ELASTOMER COMPOSITION AND ARTICLE

专利摘要:
elastomer composition and article incorporations of the invention provide block composites and their use in soft compounds.
公开号:BR112012007271B1
申请号:R112012007271-4
申请日:2010-10-01
公开日:2021-03-23
发明作者:Colin Li Pi Shan；Kim L. Walton；Gary R. Marchand；Ashish Batra；Eddy I. Garcia Meitin；Jeffrey D. Weinhold
申请人:Dow Global Technologies Llc；
IPC主号:

专利说明:

[0001] [0001] This invention relates to block composites and their use in soft compounds. History of the invention
[0002] [0002] The manufacture of durable goods in the United States alone accounts for the annual consumption of millions of tons of plastics. Durable goods are manufactured products capable of long utility that are found in various markets such as automotive, construction, medical, food and beverage, electrical, appliances, industrial machinery, and consumer markets. In these markets, some applications require the use of flexible polymers or mixtures of them with other polymers or with oils. These applications include, but are not limited to, toys, suitcases, door handles and soft touch, bumper wear bands, floors, car floor mats, wheels, casters, furniture and appliance feet, labels, hydraulic seals , gaskets such as static and dynamic gaskets, automotive doors, bumper strip, grille components, oscillator panels, hoses, liners, office supplies, coatings, diaphragms, tubes, caps, plugs, injection pistons, distribution, kitchen utensils, footwear, shoe dampers and shoe soles.
[0003] [0003] For use in applications in durable goods, polymers or mixtures of them with other polymers or oils, desirably have good processability (i.e., moldability), attractive appearance (for example, transparent or colored), appropriate surface properties ( for example, good adhesion to substrates, tactile sensation like rubber, non-viscous and good ability to receive paint), and a good combination of mechanical properties (for example, flexibility, thermal resistance, scratch and / or abrasion resistance, toughness , tensile strength, and compression deformation). Some polymers that have properties suitable for durable goods include flexible poly (vinyl chloride) (f-PVC), poly (styrene / butadiene / styrene) (SBS), poly (styrene-ethylene / butadiene-styrene) (SEBS), vulcanized thermoplastics (TPV), thermoplastic polyurethane (TPU) and polyolefins such as polyolefin homopolymers and olefin interpolymers.
[0004] [0004] Some polyolefins such as polypropylene (PP) and low density polyethylene (LDPE) are widely accepted for use in durable goods applications due to their ease of molding, good mechanical properties and thermal resistance. In addition, many formulations based on mixtures of polyolefins and other polymers have been developed to satisfy the demands required for the production of durable goods parts. For example, a mixture of polypropylene and polyethylene can be used to make fibers for applications in artificial tufts.
[0005] [0005] Additionally, some flexible polymers including some polyolefinic homopolymers or polyolefinic interpolymers can be sticky, which is an undesirable property in some processes or applications. In general, additives, such as fatty acid amides, waxes or other non-sticky polymers, can be mixed with such flexible polymers to reduce their stickiness. However, such additives are only effective to a certain extent and are known to have some undesirable properties of their own.
[0006] [0006] Despite the availability of a variety of polyolefins and their mixtures, there is a continuing need for new polymers or new polymer mixtures that have improved performance properties and characteristics. Summary of the invention
[0007] [0007] Compositions formulated featuring this combination of good modulus and low temperature impact performance have now been discovered. The compositions comprise: (A) a block composite, and (B) an oil. Brief description of the drawings
[0008] [0008] Figure 1 shows the DSC melting curve for Example B1;
[0009] [0009] Figure 2 shows the DSC melting curve for Example F1;
[0010] [0010] Figure 3 compares the TREF profiles of Examples B1, C1 and D1;
[0011] [0011] Figure 4 shows DSC curves of Examples B2 and B3;
[0012] [0012] Figure 5 shows DSC curves of Examples F2 and F3;
[0013] [0013] Figure 6 shows the composite composite index for Examples B1, F1, C1, H1, D1 and G1;
[0014] [0014] Figure 7 shows the composite composite index for Examples B1, V1, Z1, C1, W1, AA1, D1, X1, and AB1;
[0015] [0015] Figure 8 shows dynamic-mechanical analysis of Examples B1, C1 and D1;
[0016] [0016] Figure 9 shows dynamic-mechanical analysis of Examples F1, G1 and H1;
[0017] [0017] Figure 10 shows a TEM micrograph of PROFAX ULTRA SG853 polypropylene impact copolymer in 5 mm and 1 mm scales;
[0018] [0018] Figure 11 shows TEM micrographs of Examples B1, C1 and D1 in 1 mm and 0.5 mm scales;
[0019] [0019] Figure 12 shows TEM micrographs of Examples F1, G1 and H1 in scales of 2 mm, 1 mm and 0.5 mm;
[0020] [0020] Figure 13 shows TEM micrographs of Examples B2, D2 and B3 in 0.5 mm and 0.2 mm scales;
[0021] [0021] Figure 14 shows Example B2 in 1 mm and 200 nm scales;
[0022] [0022] Figure 15 shows SEM images of Comparative Example 1 on the left and Example 1 on the right on a 200 mm scale;
[0023] [0023] Figure 16 shows SEM images of Comparative Example 1 on the left and Example 1 on the right on a 100 mm scale;
[0024] [0024] Figure 17 shows SEM images of Comparative Example 1 on the left and Example 1 on the right on a 10 mm scale;
[0025] [0025] Figure 18 shows SEM images of Comparative Example 1 on the left and Example 1 on the right on a 5 mm scale;
[0026] [0026] Figure 19 shows SEM images of Example 1 on a 4 mm scale; and
[0027] [0027] Figure 20 shows a comparison of the property relative to the traction of the control sample against that of the inventive sample (C1 with 20% by weight of oil) open like two other comparatives. Description of embodiments of the invention Definitions
[0028] [0028] All references to the Periodic Table of Elements here will refer to the Periodic Table of Elements published and registered by CRC Press, Inc., 2003. Likewise, any references to a Group or Groups will be to a Group or Groups shown in this Table Periodic Table of Elements using the IUPAC system to number groups. Unless stated to the contrary, implicit in context, or customary in the technique, all parts and percentages are based on weight and all testing methods are current as of the filing date of this disclosure. For United States patent practice purposes, the contents of any patent, patent application, or publication referred to herein are hereby incorporated by reference in their entirety (or the equivalent US version thereof is also incorporated by reference) especially with respect to the dissemination of synthetic techniques, definitions (to the extent not inconsistent with any definitions provided herein) and general knowledge of the technique.
