted organic metalloid radicals include group 1, 2, and 3 substituted organic metalloid radicals of group 14 elements, each hydrocarbyl group containing from 1 to 20 carbon atoms. Examples of suitable hydrocarbyl substituted organic metalloid free radicals include trimethylsilyl, triethylsilyl, ethyldimethylsilyl, methyldiethylsilyl, triphenylgermyl, and trimethylgermyl groups. Examples of moieties containing a group 15 or 16 heteroatom include amine, phosphine, ether or thioether moieties or divalent derivatives thereof, such as transition metals or lanthanide metals, and amides linked to hydrocarbyl groups or hydrocarbyl substituted metalloid-containing groups, A phosphide, ether or thioether group is included.
Illustrative examples of such π-bonded anionic ligand groups include conjugated or non-conjugated, cyclic or acyclic dienyl groups, allyl groups, boratabenzene groups, and arene groups. Examples of suitable anionic delocalized π-bonding groups include cyclopentadienyl, indenyl, fluorenyl, tetrahydroindenyl, tetrahydrofluorenyl, octahydrofluorenyl, pentadienyl, cyclohexadienyl, dihydroanthracenyl , Hexahydroanthracenyl, decahydroanthracenyl group and s-indacenyl, and their C 1-10 hydrocarbyl substitution, C 1-10 hydrocarbyloxy substitution, di (C 1-10 hydrocarbyl) amino substitution, or tri ( C 1-10 hydrocarbyl) silyl substituted derivatives are included. Preferred anion delocalized π-bonding groups are cyclopentadienyl, pentamethylcyclopentadienyl, tetramethylcyclopentadienyl, tetramethylsilylcyclopentadienyl, indenyl, 2,3-dimethylindenyl, fluorenyl, 2-methylindenyl, 2-methyl-4-phenylindenyl, tetrahydrofluorenyl, octahydrofluorenyl, s-indacenyl, 2-methyl-s-indacenyl, and tetrahydroindenyl.
Bolatabenzene is an anionic ligand that is a benzene analog containing boron. These are already known in the art and are described in Herberich, et al. Organometallics, 1995, 14, 1, 471-480.
The first preferred geometrically constrained catalyst corresponds to Formula II:
Wherein M is titanium, zirconium or hafnium with a forming oxidation state of +2, +3 or +4 and A ′ is at least 2-position hydrocarbyl, fluoro-substituted hydrocarbyl, hydrocarbyloxy-substituted hydrocarbyl, dialkylamino-substituted hydrocarbyl, silyl, A substituted indenyl group substituted with a group selected from germyl and mixtures thereof, said group comprising up to 40 non-hydrogen atoms, wherein said A 'is further covalently bonded to M by a divalent Z group. Z is a divalent moiety bonded to A 'and M by a sigma bond, said Z containing boron or a member of group 14 of the periodic table, and containing nitrogen, phosphorus, sulfur or oxygen, X Is an anion or dianion of up to 60 atoms other than a ligand species that is a cyclic delocalized π-bonded ligand group A ligand group, X ′ is a neutral Lewis base coordination compound having up to 20 atoms each independently for each occurrence, p is 0, 1 or 2 and is 2 above the formal oxidation state of M. Less, but when X is a dianionic ligand group, p is 1 and q is 0, 1 or 2.
Additional preferred catalysts or coordination complexes are disclosed in previously incorporated WO 98/27103 and PCT / US97 / 07252. PCT / US97 / 07252, in particular page 4, line 34 to page 16, line 36, discloses preferred coordination complexes such as those regenerated as in the following formulas III, IVA and IVB. Formula I below is a variant of Formula II on page 7 of PCT / US97 / 07252.
The catalyst preferably comprises a metal coordination complex corresponding to Formula I,
Wherein M is defined as in Formula II above, and R ′ and R ″ are each independently hydride, hydrocarbyl, silyl, germyl, halide, hydrocarbyloxy, hydrocarbylsiloxy, hydrocarbylsilylamino, Di (hydrocarbyl) amino, hydrocarbyleneamino, di (hydrocarbyl) phosphino, hydrocarbylene-phosphino, hydrocarbyl sulfide, halo-substituted hydrocarbyl, hydrocarbyloxy-substituted hydrocarbyl, silyl-substituted hydrocarbyl, hydrocarbylsiloxy-substituted hydrocarbyl, hydrocarbylsilylamino-substituted hydrocarbyl , Di (hydrocarbyl) amino substituted hydrocarbyl, hydrocarbylene amino substituted hydrocarbyl, di (hydrocarbyl) phosphino substituted hydrocarbyl , Hydrocarbylene-phosphino substituted hydrocarbyl, or hydrocarbyl sulfide substituted hydrocarbyl, wherein the R ′ or R ″ group has up to 40 non-hydrogen atoms, and optionally two or more of the groups together are divalent R ′ ″ is a divalent hydrocarbylene or substituted hydrocarbylene group that forms a fusion system with the rest of the metal complex, wherein R ″ ″ is 1 to 30 Wherein Z is a divalent moiety or a moiety containing one σ bond and two neutral electron pairs capable of forming a coordination-covalent bond at M, wherein Z is boron Or a monovalent having up to 60 atoms other than the type of ligand that contains a member of group 14 of the periodic table and also contains nitrogen, phosphorus, sulfur or oxygen, wherein X is a cyclic delocalized binding ligand group shadow An ionic ligand group, X ′ is a neutral coordination compound having up to 20 atoms independently for each occurrence, and X ″ is a divalent anionic ligand group having up to 60 atoms. , P is 0, 1, 2 or 3, q is 0, 1 or 2, and r is 0 or 1.
Said complexes are optionally in pure form as isolated crystals or as a mixture with other complexes, optionally in solvents, in particular in the form of solvent adducts in organic liquids, as well as their dimers The body or chelating agent can exist in the form of a chelating derivative that is an organic substance such as ethylenediaminetetraacetic acid (EDTA).
In the metal complexes defined by formulas I and II, preferred X ′ groups are carbon monoxide, phosphine, especially trimethylphosphine, triethylphosphine, triphenylphosphine and bis (1,2-dimethylphosphino) ethane, R is C P (OR) 3 which is 1-20 hydrocarbyl, ethers, especially tetrahydrofuran, amines, especially pyridine, bipyridine, tetramethylethylenediamine (TMEDA), and triethylamine, olefins, and neutral conjugated C 4-40 dienes . Such a complex containing a neutral diene X ′ group is one in which the metal is in the +2 formal oxidation state.
The catalyst preferably includes a coordination complex corresponding to Formula III.
In which R 1 and R 2 are independently selected from hydrogen, hydrocarbyl, perfluorinated hydrocarbyl, silyl, germyl and mixtures thereof, wherein the group contains up to 20 non-hydrogen atoms, Provided that at least one of R 1 or R 2 is not hydrogen and R 3 , R 4 , R 5 , and R 6 are independently selected from hydrogen, hydrocarbyl, perfluorinated hydrocarbyl, silyl, germyl and mixtures thereof Wherein the group contains up to 20 non-hydrogen atoms, M is titanium, zirconium or hafnium, Z contains boron or a member of group 14 of the periodic table, nitrogen, phosphorus, sulfur or A divalent moiety also containing oxygen, said part containing up to 60 non-hydrogen atoms, p is 0, 1 or 2 and q is 0 or 1 Where when p is 2, q is 0, M is in the +4 formal oxidation state, X is a halide, hydrocarbyl, hydrocarbyloxy, di (hydrocarbyl) amide, di (hydrocarbyl) phosphide, hydrocarbyl sulfide, and silyl group, And an anionic ligand selected from their halo, di (hydrocarbyl) amino, hydrocarbyloxy, and di (hydrocarbyl) phosphino substituted derivatives, wherein X has up to 20 non-hydrogen atoms and p is 1. Where q is 0, M is in the +3 formal oxidation state, and X is a group consisting of allyl, 2- (N, N-dimethylamino-methyl) phenyl, and 2- (N, N-dimethyl) -aminobenzyl. Or M is in the +4 formal oxidation state and X is a conjugated dithiol group selected from A divalent derivative of ene, M and X together form a metallocyclopentene group, when p is 0, q is 1, M is in the +2 formal oxidation state, and X ′ is a neutral conjugate or A non-conjugated diene, optionally substituted with one or more hydrocarbyl groups, wherein said X ′ has up to 40 carbon atoms and forms a π complex with M.
The most preferred coordination complex, (t-butylamido) -dimethyl (η 5 -2-methyl-s-indasen-1-yl) silanetitanium (II) 1,3-pentadiene is referred to as a geometric isomer There are also two isomers, formulas IVA and IVB.