[0029] [0029] The term "comprising" and its derivatives is not intended to exclude the presence of any additional component, step or procedure, whether or not it is specifically disclosed. In order to avoid any doubt, all compositions claimed herein using the term "comprising" may include any additive, adjuvant, or compound, polymeric or not, additional, unless otherwise stated. In contrast, the term, "consisting essentially of" excludes any other component, step or procedure from the scope of any subsequent mention, except those that are not essential to operability. The term "consisting of" excludes any component, step or procedure not specifically described or listed. Unless otherwise stated, the term "or" refers to members listed individually as well as in any combination.
[0030] [0030] The term "polymer" includes both conventional homopolymers, that is, homogeneous polymers prepared from a single monomer, and copolymers (referred to here interchangeably with interpolymers), meaning polymers prepared by reacting at least two monomers or differently containing in the same segment or chemically differentiated blocks even if formed from a single monomer. More specifically, the term "polyethylene" includes ethylene homopolymers and ethylene copolymers and one or more C3-8 α-olefins in which ethylene comprises at least 50 mole percent. If used, the term "crystalline" refers to a polymer or polymer block that has a crystalline melting point or first order transition (Tm) determined by differential scanning calorimetry (DSC) or equivalent technique. The term can be used interchangeably with the term "semi-crystalline". The term "amorphous" refers to a polymer lacking a crystalline melting point. The term "isotactic" is defined as polymer repeating units having at least 70 per cent of finished by NMR analysis of C. Polymers having at least 90 per cent of isotactic patches are defined as "very isotactic" .
[0031] [0031] The term "block copolymer" or "segmented copolymer" refers to a polymer comprising two or more chemically distinct segments or regions (also referred to as "blocks") that preferably join end-to-end with with respect to polymerized ethylene functionality, rather than in pendant or grafted mode. In a preferred embodiment, the blocks differ in the amount or type of comonomer incorporated in them, density, amount of crystallinity, size of crystallite attributable to a polymer of such composition, type and degree of tacticity (isotactic or syndiotactic), regio-regularity or region-irregularity, amount of branching, including long-chain or hyper-branching branching, homogeneity, or for any other chemical or physical property. The block copolymers of the invention are characterized by unique polydispersity index distributions (PDI or Mw / Mn), block length distribution, and / or block number distribution due, in a preferred embodiment, to the effect of the agent (s) exchange (s) in combination with the catalyst (s).
[0032] [0032] The term "block composite" refers to the new polymers of the invention comprising a soft copolymer, a hard polymer and a block copolymer having a soft segment and a hard segment, the hard segment of the block copolymer having the same composition of the hard polymer in the block composite and the soft segment of the block copolymer has the same composition as the soft copolymer of the block composite. Block copolymers can be linear or branched. More specifically, when produced in a continuous process, the block composites desirably have PDI of 1.7 to 15, preferably of 1.8 to 3.5, more preferably of 1.8 to 2.2, and most preferably of 1, 8 to 2.1. When produced in a batch or semi-batch process, the block composites desirably have PDI from 1.0 to 2.9, preferably from 1.3 to 2.5, more preferably from 1.4 to 2.0, and most preferably from 1.4 to 1.8.
[0033] [0033] "Hard" segments refer to very crystalline blocks of polymerized units in which the monomer is present in an amount greater than 90 percent, preferably greater than 93 percent by weight, and more preferably greater than 95 mol%, and most preferably greater than 98 mole percent. In other words, the comonomer content in the hard segments is most preferably less than 2 molar percent, more preferably less than 5 molar percent, and preferably less than 7 molar percent, and less than 10 molar percent. In some incorporations, the hard segments comprise all or substantially all propylene units. On the other hand, "soft" segments refer to amorphous, substantially amorphous or elastomeric blocks of polymerized units in which the comonomer content is greater than 10 mol%.
[0034] [0034] The block composite polymers of the invention are preferably produced by a process comprising contacting a monomer or mixture of monomers polymerizable by addition under conditions of polymerization by addition with a composition comprising at least one polymerization catalyst by addition, a co-polymerization. catalyst and a chain exchange agent, said process characterized by the formation of at least some growing polymer chains, under different process conditions in two or more reactors operating under steady state polymerization conditions, or in two or more zones of reaction operating under polymerization conditions in continuous flow.
[0035] [0035] In a preferred embodiment, the block composites of the invention comprise a fraction of block polymer that has a very likely distribution of block lengths. According to the invention, the preferred polymers are block copolymers containing 2 or 3 blocks or segments. In a polymer containing three or more segments (i.e., blocks separated by a distinguishable block) each block can be the same or chemically different and, in general, characterized by a distribution of properties. In a process for preparing the polymers, chain exchange agent is used as a way to extend the life of a polymer chain such that a substantial fraction of the polymer chain leaves at least the first reactor in a series of multiple reactors or the first zone in a multizone reactor operating substantially under continuous flow conditions in the form of polymer terminated with a chain exchange agent, and the polymeric chain experiences different polymerization conditions in the next reactor or polymerization zone. Different polymerization conditions in the respective reactors or zones include the use of different ratios of monomers, comonomers, or monomers / comonomers, different polymerization temperatures, pressures or partial pressures of various monomers, different catalysts, different monomer gradients, or any other difference that leads to the formation of a distinguishable polymeric segment. Consequently, at least a portion of the polymer comprises two, three or more, preferably two or three distinct polymeric segments arranged in an intramolecular manner.