Specific examples of coordination complexes are described in detail in PCT / US97 / 07252, page 10, line 3 to page 16, line 36 already incorporated by reference. This coordination complex is composed of (t-butylamido) dimethyl (η 5 -2-methyl-s-indasen-1-yl) silanetitanium (II) 2,4-hexadiene, (t-butylamido) -dimethyl (η 5 -2-methyl-s-indasen-1-yl) silanetitanium (IV) dimethyl, (t-butylamido) -dimethyl (η 5 -2,3-dimethylindenyl) silanetitanium (II) 1,4-diphenyl- 1,3-butadiene, (t-butyl-amido) -dimethyl (η 5 -2,3-dimethyl-s-indasen-1-yl) silane titanium (IV) dimethyl, and (t-butylamido) -dimethyl (η 5-methyl -s- indacene-1-yl) silane titanium (II) 1,3 is preferably selected from the group consisting of pentadiene. Preferred members of this group include (t-butylamido) -dimethyl (η 5 -2methyl-s-indasen-1-yl) silane-titanium (IV) dimethyl, (t-butylamido) dimethyl (η 5 -2 -Methylindenyl) -silane titanium (II) 2,4-hexadiene and (t-butylamido) -dimethyl (η 5 -2-methyl-s-indasen-1-yl) silane titanium (II) 1,3-pentadiene Is included. The most preferred coordination complex is (t-Butylamido) -dimethyl (η 5 -2-methyl-s-indasen-1-yl) silane titanium (II) 1,3-pentadiene.
Other preferred metal complexes include derivatives of transition metals containing lanthanides, but preferred are group 3, 4 or lanthanide metals that are in the +2, +3, or +4 formal oxidation state to meet the needs already described. Preferred compounds include metal complexes (metallocenes) containing 1 to 3π-bonded anionic ligand groups, which can be cyclic or non-cyclic non-localized π-bonded anionic ligand groups. Illustrative examples of such π-bonded anionic ligand groups include conjugated or non-conjugated, cyclic or acyclic dienyl groups, allyl groups, and arene groups. Such other preferred metal complexes correspond to the formula L 1 MX m X ′ n X ″ p ′s or dimers thereof, where L is an anion delocalized π bound to M A linking group containing up to 50 atoms, not counting hydrogen, and optionally two L groups can be joined together by one or more substituents, thereby forming a cross-linked structure In addition, optionally, one L can be bonded to X by one or more L substituents, and M is a Group 4 metal in the periodic table of elements in a formal oxidation state of +2, +3, or +4. X is optionally a divalent substituent of up to 50 non-hydrogen atoms, forms a metallocycle with M together with L, and X ′ is neutral with optionally up to 20 non-hydrogen atoms A Lewis base, X ″ is a monovalent with up to 40 non-hydrogen atoms per occurrence An ionic moiety, optionally two X ″ groups bonded together to form a divalent dianionic moiety with both valences bound to M or π-bonded to M (above , M is the +2 oxidation state), can form a neutral conjugated or non-conjugated diene, or optionally, one or more X ″ and one or more X ′ groups together It is possible to bond and thereby both covalently bond to M and form a moiety coordinated to them by the Lewis base function, l is 1 or 2, m is 0 or 1, and n is Is a number from 0 to 3, p is an integer from 0 to 3, and the sum of l + m + p is equal to the formal oxidation state of M. Such complex variants have X ″ containing up to 20 non-hydrogen atoms per occurrence, and the two X ″ groups together have m = 1 and p is 1 or 2. Forms a neutral C5-30 conjugated diene.
Preferred divalent X substituents include up to 30 atoms, not counting hydrogen, oxygen, sulfur, boron, or a member of Group 14 of the Periodic Table of Elements directly attached to a delocalized π bond group. Included are groups containing at least one atom and different atoms selected from the group consisting of nitrogen, phosphorus, oxygen or sulfur covalently bonded to M.
Such other preferred complexes include those containing one or two L groups. The latter complex includes those containing a bridging group in which two L groups are bonded. Preferred bridging groups are those corresponding to the formula (ER * 2 ) x, where E is silicon or carbon, R * is independently hydrogen or silyl, hydrocarbyl, hydrocarbyloxy and combinations thereof at each occurrence Wherein R * has up to 30 carbon or silicon atoms and x is 1-8. Preferably, R * is independently methyl, benzyl, tert-butyl or phenyl for each occurrence.
Illustrative examples of said bis (L) comprising complexes are compounds corresponding to formulas V and VI;
Where M is titanium, zirconium or hafnium with a forming oxidation state of +2 or +4, and R 3 is independently hydrogen, hydrocarbyl, dihydrocarbylamino, hydrocarbyleneamino, silyl, germyl, Selected from the group consisting of cyano, halo and combinations thereof, wherein said R 3 has up to 20 atoms without counting hydrogen, or adjacent R 3 groups together form a divalent derivative; To form an anionic ligand group of up to 40 atoms without independently counting hydrogen for each occurrence of X ″, or two X ″ groups together with hydrogen A conjugated diene having from 4 to 30 atoms not forming a divalent anionic ligand group of up to 40 atoms or counting together, not counting hydrogen, together with M To form a complex and, moreover M is +2 formal oxidation state, R *, E and x are as previously defined.
The above-mentioned metal complex is particularly suitable for the production of a polymer having a stereoregular molecular structure. In such a capacity, or the complex has a C 2 symmetry or chiral, it is preferable to have a three-dimensional rigid structure. An example of the first type is a compound having different delocalized π bond systems such as one cyclopentadienyl group and one fluorenyl group. Similar systems based on Ti (IV) or Zr (IV) are described in Ewen, et al. J. et al. Am. Chem. Soc. 110, 6255-6256 (1980), disclosed for the production of syndiotactic olefin polymers. Examples of chiral structures include bis-indenyl complexes. Similar systems based on Ti (IV) or Zr (IV) are described in Wild et al. J. et al. Organomet. Chem, 232, 233-47, (1982) for the production of isotactic olefin polymers.
Examples of bridging ligands containing two π-bonding groups are (dimethylsilyl-bis-cyclopentadienyl), (dimethylsilyl-bis-methylcyclopentadienyl), (dimethylsilyl-bis-ethylcyclopentadienyl). , (Dimethylsilyl-bis-t-butylcyclopentadienyl), (dimethylsilyl-bis-tetramethylcyclopentadienyl), (dimethylsilyl-bis-indenyl), (dimethylsilyl-bis-tetrahydroindenyl), (Dimethylsilyl-bis-fluorenyl), (dimethylsilyl-bis-tetrahydrofluorenyl), (dimethylsilyl-bis-2-methyl-4-phenylindenyl), (dimethylsilyl-bis-2-methylindenyl) , (Dimethylsilyl-cyclopentadienyl-fluorenyl), (1, , 2,2-tetramethyl-1,2-disilyl-bis-cyclopentadienyl), (1,2-bis (cyclopentadienyl) ethane, and (isopropylidene-cyclopentadienyl-fluorenyl). .
Preferred X ″ groups are selected from hydrido, hydrocarbyl, silyl, germyl, halohydrocarbyl, halosilyl, silylhydrocarbyl and aminohydrocarbyl groups, wherein the two X ″ groups together form a divalent derivative of a conjugated diene? Or together, form a neutral, π-bonded conjugated diene.
Preferred geometrically constrained metal composites are also Group 4 metals corresponding to the following formula VII that can be found in previously incorporated US-A-5470993, US-A-5556928 and US-A-5624878: It is a coordination complex. For example, see US Pat. No. 5,624,878, column 1, line 61 to column 3, line 42 and column 6, line 14 to line 7, column 7.
Where M is titanium, zirconium with a forming oxidation state of +2 or +4, and R 3 is independently for each occurrence from the group consisting of hydrogen, hydrocarbyl, silyl, germyl, cyano, halo, and combinations thereof. Selected, said R 3 has up to 20 atoms without counting hydrogen, or adjacent R 3 groups together form a divalent derivative (ie, hydrocarbadiyl, siladiyl, or germanadyl group) Thereby forming a fused ring system, wherein each X ″ is a halo, hydrocarbyl, hydrocarbyloxy or silyl group, said group having up to 20 atoms without counting hydrogen, or 2 C 5 to 30 conjugated dienes to form, Y is -O together X '' is a -, - S -, - NR * -, - PR * - a and, Z is SiR * 2, CR * 2, SiR 2 SiR * 2, CR * 2 CR * 2, CR * = CR *, CR * 2 SiR * 2, or a GeR * 2, R * is as previously defined.
The aforementioned delocalized π-bonding groups, metal complexes containing them, and catalyst compositions based thereon are disclosed in the following publications, USP 5703187, 5064802, 5321106, 5374696, 5470993, 5624878, 5556928, 5466632, 5541349, 5495036, 5527929, US Pat. No. 5,616,664, WO 97/15583, WO 97/35864, WO 98/06727, and WO 98/27103, their teachings or corresponding and equivalent US patent applications are hereby incorporated by reference. .
Examples of Group 4 metal composites are found in US-A-5624878 at column 9, line 9 to column 13, line 59. Some of these complexes include: (Tert-Butylamide)-(tetramethyl-η 5 -cyclopentadienyl) dimethylsilanetitanium dichloride, (tert-butyramide) (tetramethyl-η 5 -cyclopentadienyl) dimethylsilanetitanium dimethyl, tert-butyramide) Tetramethyl-η 5 -cyclopentadienyl) -1,2-ethanediyltitanium dimethyl, (tert-butylamide) (hexamethyl-η 5 -indenyl) dimethylsilanetitanium dimethyl, (tert-butylamide) (tetramethyl-η 5 - cyclopentadienyl) dimethylsilane titanium (III) 2-(dimethylamino) benzyl, (tert-butylamido) (tetramethyl-eta 5 - cyclopentadienyl) - dimethylsilane titanium (III) ants , (Tert-butylamido) (tetramethyl-eta 5 - cyclopentadienyl) - dimethyl - silane titanium (II) 1,4-diphenyl-1,3-butadiene, (tert-butylamido) (2-methylindenyl) Dimethyl-silane titanium (II) 1,4-diphenyl-1,3-butadiene, (tert-butylamide) (2-methylindenyl) dimethyl-silane titanium (IV) 1,3-butanediene, (tert-butylamide) ( 2,3-dimethylindenyl) dimethylsilanetitanium (II) 1,4-diphenyl-1,3-butadiene, (tert-butylamide) (2,3-dimethylindenyl) dimethylsilanetitanium (IV) 1,3- Butadiene, (tert-Butylamide) (2,3-Dimethylindene ) -Dimethylsilane Titanium (II) 1,3-pentadiene, (tert-Butylamide) (2-Methylindenyl) dimethylsilane Titanium (II) 1,3-pentadiene, (tert-Butylamide) (2-Dimethylindenyl) ) Dimethylsilanetitanium (IV) dimethyl, (tert-butylamide) (2-methyl-4-phenylindenyl) -dimethylsilanetitanium (II) 1,4-diphenyl-1,3-butadiene, (tert-butylamide) ( 2-methyl-4-phenylindenyl) -dimethylsilanetitanium (II) 1,3-pentadiene, (tert-butyramide) (tetramethyl-η 5 -cyclopentadienyl) -dimethylsilanetitanium (IV) 1,3 -Butadiene, (tert-Butylamide (Tetramethyl- eta 5 - cyclopentadienyl) - dimethylsilane titanium (II) 1,4-dibenzyl-1,3-butadiene, (tert-butylamido) - (tetramethyl-eta 5 - cyclopentadienyl) dimethyl Silane titanium (II) 2,4-hexadiene, (tert-butylamide) (tetramethyl-η 5 -cyclopentadienyl) -dimethylsilane titanium (II) 3-methyl-1,3-pentadiene, (tert-butylamide) ) (2,4-dimethyl-1,3-pentadien-2-yl) dimethylsilanetitanium dimethyl, (tert-butylamide) (1,1-dimethyl-2,3,4,9,10-η-1,4 , 5,6,7,8-hexahydronaphthalen-4-yl) dimethyl-silane titanium dimethyl, ( tert-Butylamide) (1,1,2,3-tetramethyl-2,3,4,9,10-η-1,4,5,6,7,8-hexahydronaphthalen-4-yl) dimethylsilane Titanium dimethyl, (tert-butylamide) (tetramethyl-cyclopentadienyl) -dimethylsilane titanium 1,3-pentadiene, (tert-butylamide) (3- (N-pyrrolidinyl) inden-1-yl) dimethylsilane titanium 1 , 3-pentadiene, (tert-butylamido) (2-methyl-s-indacene-1-yl) dimethylsilanetitanium 1,3-pentadiene, (tert-butylamido) (2-methyl-s-indacene-1-yl) Dimethylsilane titanium 1,4-diphenyl-1,3-butadiene, and (tert-butyl) Ruamido) (3,4-cyclopenta (l) phenanthren-2-yl) dimethylsilane - Titanium 1,4-diphenyl-1,3-butadiene. Group 4 metal complexes (tert- butylamido) - (tetramethyl-eta 5 - cyclopentadienyl) - dimethylsilane titanium eta 4-3-methyl-1,3-pentadiene and C 5 Me 4 SiMe 2 NtBu) Ti It is preferably selected from (η 4 -1,3-pentadiene).
Bis (L) -containing complexes including cross-linked complexes suitable for use in the present invention include biscyclopentadienyl zirconium dimethyl, biscyclopentadienyl-titanium diethyl, biscyclopentadienyl titanium diisopropyl, bis Cyclopentadienyl titanium-diphenyl, biscyclopentadienyl zirconium dibenzyl, biscyclopentadienyl titanium-2,4-pentadienyl, biscyclopentadienyl-titanium methyl methoxide, biscyclopentadienyl titanium methyl chloride, Bispentamethylcyclopentadienyltitanium dimethyl, bisindenyltitanium-dimethyl, indenylfluorenyltitaniumdimethyl, bisindenyltitaniummethyl (2- (dimethylamino) -benzyl Bisindenyltitanium methyltrimethylsilyl, bistetrahydroindenyl-titaniummethyltrimethylsilyl, bispentamethylcyclopentadienyltitanium diisopropyl, bispentamethylcyclopentadienyltitanium dibenzyl, bispentamethylcyclopentadienyl-titaniummethylmethoxide , Bispentamethylcyclopentadienyl titanium methyl chloride, (dimethylsilyl-bis-cyclopentadienyl) zirconium dimethyl, (dimethylsilyl-bis-pentamethyl-cyclopentadienyl) titanium-2,4-pentadienyl, (dimethylsilyl) -Bis-t-butylcyclopentadienyl) -zirconium dichloride, (methylene-bis-pentamethylcyclopentadienyl) titani (III) 2- (dimethylamino) benzyl, (dimethylsilyl-bis-indenyl) zirconium chloride, (dimethylsilyl-bis-2-methylindenyl) zirconium dimethyl, (dimethylsilyl-bis-2-methyl-4-) Phenylindenyl) -zirconium dimethyl, (dimethylsilyl-bis-2-methylindenyl) -zirconium-1,4-diphenyl-1,3-butadiene, (dimethylsilyl-bis-2-methyl-4-phenylynedenyl) zirconium (II) 1,4-diphenyl-1,3-butadiene, (dimethylsilyl-bis-tetrahydroindenyl) zirconium (II) 1,4-diphenyl-1,3-butadiene, (dimethylsilyl-bis-fluorenyl) zirconium Dichloride, (dimethylsilyl-bis -Tetrahydrofluorenyl) -zirconium-di (trimethylsilyl), (isopropylidene) (cyclopentadienyl) (fluorenyl) -zirconium dibenzyl, and (dimethylsilylpentamethylcyclopentadienylfluorenyl) -zirconium dimethyl included.
The metal composite can be prepared by using well-known synthetic techniques. Optionally, a reducing agent can be used to produce a low oxidation state complex. Such methods are described in U.S. Patent No. 8/241523, filed May 13, 1994, published as WO 95-00526, the teachings of which are incorporated herein by reference, and WO 98/27103 and PCT / US97 / 07252. (Already incorporated by reference). This synthesis is carried out in a suitable non-hindered solvent at a temperature of −100 to 300 ° C., preferably at −78 to 100 ° C., most preferably 0 to 50 ° C. As used herein, the term “reducing agent” refers to a metal or compound that reduces metal M from a high oxidation state to a low oxidation state under reducing conditions. Illustrative examples of suitable metal reducing agents are alkali metals or alkaline earth metal alloys such as alkali metals, alkaline earth metals, aluminum and zinc, sodium / mercury amalgam and sodium / potassium alloys. Examples of suitable reducing agent compounds include Group 1 or Group 2 metal hydrocarbyl compounds and Grignards having 1 to 20 carbons in each hydrocarbyl group such as sodium naphthalenide, potassium graphite, alkyllithium, alkadienyllithium or potassium. It is a reagent. The most preferred reducing agents are alkali metals or alkaline earth metals, especially lithium and magnesium metals.
Suitable reaction liquids for complex formation include branched chain hydrocarbons such as aliphatic and aromatic hydrocarbons, ethers, and cyclic ethers, especially isobutane, butane, pentane, hexane, heptane, octane, and mixtures thereof, Cyclic and cycloaliphatic hydrocarbons such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof, aromatic and hydrocarbyl substituted aromatic compounds such as benzene, toluene, and xylene, C 1-4 dialkyl ethers, ( C1-4 dialkyl ether derivatives of poly) alkylene glycols and tetrahydrofuran are included. Mixtures of the above are also suitable.
A catalyst complex, a mixture of coordination complexes, or both can be used in the process aspects of the present invention. For example, the coordination complex described in WO 98/27103 and PCT / US97 / 07252 can be used in combination with a catalyst complex such as described in USP5470993. Similarly, combinations of two or more coordination complexes disclosed in WO 98/27103 and PCT / US97 / 07252, or two or more catalyst complexes disclosed in USP 5470993 also provide acceptable results. Bring.
The aforementioned catalyst composite is illustrative and not limiting. A catalyst that promotes vinyl end group termination upon polymerization conditions and subsequent reinsertion into the polymer chain is considered to be sufficient as long as the resulting polymer has a PRR of at least 4.