[0036] [0036] The following mathematical treatment of the resulting polymers is based on the theoretically derived parameters that are believed to apply and demonstrate that, especially in two or more zones or continuous reactors connected in series at steady state, having different polymerization conditions to which the polymer in growth is exposed, the block lengths of the forming polymer in each reactor or zone will be in accordance with a very probable distribution, derived in the following way, in which pi is the probability of polymer propagation in a reactor with respect to the block sequence of catalyst i. The theoretical treatment is based on hypotheses and standardized methods known in the art and used to predict the effects of polymerization kinetics on molecular architecture, including the use of mass rate reaction expressions that are not affected by block lengths or chains, and the hypothesis that polymeric chain growth is completed in a very short time compared to the average time spent in the reactor. Such methods have been previously disclosed in W.H. Ray, J. Macromol. Sci., Macromol. Chem, C8, 1 (1972) and in A.E. Hamielec and J.F. MacGregor, "Polymer Reaction Engineering", K.H. Reichert and W. Geisler, Eds., Hanser, Munich, 1983. Furthermore, it is assumed that each incidence of the chain exchange reaction in a given reactor results in the formation of a single polymeric block, whereas the transfer of the finished polymer by chain exchange agent for a different zone or reactor and exposure to different polymerization conditions results in the formation of a different block. For catalyst i, the fraction of sequences of length n produced in a reactor is given by Xi [n], where n is an integer from 1 to infinity representing the total number of monomeric units in the block.
[0037] [0037] Xi [n] = (1-pi) pi (n-1) very likely distribution of block lengths
[0038] [0038] If more than one catalyst is present in a reactor or zone, each catalyst will have a propagation probability (pi) and, therefore, will have a single average block length and distribution for the polymer being prepared in that reactor or zone. In a most preferred embodiment, the probability of propagation is defined as:
[0039] [0039] Rp [i] = Local monomer consumption rate per catalyst i, (mol / L / time)
[0040] [0040] Rt = Total rate of termination and transfer of chain to catalyst i, (mol / L / time), and
[0041] [0041] Ri [i] = Local rate of chain transfer with inactive polymer, (mol / L / time).
[0042] [0042] For a given reactor, the polymer propagation rate, Rp [i], is defined using an apparent rate constant, kpi, multiplied by a total monomer concentration, [M], and multiplied by the local concentration of catalyst i, [Ci], as follows: Rp [i] = kpi [M] [Ci]
[0043] [0043] Transfer rate, termination and chain exchange is determined as a function of chain transfer to hydrogen (H2), elimination of beta hydride, and chain transfer chain exchange agent (CSA). The quantities [H2] and [CSA] are molar concentrations and each subscribed k value is a rate constant for the reactor or zone: Rt [i] = kH2i [H2] [Ci] + kβi [Ci] + kai [CSA] [Ci]
[0044] [0044] Inactive polymer chains are created when a polymer portion is transferred to a CSA and it is assumed that each of all reacting CSA parcels is paired with an inactive polymer chain. The exchange rate of inactive polymer chain with catalyst I is given below, where [CSAf] is the feed concentration of CSA, and the amount ([CSAf] - [CSA]) represents the concentration of inactive polymer chains: Rs [i] = kai [Ci] ([CSAf] - [CSA])
[0045] [0045] As a result of the previous theoretical treatment, it can be observed that the global block length distribution for each block of the resulting block copolymer is the sum of the block length distribution given previously by Xi [n], weighted by the rate of local polymer production for catalyst i. This means that a polymer prepared in at least two different polymer forming conditions will have at least two distinguishable blocks or segments each having a very likely block length distribution. Monomers
[0046] [0046] Monomers suitable for use in the preparation of the copolymers of the present invention include any addition-curable monomers, preferably any olefin or diolefin monomer, more preferably any a-olefin, and most preferably ethylene and at least one copolymerizable comonomer having from 4 to 20 carbon atoms, or 1-butene and at least one copolymerizable comonomer having from 2 or 5 to 20 carbon atoms, 4-methyl-1-pentene and at least one different copolymerizable comonomer having from 4 to 20 carbon atoms. Preferably, the copolymers comprise propylene and ethylene. Examples of suitable monomers include 2 to 30 normal or branched chain a-olefins, preferably 2 to 20 carbon atoms, such as ethylene, propylene, 1-butene, 1-pentene, 3-methyl-1-butene, 1 -hexene, 4-methyl-1-pentene, 3-methyl-1-pentene, 1-octene, 1-decene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1-octadecene and 1-eicosene; cycloolefins from 3 to 30, preferably from 3 to 20 carbon atoms, such as cyclopentene, cycloheptene, norbornene, 5-methyl-2-norbornene, tetracyclododecene, and 2-methyl-1,4,5,8- dimethane-1,2,3,4,4a, 5,8,8a-octahydro-naphthalene; di and polyolefins, such as butadiene, isoprene, 4-methyl-1,3-octadiene, 1,4-octadiene, 1,5-octadiene, 1,6-octadiene, 1,7-octadiene, noridene ethylidene, norbornene vinyl, di-cyclopentadiene, 7-methyl-1,6-octadiene, 4-ethylidene-8-methyl-1,7-nonadiene, and 5,9-dimethyl-1,4,8-decatriene; aromatic vinyl compounds such as mono- or poly-alkyl-styrenes (including styrene, o-methyl-styrene, m-methyl-styrene, p-methyl-styrene, o, p-dimethyl-styrene, o-ethyl-styrene, m -ethyl-styrene and p-ethyl-styrene), and derivatives containing a functional group, such as methoxy-styrene, ethoxy-styrene, vinyl benzoic acid, vinyl methyl benzoate, benzyl vinyl acetate, hydroxy styrene, o-chloro-styrene , p-chloro-styrene, divinyl benzene, 3-phenyl-propene, 4-phenyl-propene and α-methyl-styrene, vinyl chloride, 1,2-difluoro-ethylene, 1,2-dichloro-ethylene, tetrafluoro- ethylene, and 3,3,3-trifluor-1-propene, as long as the monomer is polymerizable under the conditions employed. Preferred monomers or mixtures of monomers for use in combination with at least one CSA include here ethylene; propylene; mixtures of ethylene with one or more monomers selected from the group consisting of propylene, 1-butene, 1-hexene, 4-methyl-1-pentene, 1-octene, and styrene; and mixtures of ethylene, propylene and a conjugated or unconjugated diene. Catalysts and chain exchange agents
[0047] [0047] Catalysts and catalyst precursors suitable for use in the present invention include metal complexes as disclosed in WO 2005/090426, in particular those disclosed starting on page 20, line 30 through page 53, line 20, which is incorporated herein by reference. Suitable catalysts are also disclosed in US 2006/0199930, US 2007/0167578, US 2008/0311812, US 7,355,089 B2, or WO 2009/012215, which are incorporated herein by reference with respect to catalysts.