The complex, whether a catalyst complex, a coordination complex, or both, is catalytically activated by combining with an activated catalyst or by using an activation method. Activation catalysts suitable for use herein include poly or oligoalumoxanes, particularly methylalumoxane, triisobutylaluminum modified methylalumoxane, or isobutylalumoxane, C1-30 hydrocarbyl substituted group 13 compounds and the like Lewis acids, especially tri (hydrocarbyl) aluminum compounds or tri (hydrocarbyl) boron compounds and their (including perhalogenated) halogenated derivatives having 1 to 10 carbon atoms in each hydrocarbyl or halogenated hydrocarbyl group, Particularly included are perfluorinated tri (aryl) boron compounds, and most particularly tris (pentafluorophenyl) borane (hereinafter “FAB”).
Alternatively, the complex may be replaced with non-polymerized compatible non-coordinating ion forming compounds (including the use of such compounds under oxidizing conditions), particularly ammonium salts, phosphonium salts, oxonium salts, carbonium of compatible non-coordinating anions It is made catalytically active by combining it with a ferrocenium salt of a salt, a silylium salt or a sulfonium salt or a compatible non-coordinating anion, and activated cocatalysts and techniques described above. Said activation cocatalyst and activation technique have been previously described in the following references: EP-A-277003, US-A-5153157, US-A-5064802, EP-A-468651 (US Patent Application No. 07/547718). ), EP-A-520732 (equivalent to US patent application 07/87268), and EP-A-520732 (equivalent to US patent application 07/884966, filed May 1, 1992). The teachings are directed to composites, the teachings of which are incorporated herein by reference.
In combination with neutral Lewis acids, in particular trialkylaluminum compounds having 1 to 4 carbon atoms in each alkyl group and tri (hydrocarbyl) boron halide compounds having 1 to 20 carbon atoms in each hydrocarbyl group, in particular Combinations of FABs, as well as combinations of such neutral Lewis acid mixtures and poly or oligoalumoxanes, single neutral Lewis acids, especially combinations of FAB and poly or oligoalumoxanes, are particularly desirable activated cocatalysts. It is. The preferred molar ratio of Group 4 metal complex: FAB: alumoxane is 1: 1: 1 to 1: 5: 20, more preferably 1: 1: 1.5 to 1: 5: 10. The use of low concentrations of alumoxane in the process of the present invention allows for the production of EAODM polymers with high catalytic effects even if less expensive alumoxane cocatalyst is used. Furthermore, a polymer with a clearly low concentration of aluminum residues is thus obtained.
Further suitable ion forming, activating cocatalysts include compounds that are salts of silylium ions and non-coordinated, compatible anions of the formula R 3 Si (X ′) q + A − where R Is as defined above for C 1-10 hydrocarbyl and X ′, q and A − .
Preferred silylium salt-activated cocatalysts are trimethylsilylium tetrakispentafluoro-phenylborate, triethylsilylium tetrakispentafluorophenylborate and their ether-substituted additives. Silylium salts are already commonly used in J. Org. Chem. Soc. Chem. Comm. 1993, 383-384, and Lambert, J. et al. B. Et al. , Organometallics, 1994, 13, 2430-2443. The use of the silylium salt as an activation catalyst for additional polymerization catalysts was described on March 21, 1996 in US Patent Application No. 304314, published September 12, 1994, the equivalent of which was published as WO 96/08519. The teachings of which are incorporated herein by reference.
Certain complexes of alcohol, mercaptans, silanols, and FAB oximes are also effective catalyst activators and can be used according to the present invention. Such catalysts are disclosed in US Pat. No. 5,296,433, the teachings of which are incorporated herein by reference.
Mass electrolysis techniques include electrochemical oxidation of metal complexes under electrolysis conditions in the presence of a supporting electrolyte containing non-coordinating inert anions. This technique is more fully described in column US Pat. No. 5,624,878, column 15, line 47 to column 16, line 48.
The molar ratio of catalyst / cocatalyst used is preferably in the range of 1: 10000 to 100: 1, more preferably 1: 5000 to 10: 1, most preferably 1: 1000 to 1: 1. Alumoxane is used in large quantities when used alone as an activating cocatalyst, generally at least 100 times the amount of metal complex (calculated in moles of aluminum (Al)) based on moles. FAB, when used as an activated cocatalyst, has a molar ratio to metal complex of 0.5: 1 to 10: 1, more preferably 1: 1 to 6: 1, most preferably 1: 1 to 5 : 1 The remaining activated cocatalyst is generally used in approximately equimolar amounts with the amount of metal complex.
In general, the polymerization is carried out under conditions well known in the art for polymerization reactions of the Ziegler-Natta or Kaminsky-Sinn type, ie a temperature of 0 to 250 ° C., preferably 30 to 200 ° C. and a pressure of atmospheric pressure. To 10,000 atm. For example, Kaminsky, J., et al., Reporting the use of a soluble bis (cyclopentadienyl) zirconium dimethyl-alumoxane catalyst system for solution polymerization of EP and EAODM elastomers. Poly. Sci. Vol. 23, pp. 2151-64 (1985). USP 5229478 discloses a slurry polymerization process using bis (cyclopentadienyl) zirconium based on a similar catalyst system.
Suspension, solution, slurry, gas phase, solid state powder polymerization or other process conditions can be used if desired. Supports, particularly silica, alumina, or polymers (especially poly (tetrafluoroethylene) or polyolefins) can be used and are desirably used when the catalyst is used in a gas phase polymerization process. The support has a (metal based) catalyst: support weight ratio of 1: 100,000 to 1:10, more preferably 1: 50000 to 1:20, most preferably 1: 10000 to 1:30. It is preferred to use the amount provided. In most polymerization reactions, the molar ratio of catalyst: polymerizable compound used is from 10-12 : 1 to 10-1 : 1, more preferably from 10-9 : 1 to 10-5 : 1. The methods used to prepare the EAODM interpolymers of the present invention are solution methods or slurry methods, both of which are already known in the art.
An inert liquid is a solvent suitable for polymerization. Examples include cyclic and fatty acids such as straight and branched chain hydrocarbons such as isobutane, butane, pentane, hexane, heptane, octane, and mixtures thereof, cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof. Included are cyclic hydrocarbons, perfluorinated hydrocarbons such as perfluorinated C 4-10 alkanes, and aromatic and alkyl substituted aromatic compounds such as benzene, toluene, xylene, and ethylbenzene. Suitable solvents also include butadiene, cyclopentene, 1-hexene, 1-hexane, 4-vinylcyclohexene, vinylcyclohexane, 3-methyl-1-pentene, 4-methyl-1-pentene, 1,4-hexadiene, 1 -Liquid olefins that can act as monomers or comonomers, including octene, 1-decene, styrene, divinylbenzene, allylbenzene, and vinyltoluene (including single or mixed isomers). If desired, normal gaseous olefins can be converted to liquids by applying the pressures used herein.
The catalyst is combined with at least one additional homogeneous or heterogeneous polymerization catalyst in separate reactors connected in series or in parallel to prepare a polymer blend having the desired properties. It is possible to use. Examples of such methods are disclosed in WO94 / 00500 equivalent to US patent application No. 07/904770, and in US patent application No. 08/10958, filed January 29, 1993, the teachings of which are Incorporated herein by reference.
By using the aforementioned catalyst, catalyst complex and coordination complex in combination with a cocatalyst in the method of one aspect of the present invention, the interpolymer of another aspect of the present invention is readily prepared. The resulting EAO (D) M interpolymer exhibits a PRR of at least 4 without incorporating NBR or other normal LCB monomers. This interpolymer has a linear polymer backbone and improved polymer processability (higher throughput can be included), higher melt strength, higher green strength, lower than interpolymer without LCB Shows pigment odor, resistance to melt breakage, and filler extensibility.
The catalyst used in the process of the invention is particularly advantageous for the production of interpolymers having a PRR of at least 4. The use of catalysts in continuous polymerization processes, especially continuous solution polymerization processes, allows for long chain branching, taking into account the high reaction temperatures favoring the formation of vinyl-terminated polymer chains that can be incorporated into increasing polymers. Get. It is believed that a unique combination of high reaction temperature, high ethylene conversion, and substantially no or very low concentration of molecular hydrogen produces the desired interpolymer of the first aspect of the invention. As used herein, “very low concentration” means a concentration that is greater than 0 but less than or equal to 0.1 mole percent with respect to the sum of fresh ethylene feed content and fresh hydrogen feed content.
In general terms, it is desirable to produce an EAODM elastomer under conditions that increase the reactivity of the diene monomer component. The reason for this is explained in the '487 patent identified above in the following manner and remains unchanged despite progress achieved in such literature. A major factor affecting production costs, and therefore EAODM applications, is the cost of the diene monomer. This diene is a more expensive monomer material than C 2 or C 3 . Furthermore, the reactivity of diene monomers with the already known metallocene catalysts is lower than C 2 and C 3 . Thus, in order to achieve the degree of diene incorporation required to produce EAODM with an acceptable fast cure rate, the diene that is desired to be incorporated into the final EAODM product, expressed as a percentage of the total concentration of monomer present. It was necessary to use a substantially excess diene monomer concentration compared to the percentage of. Manufacturing costs are further increased because substantial amounts of non-reactive diene monomers must be recovered from the polymerization reaction vessel recycle effluent.
Furthermore, in addition to EAODM manufacturing costs, exposure of olefin polymerization catalysts to diene, particularly the high concentration of diene monomer required to provide the required concentration of diene incorporation into the final EAODM, often results in the ethylene and polyethylene monomers processed by the catalyst. There is the fact that it reduces the rate or activity that causes polymerization. Correspondingly, lower throughput and longer reaction times were required compared to the production of ethylene-propylene copolymer elastomers or other α-olefin copolymer elastomers.
The EAO (D) M polymer of the present invention can also be used as described above, gas phase polymerization, reactor cooling is generally used to prepare EAO (D) M polymer, recycle gas, inert liquid or monomer. Or any other well-known process that occurs by distillative cooling of any volatiles such as dienes. Suitable inert liquids are C 3-8 , preferably C 4-6 , saturated hydrocarbon monomers. Volatiles or liquids are distilled off in a hot fluidized bed to form a gas that mixes with the fluidized gas. Such methods are described, for example, in EP 89691, US-A-4543399, WO 94/25495, WO 94/28032, and US-A-532749, the teachings of which are incorporated herein by reference. US-A-4588790, US-A-4543399, US-A-5352799, US-A-5436304, US-A-5405922, US-A-5462999, US, although other related teachings are also incorporated by reference. -A-5461123, US-A-5453471, US-A-5032562, US-A-5028670, US-A-5473028, US-A-5510804, US-A-5541270, EP-A-659773, EP-A -692500, and PCT applications WO94 / 29032, WO94 / 25497, WO94 / 25495, WO94 / 28032, WO95 / 13305, WO94 / 26793 and WO95 / 07942.
The polymerization reaction occurring in the fluidized bed is catalyzed by continuous or semi-continuous addition of catalyst. Such catalysts can be supported on inorganic or organic support materials.
A gas phase process suitable for the practice of the present invention provides a large steady state environment in the reaction zone of the reactor by continuously feeding reactants to the reaction zone of the reactor and removing product from the reaction zone of the reaction vessel. A continuous process that results in is preferred.
In contrast, solution polymerization conditions use a solvent for each component of the reaction. Preferred solvents include mineral oil and various hydrocarbons that are liquid at the reaction temperature. Examples of useful solvents include alkanes such as pentane, iso-pentane, hexane, heptane, octane and nonane, and kerosene and Exxon Chemicals Inc. Included are alkane mixtures such as Isopar E ™, cycloalkanes such as cyclopentane and cyclohexane, and aromatics such as benzene, toluene, xylene, ethylbenzene and diethylbenzene.
At any time, each component and the recovered catalyst component should be protected from oxygen and moisture. Thus, the catalyst components and catalyst should be prepared and recovered in an oxygen and moisture free atmosphere and are preferred. The reaction is therefore preferably carried out in the presence of a dry, eg inert gas such as nitrogen.
Ethylene is added to the reaction vessel in an amount sufficient to maintain a differential pressure that exceeds the vapor pressure of the combined α-olefin and diene monomer. C 2 content of the polymer is determined by the ratio of C 2 differential pressure to the total reactor pressure. Generally occurs in polymerization is 1,500 lbs C 2 differential pressure from square inch per 10 (psi) (10500kPa 70), and most preferably 800psi from 40 (5600kPa from 280). The polymerization temperature is suitably from 70 to 225 ° C, preferably from 80 to 170 ° C, most preferably above 80 and up to 140 ° C.
The polymerization reaction is desirably carried out under conditions sufficient to achieve at least 60 wt% ethylene conversion relative to the amount of ethylene fed to the reactor. This ethylene conversion is preferably greater than 65 wt%, more preferably greater than 70 wt%. The polymer concentration in the reactor in the steady state condition solution process is desirably 5 to 25 wt%, preferably 8 to 25 wt%, and most preferably 10 to 20 wt%. Using solution process polymer concentrations greater than 25 wt%, it is possible that the resulting polymer solution also has a solution viscosity advantageous for processing. Methods other than solution methods such as slurry method or gas phase method are different, but have polymer concentration limits that are measured rapidly.
Polymerization can be carried out in either a batch or continuous polymerization process using one or more reactors. The polymerization is preferably carried out by a continuous process so that the catalyst, ethylene, α-olefin, diene and optional solvent are continuously fed to the reaction zone and the polymer product is continuously removed therefrom.
Without limiting the scope of the invention, one means for carrying out such a polymerization process uses a stirred tank reactor in which the α-olefin monomer is introduced continuously with the solvent, diene monomer and C 2 monomer. . The reaction vessel contains a liquid phase comprising substantially C 2 , C 3 and a diene (also known as “polyene”) monomer with a solvent or additional diluent. If desired, conventional LCBs containing dienes such as NBD, 1,7-octadiene or 1,9-decadiene can also be added in small amounts, as long as the desired polymer properties are not adversely affected. Catalyst and cocatalyst are continuously introduced into the reactor liquid phase. Reactor temperature and pressure can be controlled by adjusting the solvent / monomer ratio, catalyst addition rate, and using cooling or heating coils, jackets, or both. The catalyst addition rate controls the polymerization rate. Controlling the ethylene content of the polymer product is achieved by manipulating the respective feed rates of ethylene, α-olefin and diene to the reaction vessel. The polymer product molecular weight is controlled by control of temperature, monomer concentration or other polymerization variables such as introduction of a hydrogen stream into the reactor. The reactor effluent comes into contact with a catalytic cracking agent such as water. The polymer solution is optionally heated, gaseous ethylene and polyethylene, residual dienes and residual solvents or diluents are discharged under reduced pressure, and if necessary, further devolatilization is performed with a device such as a devolatilization extruder. And recover the polymer product. In a continuous process, the average stagnation time of catalyst and polymer in the reactor is generally from 5 minutes to 8 hours, preferably from 10 minutes to 6 hours.
In a preferred method of operation, the polymerization is carried out in a continuous solution polymerization system comprising two reactors connected in series or in parallel. In one reactor, a relatively high molecular weight product (M W 50000 to 1000000, more preferably 100000 to 500000) is formed without hydrogen, while in the second reactor, a relatively low molecular product (M W 20,000 to 300,000) are formed. In the second reactor, the presence of hydrogen is optional. Alternatively, the same molecular weight product can be produced in each of the two reactors. The final product is a blend of two reactor effluents combined prior to devolatilization to obtain a homogeneous blend of the two polymer products. It is conceivable to manufacture a product with improved characteristics by such a two-reactor method. In a preferred embodiment, the reactors are connected in series, the effluent from the first reactor is charged to the second reactor, and fresh monomer, solvent and hydrogen are added to the second reactor. The reactor conditions are adjusted so that the weight ratio of polymer produced in the first reactor to polymer produced in the second reactor is from 20:80 to 80:20. However, a wider range of weight ratios can be used if desired. It is also possible to use different catalyst systems for each reactor if desired. For example, one reactor can use the metallocene-based catalyst system outlined above, and the second reactor can use normal Ziegler-Natta or other process conditions outlined This is a catalyst system based on metallocene of the type. In addition, the temperature of the second reactor is controlled to produce a low MW product. This system allows for the beneficial production of EAODM products with a wide MV range and excellent strength and processability. The preferred method of operation uses two reactors, but more than two reactors can also be used.
The following examples are illustrative and are not intended to limit the invention, whether specified or not. Unless otherwise noted, all parts and percentages are expressed on a weight basis.
Several standard tests are used to evaluate the physical properties of EAODM. This test includes MV, compositional analysis by Fourier Transform Infrared Analysis (FTIR) (ASTM D3900), and density (ASTM D-792). Other inherent properties include the rheological ratio measured as follows and the PRR measured as described above.
RR (V 0.1 / V 100 ) is available from Rheometric Scientific, Inc. It is measured by testing the sample using melt rheology techniques on an ARES (Advanced Rheometric Expansion System) dynamic mechanical spectrometer (DMS). Samples are tested at 190 ° C. using dynamic frequency mode and 2 millimeter spaced 25 millimeter (mm) radius parallel fixed plates. Five data points taken at every 10 frequencies are analyzed with a strain rate of 8% and a vibration rate increasing from 0.1 to 100 rad / sec. Each sample (pellet or bail) is 3 inches (1.18 centimeters (cm)) in size and 1/8 inch (0) thick at a pressure of 20000 psi (137.9 megapascals (MPa)) at 180 ° C. per minute. .0049cm). The plaque is quenched and cooled to room temperature (over 1 minute). Cut out a 25 mm plaque from the center of the large plaque. These 25 mm diameter sections are then inserted into the ARES at 190 ° C. and allowed to equilibrate for 5 minutes before starting the test. To minimize oxidative degradation, the sample is maintained under a nitrogen atmosphere during the analysis. Data processing and manipulation is performed by the ARES2 / A5: RSI Orchestrator Windows 95 based software package. RR measures the ratio of viscosity to shear rate curve.