[0048] [0048] Particularly preferred catalysts are those of the following formula: 2
[0049] [0049] Preferably, such complexes correspond to the formula:
[0050] [0050] Preferred examples of metal complexes of the above formula include the following compounds:
[0051] [0051] The compounds of the formula are especially preferred:
[0052] [0052] Other suitable metal complexes are those of the formula:
[0053] [0053] The preceding polyvalent Lewis base complexes are conveniently prepared by standard ligand exchange and metallization procedures involving a Group 4 metal source and the neutral polyfunctional ligand source. In addition, complexes can also be prepared by means of a hydrocarbilization and amide elimination process starting from the corresponding Group 4 metal tetra-amide and a hydrocarbilizing agent, such as trimethyl aluminum. Other techniques can also be used. These complexes are known from the disclosures of, among others, U.S. Patent Nos. 6,320,005, 6,103,657, 6,953,764 and from international publications No. WO 02/38628 and WO 03/40195.
[0054] [0054] Suitable co-catalysts are those disclosed in WO 2005/090426, in particular, those disclosed on page 54, line 1 through page 60, line 12, which is incorporated herein by reference.
[0055] [0055] Suitable chain exchange agents include those disclosed in WO 2005/090426, in particular, those disclosed on page 19, line 21 through page 20, line 12, which is incorporated herein by reference. Particularly preferred chain exchange agents are dialkyl zinc compounds. Block composite polymer product
[0056] [0056] Using the present process, the new polymers of block composites are quickly prepared. Preferably, the composite block polymers comprise propylene, 1-butene or 4-methyl-1-pentene and one or more comonomers. Preferably, the block polymers of the block composites comprise, in polymerized form, propylene and ethylene and / or one or more comonomers of C4-20 α-olefins, and / or one or more additional copolymerizable comonomers or they comprise 4-methyl -1-pentene and ethylene and / or one or more C4-20 α-olefin comonomers, or they comprise 1-butene and ethylene, propylene and / or one or more C4-20 α-olefin comonomers and / or one or more additional copolymerizable comonomers. Additional comonomers are selected from diolefins, cyclic olefins, and cyclic diolefins, halogenated vinyl compounds, and aromatic vinylidene compounds.
[0057] [0057] One can measure the comonomer content in the resulting composite block polymers using any appropriate technique, preferring techniques based on nuclear magnetic resonance (NMR) spectroscopy. It is very desirable that some or all of the polymeric blocks comprise amorphous or relatively amorphous polymers such as copolymers of propylene, 1-butene or 4-methyl-1-pentene and a comonomer, especially random copolymers of propylene, 1-butene or 4-methyl -1-pentene with ethylene, and any remaining polymeric blocks (hard segments), if any, comprise predominantly propylene, 1-butene or 4-methyl-1-pentene in polymerized form. Preferably, such segments are very crystalline or specific stereo polypropylene, polybutene or poly (4-methyl-1-pentene), especially isotactic homopolymers.
[0058] [0058] Still preferably, the block copolymers of the invention comprise 10 to 90 percent relatively hard or crystalline segments, preferably 5 to 50 percent and 90 to 10 percent amorphous or relatively amorphous segments (soft segments) . Within the soft segments, the molar percentage of comonomer can vary from 5 to 90 mole percent, preferably from 10 to 60 mole percent. In the case where the comonomer is ethylene, it is preferably present in an amount of 10% by weight to 75% by weight, preferably from 10% by weight to 70% by weight, or from 10 to 70 mol%, more preferably from 30 mol% to 75 mol percent, and most preferably 33 to 65 mol percent. Block composites can have from 5% by weight to 50% by weight of hard blocks and from 95% by weight to 50% by weight of soft blocks.
[0059] [0059] Preferably, the copolymers comprise hard segments that are 80% by weight to 100% by weight of propylene. The hard segments can be more than 90% by weight, preferably more than 95% by weight and more preferably more than 98% by weight of propylene.
[0060] [0060] Composite polymers in blocks can be differentiated from conventional random copolymers, physical mixtures of polymers, and from conventional block copolymers prepared via sequential addition of monomer. Block composites can be differentiated from random copolymers by characteristics such as higher melting temperatures for a comparable amount of comonomer, block index and block composite index, as described below; of a physical mixture for characteristics such as block index, block composite index, better tensile strength, improved fracture resistance, finer morphology, improved optics, and better impact resistance at lower temperature; of block copolymers prepared by sequential addition of monomer by molecular weight distribution, rheology, shear decrease, rheology ratio, and the fact that there is block polydispersity.
[0061] [0061] In some embodiments, the block composites of the invention have a block compound index (BCI), defined below, which is greater than zero, but less than about 0.4 or about 0.1 to about of 0.3. In other incorporations, BCI is greater than about 0.4 and even about 1.0. In addition, BCI can be in the range of about 0.4 to about 0.7, about 0.5 to about 0.7, or about 0.6 to about 0.9. In some incorporations, BCI is in the range of about 0.3 to about 0.9, from about 0.3 to about 0.8, or from about 0.3 to about 0.7, of about 0.3 to about 0.6, about 0.3 to about 0.5, or about 0.3 to about 0.4. In other embodiments, BCI is in the range of about 0.4 to about 1.0, about 0.5 to about 1.0, or about 0.6 to about 1.0, about from 0.7 to about 1.0, from about 0.8 to about 1.0, or from about 0.9 to about 1.0.
[0062] [0062] Block composites preferably have a Tm greater than 100 ° C, preferably greater than 120 ° C, and more preferably greater than 125 ° C. Preferably, the MFR of the block composite is from 0.1 to 1000 dg / min, more preferably from 0.1 to 50 dg / min and more preferably from 0.1 to 30 dg / min.
[0063] [0063] Block composites preferably have domains in the dispersed phase that are less than 300 nm, preferably less than 200 nm, more preferably less than 100 nm; the block composite can have domains of 0.05 mm at 300 nm, 0.1 mm at 100 nm or 0.5 mm at 100 nm.