Interpolymer MV (ML 1 + 4 at 125 ° C.) is measured according to American Society for Testing and Materials Test D1646-94 (ASTM D1646-94). PRR is calculated from MV and RR in accordance with the formula listed above.
Polymer MWD is measured by gel permeation chromatography (GPC) using a Millipore / water 150-C ALC / GPC chromatograph. Add 0.10 milligrams (mg) of interpolymer sample to 50.0 milliliters (ml) of 1,2,4-trichlorobenzene and heat at 160 ° C. for 2 hours. Thereafter, a 5 ml portion is dispensed into one drum (0.37 centimeter) automatic sample vial and placed in the instrument material chamber by a rotating rack having 16 storage locations. After equilibration at 130 ° C. for 90 minutes in the chromatograph, a 100 microliter sample portion was eluted on a Polymer Labs PLgel® 10 micrometer Mixed-B 900 × 7.5 millimeter GPC column at a flow rate of 1 ml per minute. Inject under conditions sufficient to achieve 60 minutes. The concentration response of the eluate is measured using a Millipore / water differential refraction index detector. TriSec v2.7 software is used to perform data collection, processing and manipulation with calibration based on NBS tracking polystyrene standards.
The catalyst efficiency (Cat. Eff.) Is expressed as polymer milliponds (MM # / #) per pound of Group 4 metal in the catalyst. In the batch method, the polymer product is weighed and determined by dividing by the amount of Group IV metal added to the reactor. In a continuous method, the polymer product weight is determined by measurement of ethylene or outlet conversion.
(Examples 1-3)
All three sample ethylene / propylene / ENB interpolymer compositions represent the present invention and were prepared using a single loop reactor designed for continuous addition of reactants and continuous removal of polymer solution. To do. After removal of the polymer solution from the reactor, devolatilization and polymer recovery are performed. Each catalyst of Example 1 and 2, cocatalyst and scavenger, (t-butylamido) - dimethyl (eta 5-2-methyl -s- indacene-1-yl) silane titanium (II) 1,3-pentadiene, FAB and MMAO (triisobutylaluminum modified methylalumoxane). See Example 3 of PCT / US97 / 07252 detailing the preparation of this catalyst (already incorporated by reference). The catalyst of Example 3 is (tetramethylcyclo-pentadienyl) dimethyl (t-butylamido) -silane titanium 1,3-pentadiene. Example 1 uses a reactor temperature of 120 ° C. and an ethylene conversion of 92.3% to obtain an interpolymer product. In Example 2, a reactor temperature of 126 ° C. and ethylene conversion of 86.1% is used to obtain the interpolymer product. Neither embodiment uses a gaseous hydrogen (H 2 ) stream. Examples 1 and 2 both use a pressure of 473 pounds per square inch (3.26 megapascals (MPa)). Example 3 has a H 2 flow rate of 10 standard cubic centimeters per minute (sccm), using a pressure of 795 psig (5.5 MPa) and a reactor temperature of 101 ° C.
The interpolymer is produced using the procedure outlined in Example 4 as a modification of Example 3 only considering the absence of PCT / US97 / 07252 hydrogen (already incorporated by reference). Thus, ethylene and polyethylene are combined into a single stream before being introduced into a dilute mixture containing mixed alkane solvent (Isopar-E ™, Exxon Chemicals Inc.) and ENB, and combined feed A mixture is formed. The combined feed mixture is continuously injected into the reactor. The blend of catalyst, cocatalyst and capture compound are combined into a single stream and are continuously injected into the reactor.
Table 1A shows the solvent, C 2, the flow rate of propylene pounds per hour (C 3) and ENB (pph). Table IA also shows catalyst (Cat) concentration parts per million (ppm) and cocatalyst (Cocat) concentration ppm and scavenger (Scav) concentration ppm and Cat, Cocat (FAB) and Scav (MMAO) flow rates pph. Table IB shows catalytic efficiency, ratio of cocat to metal (M) when M is titanium (Ti), scavenger: titanium ratio (Scav / Ti) and polymer properties (measured by MV and EAODM composition (FTIR) )), show RR, PRR, the M W and MWD. C 2 Conversion of Examples 1-3, respectively 92.3Wt%, is 86.1wt% and 83 wt%.
The reactor effluent stream is continuously introduced into the separator and the molten polymer is continuously separated from unreacted comonomer, unreacted ethylene, unreacted ENB, and solvent. An underwater pelletizer converts the molten polymer into solid pellets.
The data shown in Examples 1-3 show several things. First, polymers with acceptable PRR can be produced substantially free of hydrogen (Examples 1 and 2) or in the presence of very small amounts of hydrogen (Example 3). Second, sufficient PRR values are obtained when the interpolymer MW is changed. Third, as shown in Examples 1 and 2, the percent ethylene conversion affects the interpolymer PRR with a high conversion rate (Example 1) that results in a high PRR. All conditions that minimize vinyl end group formation (also known as “vinyl termination”), such as low polymerization temperature (below 70 ° C.), high hydrogen concentration (above 0.1 mol%), or both It is believed to lead to an interpolymer of less than PRR4.
The EPDM interpolymer is prepared using a dual reactor arrangement (with the first reactor connected in series with the second reactor) rather than the single reactor of Examples 1-3. Each reactor is devised and arranged in the same way as a single reactor except that the polymer recovery is after the second reactor. Polymer production in the first reactor follows the procedure used in the single reactor without polymer recovery due to different variables. Similar to Examples 1 and 2, there is no hydrogen flow in the first reactor. The variables are as follows: C 2 feed rate 22.9pph, C 3 feed rate 9.3pph, ENB feed rate 0.08Pph, reactor temperature 114 ° C., the catalyst flow rate 0.57Pph, cocatalyst (Cocat or FAB) flow rate 0.72Pph, scavenger ( scav or MMAO) flow rate 0.56pph, FAB / Ti (cocat / Ti) ratio 3.98, Scav / Ti ratio 3.98 and C 2 conversion 92.9%. The catalyst efficiency is 0.295 MM # / #. The reactor pressure is 475 psig (3.28 MPa).
The product of the first reactor enters the second reactor and encounters a new set of variables including gaseous hydrogen (H 2 ). The variables are as follows: C 2 feed rate 8.2 pph, C 3 feed rate 3.9 pph, ENB feed rate 0.03 pph, H 2 feed rate 364 sccm (0.018 mol% H 2 , fresh mole in feed H 2 in feed fresh H 2 mol and based on divided by the sum of fresh C 2 molar in the feed), reactor temperature 110 ° C., the catalyst flow rate 0.41Pph, FAB velocity 0.51Pph, MMAO flow rate 0.48pph, cocat / Ti ratio 3 .77, Scav / Ti ratio 4.94 and C 2 conversion 82.6%. The reactor pressure is the same as in the first reactor. The catalyst efficiency is 0.315 MM # / #. The resulting polymer propylene content 28.1 percent, a 0.55% ENB content, is based on any of percent polymer weight were obtained, total MV22.9, total M W 109100, all MWD2.85 , RR42 and PRR36.3. Samples of the polymer solution in the first reactor, by analysis, indicating the MV40 estimated from PRR76 and M W.
The reactor split between the first reactor and the second reactor is 59:41, meaning that 59% of the interpolymer is formed in the first reactor. As an initial condition for the first reactor, 59% of the interpolymer contains LCB.
Example 4 shows some points like Example 1-3. First, the interpolymers of the present invention can be produced with a dual reactor composition even when favorable conditions for 4 or more PRRs exist in only one of the two reactors. . However, those skilled in the art will note that in order to achieve a second reactor product having a PRR of at least 4, the polymer product of the first reactor must necessarily have a correspondingly higher PRR. It has recognized. Second, MWD spread due to the dual reactor composition does not adversely affect the interpolymer PRR.
(Example 5 and Comparative Example A)
Example 4 is repeated using the conditions shown in Table IIA-IID.
Comparison of Example 5 and Comparative Example A shows the effect on hydrogen concentration change. As in Comparative Example A, excess hydrogen causes the PRR to be less than 4.
(Example 6 and Comparative Example B)
EAODM interpolymer 100 pbw, low density polyethylene (LDPE) 8 pbw (melting index 2 dg / min, density 0.92 grams per cubic centimeter, LD-400, Exxon Chemical), treated clay (vinylsilane treated aluminum silicate (calcined) 60 pbw, Translink (Registered trademark) 37, Engelhard), zinc oxide 5 pbw (85% zinc oxide in EPDM binder, ZnO-85-SG, Rhein-Chemie), lead stabilizer 5 pbw (90% lead in EPDM binder, TRD- 90, Rhein-Chemie), paraffin wax 5 pbw (melting point 130-135 ° F. (54-57 ° C.) International Waxes, Ltd.), antioxidant 1 pbw (polymerized 1,2-dihydro-2, , 4-trimethylquinoline, Agateite® resin D, RT Vanderbilt), 1 pbw crosslinker (vinyl-tris- (2-methoxy-ethoxy) silane 40% in wax binder, PAC-473, OSI Standard wire and cable compositions including Specialties) and 3.5 pbw dicumyl peroxide (DiCUP®, Hercules) are processed using a Davis-Standard extruder. In Example 6, the polymer is prepared in the same manner as in Example 4, but the MV is 18, not 22. In Comparative Example B, the polymer was DuPont Dow Elastomers L. L. C. Nordel <(R)> 2722, commercially available from the company Ethylene / propylene / 1,4-hexadiene / NBD tetrapolymer. The extruder is a 3.5 inch (8.9 centimeter) extruder with a barrier screw and mixing tip and a length to diameter ratio (L / D) of 20: 1. The extrusion tube die has an outer diameter of 52.6 millimeters (mm), an inner diameter of 0.375 inches (9.5 mm) and a length of 0.66 inches (16.8 mm). The extruder has a feed area, three continuous mixing areas, a die head area and a die area, each of which is 190 ° F. (88 ° C.), 190 ° F. (88 ° C.). ), 200 ° F. (93 ° C.), 200 ° F. (93 ° C.), 225 ° F. (107 ° C.), and 225 ° F. (107 ° C.). Table III below shows the extruder operating variables and extrusion characteristics of Example 6 and Comparative Example B.
The data in Table III shows that the EPDM interpolymers of the present invention that do not contain conventional LCB monomers provide properties that are comparable to the extrusion properties of conventional tetrapolymers that contain conventional LCB monomers. This data also shows that the EPDM interpolymers of the present invention are processed at lower pressures than tetrapolymers by a similar process speed extruder.
Example 7-Production of thermoplastic elastomer
TPE is PP63% (AccPro® 9934, Amoco Chemical), 27% interpolymer prepared as in Example 4, and 1 micrometer talc (Microtuf® AG101, Specialty Minerals) 10% To prepare. This interpolymer has MV18, RR29.3 and PRR24.96. This interpolymer is expected to be MWD 2.8 based on other properties. This combination occurs in a 30 mm Werner Pfleiderer twin screw extruder operated at a set temperature of 220 ° C. at a speed of 200 revolutions per minute (rpm) and produces an extrudate at a temperature of 225 ° C. The resulting extrudate is molded on a 100 ton (800 kilonewton) Arburg molding machine using a molding temperature of 83 degrees Fahrenheit (28 ° C.) to form a test plaque. Various data are obtained in the physical property test of the test plaque. The Shore D hardness (ASTM D-2240) at 1 and 10 seconds of this sample is 62.2 and 58.9, respectively. The test plaque has the following tensile properties (ASTMD-638) when tested at a pull rate of 2 inches (in) (5.1 cm) per minute. Tensile strength at break 2599 psi (17.9 MPa), ultimate elongation 44%, tensile strength 3064 psi (21.1 MPa) at production, and elongation 6% at production. Weldline tensile properties (ASTM D-638, tensile speed 2 inches per minute / 5.1 cm): tensile strength at break 1877 psi (12.9 MPa), ultimate elongation 2%, tensile strength at production 1877 psi (12 0.9 MPa), and the elongation at production is 2%. This plaque has a melt index (I 2 ) (ASTM D-1238, 230 ° C., 2.16 kg) of 11.49 decigrams per minute (dg / min). When performing a three-point bending test (ASTM D-790), the test reveals a bending coefficient of 219273.5 psi (1511.9 MPa) and a second coefficient of 158680.9 psi (1094.1 MPa). The results of the gloss test (ASTM D-523) are 26.1, 55.0 and 96.9 at incident angles of 20 °, 60 ° and 85 °, respectively. The Dynatup total energy tested at 23 ° C. is rated 15.3 ft-lbs (20.74 Joules (J)). The results of the Izod impact strength test at 23 ° C. and −30 ° C. are 0.97 ft-lbs / in and 0.70 ft-lbs / in, respectively. The weld line Izod impact strength at room temperature is 1.43 ft-lbs / in. (3.0 KJSM (Kilo Joules Square Meters)). The heat distortion at 66 psi (0.46 KPa) is 94.3 ° C.
Example 8-TPO preparation
Example 7 is repeated using EO copolymer prepared in a single reactor instead of the interpolymer used in Example 7. The EO copolymer is MV21, RR16 and PRR10.7. The resulting samples have a Shore D hardness of 65.4 and 61.6 at 1 and 10 seconds, respectively. Tensile properties are: tensile break strength 2342 psi (16.1 MPa), ultimate elongation 146%, tensile strength 3309 psi (22.8 MPa) during production, and elongation 8% during production. The tensile properties of the weld line are: tensile rupture strength 1983 psi (13.7 MPa), ultimate elongation 2%, tensile strength 1978 psi (13.6 MPa) during production, and elongation 2% during production. This plaque is I 2 11.49 dg / min. The flexural modulus and 2% Secant modulus are 209944.0 psi (1447.5 MPa) and 167938.0 psi (1157.9 MPa), respectively. The results of the gloss test are 51.5, 71.5 and 91.2 at incident angles of 20 °, 60 ° and 85 °, respectively. The Dynatup test tested at 23 ° C has a rating of 20.5 ft-lbs (27.8 J). The result of the Izod impact strength test at 23 ° C. is 2.39 ft-lbs / in (5.0 KJSM). The weld line Izod impact strength at room temperature is 1.82 ft-lbs / in. (3.8KJSM).
Examples 7 and 8 show that satisfactory TPE and TPO can be prepared using the inventive interpolymers, respectively. Other TPEs, TPOs and TPVs are suitably prepared in accordance with the teaching provided herein.
Example 9-EAO polymer production
The process of Examples 1 and 2 is repeated except that the H 2 stream is added and the variables and monomers are changed to produce the EO copolymer. The variables are as follows: C 2 feed rate 30.4 pph, C 8 feed rate 29.8 pph, H 2 feed rate 10.6 sccm (0.0055 mol%), reactor temperature 102 ° C., first catalyst flow 0.65 pph, co-cat flow 0 .35 pph, scav flow 0.69 pph, Cz conversion 89.8%, reactor pressure 475 psig (3.28 MPa), catalyst efficiency 0.78 MM # / #, cocat / Ti molar ratio 4, and Scav / Ti molar ratio 5. 54. The resulting polymers are MV21.4, RR16, PRR10.7, MW120300 and MWD2.6.
Any results similar to those obtained in Examples 1-9 are expected with the other catalysts, cocatalysts, scavengers and process variables disclosed above.
[1] Shear thinning ethylene / α-olefin interpolymer, wherein the interpolymer is polymerized with ethylene, at least one α-olefin monomer, and optionally at least one diene monomer. Having a processing rheological ratio (PRR) of at least 4;
PRR = (interpolymer viscosity measured at 190 ° C. and shear rate of 0.1 rad / sec) / (interpolymer viscosity measured at 190 ° C. and shear rate of 100 rad / sec) + [3.82−interpolymer Mooney viscosity (ML 1 + 4 @ 125 ° C.)] × 0.3.
[2] The interpolymer is
(A) having a weight ratio of ethylene to α-olefin in the range of 90:10 to 10:90, wherein the α-olefin is a C 3-20 α-olefin;
(B) The interpolymer according to [1], characterized in that it has a diene monomer content in the range of 0 to 25 weight percent based on the interpolymer weight.
[3] The interpolymer according to [1], wherein the interpolymer has a Mooney viscosity (ML 1 + 4 at 125 ° C.) in the range of 0.5 to about 200.
[4] The interpolymer according to [1], wherein the interpolymer has a molecular weight distribution (Mw / Mn) of at least 2.0.
[5] The interpolymer according to [4], wherein the molecular weight distribution is at least 2.5 and the PRR is at least 8.
[6] The interpolymer according to [1], wherein the interpolymer is an EAODM interpolymer having a molecular weight distribution of at least 2.3, a Mooney viscosity (ML 1 + 4 at 125 ° C.) of at least 15 and a PRR of at least 20. .
[7] The interpolymer according to [1], wherein the interpolymer is an ethylene / octene-1 copolymer having a molecular weight distribution of at least 2.3 and a Mooney viscosity (ML 1 + 4 at 125 ° C.) of at least 5.
[8] The α-olefin is selected from the group consisting of propylene, butene-1, pentene-1,4-methyl-pentene-1, hexene-1, octene-1, styrene, p-methylstyrene, and mixtures thereof. And the optional diene monomer is 5-ethylidene-2-norbornene, 5-vinylidene-2-norbornene, 5-methylene-2-norbornene, 1,4-hexadiene, 1,3-pentadiene, 7-methyl-1 , 6-octadiene, 1,3-butadiene, 4-methyl-1,3-pentadiene, 5-methyl-1,4-hexanediene, 6-methyl-1,5-heptadiene and mixtures thereof The interpolymer according to [2], wherein
[9] Further comprising a PRR promoting amount of an additional diene monomer, wherein the additional diene monomer is selected from the group consisting of dicyclopentadiene, norbornadiene, 1,7-octadiene, and 1,9-decadiene. The interpolymer according to [2], wherein
[10] A process for producing an ethylene / α-olefin interpolymer according to [1], wherein the process is carried out under conditions sufficient to achieve an ethylene conversion of at least 60 weight percent. Contacting the olefin monomer and optionally at least one diene monomer with the catalyst and the activating cocatalyst, wherein the conditions are at a temperature of at least 70 ° C. and optionally in the presence of an effective amount of hydrogen. The method, wherein the amount is sufficient to maintain an interpolymer PRR of at least 4 and the catalyst is a geometrically constrained metal composite.