[0064] [0064] Other desirable compositions according to the present invention are elastomeric copolymers in blocks of propylene, 1-butene or 4-methyl-1-pentene with ethylene, and optionally one or more α-olefins or diene monomers. Preferred α-olefins for use in this embodiment of the present invention are designated by the formula CH2 = CHR *, where R * is a linear or branched alkyl group of 1 to 12 carbon atoms. Examples of suitable α-olefins include, but are not limited to, isobutylene, 1-butene, 1-pentene, 1-hexene, 4-methyl-1-pentene (when copolymerized with propylene), and 1-octene. Dienes suitable for use in the preparation of such polymers, especially polymers of the EPDM type in multiblocks include conjugated and unconjugated, normal or branched chain, cyclic or polycyclic dienes containing from 4 to 20 carbon atoms. Preferred dienes include 1,4-pentadiene, 1,4-hexadiene, 5-ethylidene-2-norbornene, di-cyclopentadiene, cyclohexadiene, and 5-butylidene-2-norbornene. A particularly preferred diene is 5-ethylidene-2-norbornene. The resulting product may comprise segments of isotactic homopolymer alternating with segments of elastomeric copolymer, prepared at the site during polymerization. Preferably, the product may comprise only the elastomeric block copolymer of propylene, 1-butene or 4-methyl-1-pentene with one or more comonomers, especially ethylene.
[0065] [0065] Since polymers containing diene contain alternating segments or blocks containing greater or lesser amounts of diene (including no amount) and a-olefin (including none), the total amount of diene and a-olefin can be reduced without loss subsequent polymeric properties. That is, as the diene and a-olefin monomers are preferably incorporated into one type of polymer block rather than uniformly or randomly throughout the polymer, they are used more efficiently and subsequently the polymer crosslinking density can be better controlled . Such crosslinkable elastomers and cured products have advantageous properties, including greater tensile strength and better elastic recovery.
[0066] [0066] Even more preferably, the block composites of this embodiment of the invention have a weight average molecular weight (Mw) of 10,000 to about 2,500,000, preferably from 35,000 to about 1,000,000 and more preferably from 50,000 to about 300,000 , preferably from 50,000 to about 200,000.
[0067] [0067] The polymers of the invention can be diluted in oil with up to 95% by weight of oil, with from 5 to about 95 percent, preferably from 20 to 80 percent, more preferably from 30 to 70 percent of an oil of processing, based on the total weight of the composition. Suitable oils include any oil that is conventionally used in the preparation of diluted EPDM rubber formulations. Examples include both naphthenic and paraffinic oils, with paraffinic oils being preferred.
[0068] [0068] Additional components of the present formulations usefully employed in accordance with the present invention include various other ingredients in amounts that do not detract from the properties of the resulting composition. These ingredients include, but are not limited to, activators such as calcium or magnesium oxide; fatty acids such as stearic acid and salts thereof; fillers and reinforcers such as calcium or magnesium carbonate, silica, and aluminum silicates; plasticizers such as dialkyl esters of dicarboxylic acids; antidegraders; emollients; waxes; and pigments. Preparation of polymeric mixtures
[0069] [0069] The ingredients of the polymeric mixtures, i.e. the block composite, polyolefins and optional additives can be combined or mixed using methods known to a person of ordinary skill in the art, preferably methods that can provide a substantially homogeneous distribution of the polyolefin and / or additives in the ethylene / α-olefin interpolymer. Non-limiting examples of suitable mixing methods include melt mixing, solvent mixing, extrusion, and the like.
[0070] [0070] Suitable polyolefins include, but are not limited to, polyethylene, such as LLDPE, HDPE, LDPE or random ethylene interpolymers; polypropylenes, such as iPP, PP homopolymer and RCPs; and olefinic block copolymers. Block olefinic copolymers comprise polymerized units of ethylene and a-olefin, and are characterized by an average block index greater than zero and up to about 1.0 and by a molecular weight distribution, Mw / Mn, greater than about 1.3. Block olefinic copolymers can also comprise polymerized units of ethylene and a-olefin, in which the average block index is greater than zero, but less than about 0.5 and by a greater molecular weight distribution, Mw / Mn, greater that about 1.3. Preferably, the olefinic block copolymer is a linear multi-block copolymer with at least three blocks. Also preferably, the ethylene content in the interpolymer is at least about 50 mole percent. These copolymers are described in and can be produced via polymerization techniques illustrated, for example, in U.S. Patent No. 7,608,668 B2, which is incorporated herein by reference. Another type of block olefinic copolymers that can be used are those referred to as "mesophase separated". The narrowest dimension of a domain, such as perpendicular to the lamella plane, is generally greater than about 40 nm in separate block copolymers for the mesophase of the present invention. Examples of these interpolymers can be found, for example, in international publications No. WO / 2009/097560, WO / 2009/097565, WO / 2009/097525, WO / 2009/097529, and WO / 2009/097535, all of which here they are incorporated by reference. The polyolefin can be present in an amount of 0-100 phr.
[0071] [0071] In some embodiments, the ingredients of the polymeric mixtures are mixed melted by a method described by Guerin et al., In U.S. Patent No. 4,152,189. First, all solvents, if any, are removed from the ingredients by heating them to an appropriate elevated temperature of about 100 ° C to about 200 ° C or from about 150 ° C to about 175 ° C at a pressure of about from 667 Pa (5 torr) to about 1333 Pa (10 torr). Next, the ingredients are weighed in a container in the desired proportions and the polymeric mixture is formed by heating the contents of the container to a stirred melting state.
[0072] [0072] In other embodiments, the ingredients of the polymeric mixtures are processed using solvent mixing. First, the ingredients of the desired polymeric mixture are dissolved in an appropriate solvent and then the mixture is composed or combined. Then, the solvent is removed to provide the polymeric mixture.
[0073] [0073] In additional incorporations, physical mixing devices that provide dispersive mixing, distributive mixing, or a combination of dispersive and distributive mixing may be useful in the preparation of homogeneous mixtures. Both batch methods and continuous physical mixing methods can be used. Non-limiting examples of batch methods include those methods using BRABENDER® mixing equipment (for example, BRABENDER PREP CENTER®, obtainable from CW, Brabender Instruments, Inc., South Hackensack, NJ) or internal mixing equipment or BANBURY® laminator (obtainable from Farrel Company, Ansonia, Conn.). Non-limiting examples of continuous methods include single screw extrusion, double screw extrusion, disk extrusion, reciprocating single screw extrusion, and single screw extrusion. In some embodiments, additives can be added to an extruder through a feed funnel or feed throat during the extrusion of the ethylene / a-olefin interpolymer, polyolefin or polymeric mixture. The mixing or composition of polymers by extrusion has been described in C. Rauwendaal, "Polymer Extrusion", Hanser Publishers, New York, NY, pages 322334 (1986), which is incorporated herein by reference. When one or more additives are required in the polymeric mixtures, the desired amounts of the additives can be added in one filler or in multiple fillers to the ethylene / α-olefin interpolymer, polyolefin or polymeric mixture. In addition, the addition can occur in any order. In some embodiments, first, the additives are added and mixed or combined with the ethylene / α-olefin interpolymer and then the additive-containing interpolymer is mixed with the polyolefin. In other embodiments, first, the additives are added and mixed or combined with the polyolefin and then the polyolefin containing additives is mixed with the ethylene / α-olefin interpolymer. In additional incorporations, the ethylene / α-olefin interpolymer is first mixed with the polyolefin and then the additives are mixed with the polymeric mixture. Polymeric mixtures can also be prepared in the manufacturing equipment as dry mixes (no pre-composition is required).
[0074] [0074] Alternatively, standard mixtures containing high concentrations of the additives can be used. In general, standard mixtures can be prepared by mixing the ethylene / a-olefin interpolymer, polyolefin or polymeric mixture with high concentrations of additives. Standard mixtures can have additive concentrations of about 1 to about 50% by weight, about 1 to about 40% by weight, about 1 to about 30% by weight, or about 1 to 20% by weight of the total weight of the polymer mixture. The standard mixtures can then be added to the polymeric mixtures in a certain amount to provide the desired concentrations of additives in the final products. In some embodiments, the standard mixture contains a slip agent, a non-stick agent, a plasticizer, an antioxidant, a UV stabilizer, a dye or pigment, a filler, a lubricant, an anti-condensation agent, a flow aid, a coupling agent, crosslinking agent, nucleating agent, surfactant, solvent, flame retardant, antistatic agent, or a combination thereof. In other embodiments, the standard mixture contains a glidant, a non-stick agent or a combination thereof. In another embodiment, the standard mixture contains a sliding agent.
[0075] Preferably, the mixtures have a dispersed morphology with the narrowest dimension being less than 300 nm in width, diameter or height, preferably less than 200 nm, more preferably less than 100 nm; morphologies can also be from 1 nm to 300 nm, from 10 nm to 200 nm or from 20 nm to 100 nm.
[0076] [0076] The mixtures can comprise 100 parts of block composite, 50-150 phr of oil, 0-11 phr of polyolefin and 0-200 phr of load. The compression deformation of the mixtures can be 40% to 70%. Shore A can be 50 to 90.
[0077] [0077] Applications of polymeric mixtures
[0078] [0078] The polymeric mixtures disclosed here can be used to manufacture durable items for the markets: automotive, construction, medical, food and beverage, electrical, household articles, industrial machinery, and consumer. In some incorporations, polymeric mixtures are used to manufacture flexible durable parts or selected items from toys, suitcases, knobs and soft touch, bumper wear bands, floors, car floor mats, wheels, casters, feet furniture and appliances, labels, hydraulic seals, gaskets such as static and dynamic gaskets, automotive doors, bumper strip, grille components, oscillator panels, hoses, linings, office supplies, coatings, diaphragms, tubes, covers , tampons, injection pistons, distribution systems, kitchen utensils, footwear, shoe buffers and shoe soles. In other embodiments, polymeric mixtures can be used to manufacture durable articles or parts that require high tensile strength and low compression deformation. In additional incorporations, polymeric mixtures can be used to manufacture durable articles or parts that require a high upper service temperature and low modulus.
[0079] [0079] Polymeric mixtures can be used to prepare these durable parts or articles with known polymeric processes such as extrusion (for example, sheet extrusion and profile extrusion); molding (for example, injection molding, rotational molding, and blow molding); fiber spinning; and expanded film and cast film processes. In general, extrusion is a process by which a polymer is continuously driven along a spindle through regions of high temperature and pressure where it is melted and compacted, and finally forced through a matrix. The extruder can be a single-screw extruder, a multi-screw extruder, a disk extruder or a percussion plunger extruder. The matrix can be a film matrix, expanded film matrix, sheet matrix, pipe matrix, pipe matrix or profile extrusion matrix. Polymer extrusion has been described in C. Rauwendaal, "Polymer Extrusion", Hanser Publishers, New York, NY, pages 322-334 (1986), and in MJ Stevens, "Extruder Principals and Operation", Elsevier Applied Science Publishers, New York, NY (1985), both of which are incorporated herein by reference.
[0080] [0080] Injection molding is also widely used to manufacture a variety of plastic parts for various applications. In general, injection molding is a process by which a polymer is melted and injected at high pressure into a mold, which is the reverse of the desired shape to form parts of the desired size and shape. The mold can be made with metal such as steel and aluminum. Polymer injection molding has been described in Beaumont et al., "Successful Injection Molding: Process, Design, and Simulation", Hanser Gardner Publications, Cincinnati, Ohio (2002), which is incorporated herein entirely by reference.
[0081] [0081] In general, molding is a process by which a polymer is melted and taken into a mold, which is the reverse of the desired shape to form parts of the desired size and shape. Molding can be pressure-free or pressure-assisted. Polymers molding is described in Hans-Georg Elias "Na Introduction to Plastics", Wiley-VHC, Weinhei, Germany, pp. 161-165 (2003), which is incorporated by reference.
[0082] [0082] The following examples are presented to illustrate embodiments of the invention. All numerical values are approximate. When numerical ranges are given, it should be understood that incorporations outside the declared ranges may still be within the scope of the invention. Specific details described in each example should not be construed as necessary features of the invention.