[11] The method according to [10], wherein the amount of hydrogen is more than 0 mole percent but less than 0.10 mole percent with respect to the sum of the total monomer content and the hydrogen content.
[12] The method according to [10], wherein the hydrogen amount is more than 0 mole percent but less than 0.05 mole percent with respect to the sum of the total monomer content and the hydrogen content.
[13] The catalyst is (t-butyl-amido) -dimethyl (η 5 -2-methyl-s-indasen-1-yl) silane-titanium (IV) dimethyl, (t-butylamido) -dimethyl- (η 5 -2-Methyl-s-indacene-1-yl) silane titanium (II) 1,3-pentadiene and (t-butylamido) dimethyl- (η 5 -2-methyl-s-indacene-1-yl) silane-titanium (II) 2,4-hexadiene or (t-butylamido) -dimethyl (η 5 -2,3-dimethylindenyl) silane titanium (II) 1,4-diphenyl-1,3-butadiene, (t-butyl- amide) - selected from dimethyl (eta 5-2,3-dimethyl -s- indacene-1-yl) silane titanium (IV) dimethyl and mixtures thereof Characterized in that it is selected from the group consisting of Group B catalyst, [10] The method according.
[14] The method according to [10], wherein the activating cocatalyst is trispentafluorophenylborane.
[15] The interpolymer has an ethylene content of 20 to 95 weight percent (wt%), an α-olefin content of 80 to 5 wt%, and the α-olefin is a C 3-20 α-olefin, optionally from 0 [10] The process of [10], characterized in that it has a diene monomer content in the range of 25 weight percent, all of the percentages being based on the interpolymer weight and totaling 100 wt%.
[16] The method according to [10], wherein the interpolymer is amorphous.
[17] The method of [10], wherein the interpolymer is at least partially crystalline, the temperature is at least 80 ° C., and the ethylene conversion is at least 80%.
[18] An article of manufacture characterized in that at least one part is formed from a composition comprising the interpolymer of claim 1.
[19] The article is selected from the group consisting of wire and cable components, electrical insulators, belts, hoses, tubes, gaskets, membranes, molded articles, extruded parts, automotive parts, adhesives, tire walls and tires. The article according to [18], which is characterized.
[20] The composition is further at least one selected from the group consisting of a filler, a fiber, a plasticizer, an oil, a colorant, a stabilizer, a foaming agent, a setting retarder, a setting accelerator, and a crosslinking agent. The article according to [18], characterized by comprising the additive:
[21] The composition contains more than 50 parts by weight of the crystalline polyolefin resin and less than 50 parts by weight of the interpolymer of [1], and the total amount of the crystalline polyolefin resin and the interpolymer is 100 parts by weight. A polymer blend composition.
[22] The composition comprises less than 60 to less than 10 parts by weight of crystalline polyolefin resin and more than 40 to 90 parts by weight of the interpolymer of [1], wherein the interpolymer comprises at least the composition relative to the weight of the interpolymer. A thermoplastic vulcanization composition characterized in that it is at least partially crosslinked so as to have a gel content of 70% and the total amount of crystalline polyolefin resin and interpolymer is 100 parts by weight.
[23] The crystalline polyolefin resin comprises a polypropylene homopolymer, propylene and ethylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 2-methyl-1-propane or 4-methyl-1-pentene. The composition according to [21] or [22], characterized in that it is a copolymer of an α-olefin selected from the group, or a blend of polypropylene homopolymer and propylene / α-olefin copolymer or a mixture thereof.
[24] The composition according to [23], wherein the α-olefin is ethylene.
[25] An article manufactured from the composition according to any one of [21] to [24].
Shear thinning ethylene / α-olefin interpolymer,
The interpolymer has polymerized ethylene, at least one α-olefin monomer and at least one diene monomer therein,
Processing rheological ratio (PRR) of 10 to 35.8, where said PRR = (interpolymer viscosity measured at 190 ° C. and shear rate 0.1 rad / sec) / (measured at 190 ° C. and shear rate 100 rad / sec) Interpolymer viscosity) + [3.82-interpolymer Mooney viscosity (ML 1 + 4 @ 125 ° C.)] × 0.3,
2.5 to 3.8 molecular weight distribution (Mw / Mn) and at least 15 Mooney viscosities (ML 1 + 4 at 125 ° C.)
An interpolymer that is characterized by:
The interpolymer is
(A) having a weight ratio of α-olefin to ethylene in the range of 90:10 to 10:90, wherein the α-olefin is a C 3-20 α-olefin;
2. The interpolymer of claim 1 having a diene monomer content of 25 weight percent or less based on (b) interpolymer weight.
The interpolymer according to claim 1 or 2, wherein the interpolymer has a Mooney viscosity (ML 1 + 4 at 125 ° C) in the range of 15 to 200.
The interpolymer according to any one of claims 1 to 3, wherein the diene is a non-conjugated diene.
The α-olefin is selected from the group consisting of propylene, butene-1, pentene-1,4-methyl-pentene-1, hexene-1, octene-1, styrene, p-methylstyrene and mixtures thereof; The diene monomer is 5-ethylidene-2-norbornene, 5-vinylidene-2-norbornene, 5-methylene-2-norbornene, 1,4-hexadiene, 1,3-pentadiene, 7-methyl-1,6-octadiene, Is selected from the group consisting of 1,3-butadiene, 4-methyl-1,3-pentadiene, 5-methyl-1,4-hexadiene, 6-methyl-1,5-heptadiene and mixtures thereof; The interpolymer according to any one of claims 1 to 3.
The interpolymer further comprises a PRR promoting amount of an additional diene monomer, wherein the additional diene monomer is selected from the group consisting of dicyclopentadiene, norbornadiene, 1,7-octadiene and 1,9-decadiene; The interpolymer according to any one of claims 1 to 5.
An article of manufacture that is formed from a composition comprising the interpolymer of any one of claims 1-6.
8. An article of manufacture according to claim 7, wherein the article is selected from wire and cable components.
The composition further comprises at least one additive selected from the group consisting of fillers, fibers, plasticizers, oils, colorants, stabilizers, foaming agents, set retarders, set accelerators and crosslinkers. The manufactured article according to claim 7, which is included.
A polymer comprising more than 50 parts by weight of crystalline polyolefin resin and less than 50 parts by weight of the interpolymer according to any one of claims 1 to 6, wherein the total amount of crystalline polyolefin resin and interpolymer is 100 parts by weight Blend composition.
7. comprising less than 60 to less than 10 parts by weight of crystalline polyolefin resin and greater than 40 to 90 parts by weight of the interpolymer according to any one of claims 1 to 6, wherein the composition is at least 70% based on the weight of the interpolymer A thermoplastic vulcanization composition wherein the interpolymer is at least partially crosslinked so that the total amount of crystalline polyolefin resin and interpolymer is 100 parts by weight so as to have a gel content of
The crystalline polyolefin resin is a group consisting of polypropylene homopolymer, propylene, ethylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 2-methyl-1-propane or 4-methyl-1-pentene. 11. A composition according to claim 10 which is a copolymer of [alpha] -olefins selected from or a blend of polypropylene homopolymer and propylene / [alpha] -olefin copolymers or mixtures thereof.
The crystalline polyolefin resin is a group consisting of polypropylene homopolymer, propylene, ethylene, 1-butene, 1-pentene, 1-hexene, 1-octene, 2-methyl-1-propane or 4-methyl-1-pentene. The composition of claim 11, which is a copolymer of an α-olefin selected from: or a blend of polypropylene homopolymer and propylene / α-olefin copolymer or a mixture thereof.
The composition according to claim 13, wherein the α-olefin is ethylene.
An article of manufacture formed from the composition of any one of claims 10 to 14.
JP2012031987A 1998-11-02 2012-02-16 Shear thinning ethylene / α-olefin interpolymers and methods for their production Active JP6039906B2 (en)
US10656998P true 1998-11-02 1998-11-02
US60/106,569 1998-11-02
JP2000579651 Division 1999-11-02
JP2012136706A JP2012136706A (en) 2012-07-19
JP6039906B2 true JP6039906B2 (en) 2016-12-07
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JP2000579651A Expired - Lifetime JP5276757B2 (en) 1998-11-02 1999-11-02 Shear thinning ethylene / α-olefin interpolymers and methods for their production
JP2012031987A Active JP6039906B2 (en) 1998-11-02 2012-02-16 Shear thinning ethylene / α-olefin interpolymers and methods for their production
JP2014078394A Active JP6117143B2 (en) 1998-11-02 2014-04-07 Shear thinning ethylene / α-olefin interpolymers and methods for their production
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