[0083] [0083] Polymerization methods
[0084] [0084] Appropriate processes useful for producing the block composites of the invention can be found, for example, in U.S. Patent Application Publication No. 2008/0269412, published on October 30, 2008, which is incorporated herein by reference. In particular, polymerization is desirably carried out as a continuous polymerization, preferably a continuous polymerization in solution, in which the catalytic components, and optionally solvent, adjuvants, purgers, and polymerization aids are supplied continuously to one or more reactors or zones and the polymeric product continuously removed from them. Within the scope of the terms "continuous" or "continuously" when used in this context are those processes in which intermittent additions of reagents and removal of products occur at small regular or irregular intervals, so that, over time, the overall process is substantially continuous. In addition, as explained above, the exchange agent (s) can be added at any point during polymerization including in the first reactor or zone, at the outlet or just before the outlet of the first reactor, between the first reactor or zone and the second or any subsequent reactor or zone, or even only in the second or any subsequent reactor or zone. Due to the difference in monomers, temperatures, pressures or other difference in polymerization conditions between at least two of the reactors or zones connected in series, polymeric segments of different composition such as comonomer content, crystallinity, density are formed in the different reactors or zones. , tacticity, regularity, or other chemical or physical difference, within the same molecule. The size of each segment or block is determined by continuous polymer reaction conditions, and preferably it is a very likely distribution of polymer sizes.
[0085] [0085] Each reactor in series can be operated under conditions of high pressure polymerization, in solution, in semi-fluid paste (sludge), or in gas phase. In a polymerization in multiple zones, all zones operate in the same type of polymerization, such as in solution, in semi-fluid paste (sludge), or in gas phase, but in different process conditions. For a solution polymerization process, it is desirable to employ homogeneous dispersions of the catalytic components in a liquid diluent in which the polymer is soluble under the polymerization conditions employed. Such a process is disclosed, using extremely fine silica or similar dispersing agent to produce such a homogeneous catalytic dispersion in which normally the metal complex or co-catalyst is only slightly soluble, in US-A-5,783,512. Usually, a high pressure process is performed at temperatures from 100 ° C to 400 ° C and at pressures above 50 MPa (500 bar). A semi-fluid slurry (sludge) process typically uses an inert diluting hydrocarbon and temperatures from 0 ° C to a temperature just below the temperature at which the resulting polymer becomes substantially soluble in the inert polymerization medium. In a semi-fluid slurry (sludge) polymerization the preferred temperatures are 30 ° C, preferably 60 ° C to 115 ° C, preferably up to 100 ° C. Typically, pressures range from atmospheric (100 kPa) to 3.4 MPa (500 psi).
[0086] [0086] In all of the above processes, conditions of continuous or substantially continuous polymerization are preferably employed. The use of such polymerization conditions in especially continuous solution polymerization processes allows the use of high reactor temperatures which results in the economical production of the present block copolymers in high yields and efficiencies.
[0087] [0087] The catalyst can be prepared as a homogeneous composition by adding the necessary metal complex or multiple complexes in a solvent in which the polymerization will be carried out or in a diluent compatible with the final reagent mixture. The desired activator or co-catalyst and, optionally, the exchange agent, can be combined with the catalytic composition before, simultaneously with, or after combining the catalyst with the monomers to be polymerized and any additional reaction diluent.
[0088] [0088] At all times, the individual ingredients, as well as any active catalyst composition, must be protected from oxygen, moisture and other catalyst poisons. Therefore, the components of catalyst, exchange agent and activated catalysts should be prepared and stored in an atmosphere free of oxygen and moisture, preferably in dry, inert air such as nitrogen.
[0089] [0089] Without limiting the scope of the invention in any way, a means of carrying out such a polymerization process is as follows. In one or more circulation reactors or a well-stirred tank operating under solution polymerization conditions, the monomers to be polymerized are continuously introduced together with any solvent or diluent in a part of the reactor. The reactor contains a relatively homogeneous liquid phase composed substantially of monomers together with any solvent or diluent and dissolved polymer. Preferred solvents include C4-10 hydrocarbons or mixtures thereof, especially alkanes such as hexane or mixture of alkanes, as well as one or more of the monomers employed in the polymerization. Examples of suitable circulation reactors and a variety of operating conditions suitable for use with them, including the use of multiple circulation reactors, operating in series, are found in US Patent Nos. 5,977,251, 6,319,989 and 6,683,149 .
[0090] [0090] Catalyst together with co-catalyst and optionally chain exchange agent are introduced continuously or intermittently into the liquid reactor phase or any recycled portion thereof at least in one place. The reactor temperature and pressure can be controlled by adjusting the solvent / monomer ratio, the catalyst addition rate, as well as by using cooling or heating coils, liners or both. The rate of polymerization is controlled by the rate of addition of catalyst. The content of a given monomer in the polymeric product is influenced by the ratio of monomers in the reactor, which is controlled by manipulating the respective feed rates of these components to the reactor. The molecular weight of the polymeric product is optionally controlled by controlling other polymerization variables such as temperature, monomer concentration, or by the aforementioned chain exchange agent, or a chain terminating agent such as hydrogen, as is well known in the art. A second reactor is connected to the reactor discharge, optionally by means of a conduit or other transfer medium, such that the reaction mixture prepared in the first reactor is discharged into the second reactor without substantial termination of polymer growth. Between the first and second reactors, a differential is established in at least one process condition. Preferably for use in forming a copolymer of two or more monomers, the difference is the presence or absence of one or more comonomers or a difference in monomer concentration. Additional reactors can also be provided, each arranged similarly to the second reactor in the series. At the outlet of the last reactor in the series, the effluent is contacted with a catalyst extinguishing agent such as water, water vapor or an alcohol with a coupling agent.
[0091] [0091] The resulting polymeric product is recovered by eliminating the volatile components of the reagent mixture such as residual monomers or diluent under reduced pressure, and, if necessary, performing additional devolatilization in equipment such as a devolatilization extruder. In a continuous process the average residence time of the catalyst and polymer in the reactor is generally from 5 minutes to 8 hours, and preferably from 10 minutes to 6 hours.
[0092] [0092] Alternatively, the previous polymerization can be carried out in a continuous flow reactor with a monomer, catalyst, exchange agent, temperature or other gradient established between different zones or regions of the same, optionally, accompanied by separate addition of catalysts and / or chain exchange agent, and operating under adiabatic or non-adiabatic polymerization conditions.
[0093] [0093] The catalytic composition can also be prepared and used as a heterogeneous catalyst by adsorbing the indispensable components in an inert organic or inorganic particulate solid, as discussed above. In a preferred embodiment, a heterogeneous catalyst is prepared by co-precipitating the metal complex and the reaction product of an inert inorganic compound and an activator containing active hydrogen, especially the reaction product of a tri (C1-4 alkyl) compound. aluminum and an ammonium salt of an aryl tris hydroxy borate (pentafluorophenyl), such as an ammonium salt of (4-hydroxy-3,5-ditherciobutyl-phenyl) tris (pentafluorophenyl). When prepared in a heterogeneous form or supported on support, the catalytic composition can be used in a polymerization in semi-fluid paste (sludge) or in gas phase. As a practical limitation, polymerization in slurry (sludge) occurs in liquid diluents in which the polymeric product is substantially insoluble. Preferably, the diluent for sludge polymerization is one or more hydrocarbons with less than 5 carbon atoms. If desired, saturated hydrocarbons such as ethane, propane or butane may be used in whole or in part as the diluent. When with a solution polymerization, the a-olefin comonomer or a mixture of different a-olefin monomers can be used in whole or as part as the diluent. Most preferably at least a major part of the diluent comprises the monomer or monomers of α-olefins to be polymerized. Testing methods
[0094] [0094] The overall composition of each resin is determined by DSC, NMR, GPC, DMS, and TEM morphology. In addition, xylene fractionation or HTLC fractionation can be used to estimate block copolymer production. Differential scanning calorimetry (DSC)
[0095] [0095] Differential scanning calorimetry (DSC) is performed on a TA Instruments DS1000 QC equipped with an RSC cooling accessory and an automatic sample collector. A flow of nitrogen purge gas of 50 mL / min is used. The sample is pressed into a thin film and melted in the press at about 190 ° C and then cooled in air at room temperature (25 ° C). Then 3-10 mg of material is cut, weighed accurately, and placed in a light aluminum pan (ca 50 mg), which is then closed and set. The thermal behavior of the sample is investigated with the following temperature profile: the sample is quickly heated to 190 ° C and isothermally maintained for 3 minutes in order to remove any previous thermal history. The sample is then cooled to -90 ° C at a cooling rate of 10 ° C / min and maintained at -90 ° C for 3 minutes. The sample is then heated to 150 ° C at a heating rate of 10 ° C / min. The cooling and second heating curves are recorded. Nuclear magnetic resonance (NMR) of C Sample preparation
[0096] [0096] Samples were prepared by adding approximately 2.7 g of 50/50 mixture of tetrachloroethane-d2 / ortho-dichloro-benzene which is 0.025M in chromium acetyl acetonate (relaxation agent) to 0.21 g of sample in a 10 mm NMR tube. The samples are dissolved and homogenized by heating the tube and its contents to 150 ° C. Data acquisition parameters
[0097] [0097] The data are collected using a 400 MHz Bruker spectrometer equipped with a Bruker high temperature double cryogenic probe DUL. Data is acquired using 320 transients per data file, a 7.3 s relaxation delay (6 s delay and 1.3 s acquisition time), 90 degree turn angles, and inverse restricted decoupling with a temperature sample temperature of 125 ° C. All measurements are obtained from rotation samples in locked mode. The samples are homogenized immediately before insertion into the heated NMR sample changer (130 ° C), and remain in the probe for 15 minutes to achieve thermal equilibrium before data acquisition. Gel permeation chromatography (GPC)
[0098] [0098] The gel permeation chromatographic system consists of one of a Model PL-210 or Model PL-220 instrument from Polymer Laboratories. The carousel compartment and the column compartment are operated at 140 ° C. Three 10 Mixed-B columns from Polymer Laboratories are used. The solvent is 1,2,4-trichlorobenzene. The samples are prepared in a concentration of 0.1 g of polymer in 50 ml of solvent containing 200 ppm of butylated hydroxytoluene (BHT). The samples are prepared by gently shaking for 2 hours at 160 ° C. The injection volume used is 100 µL and the flow rate is 1.0 mL / min.
[0099] [0099] The calibration of the GPC column set is performed with 21 polystyrene standards of narrow molecular weight distribution, with molecular weights ranging from 580 to 8,400,000 g / mol, arranged in 6 "cocktail" mixtures with at least one ten of separation between individual molecular weights. The standards were purchased from Polymer Laboratories (Shropshire, UK). Polystyrene standards are prepared in 0.025 g in 50 mL of solvent for molecular weights greater than or equal to 1,000,000, and 0.05 g in 50 mL of solvent for molecular weights less than 1,000,000. The polystyrene standards are dissolved at 80 ° C with gentle agitation for 30 minutes. Mixtures of narrow patterns are used first, and in descending order from the highest molecular weight component, to minimize degradation. The peak molecular weights of polystyrene standard are converted to molecular weights of polyethylene using the following equation (described in Williams and Ward, J. Polym. Sci., Polym. Let., 6, 621 (1968)): Mpolethylene 0, 645 (Mpolietireno).
[0100] [0100] Calculations of equivalent molecular weight of polypropylene are performed using the Viscotek TriSEC software version 3.0. Elution fractionation with rapid temperature gradient (F-TREF)
[0101] [0101] In F-TREF analysis, the composition to be analyzed is dissolved in ortho-dichloro-benzene and crystallization is allowed in a column containing an inert support (stainless steel granule), slightly reducing the temperature to 30 ° C ( at a preferred rate of 0.4 ° C / min). The column is equipped with an infrared detector. Then, an F-TREF chromatogram curve is generated by eluting the crystallized polymer sample from the column by slightly increasing the temperature of the elution solvent (o-dichloro-benzene) from 30 to 140 ° C (at a preferred rate of 1.5 ° C / min). High temperature liquid chromatography (HTLC)
[0102] [0102] HTLC is performed according to the methods disclosed in US Patent Application Publication No. 2010-0093964 and US Patent Application No. 12/643111, filed on December 21, 2009, both of which are here incorporate by reference. The samples are analyzed using the methodology described below.
[0103] [0103] Waters GPCV2000 high temperature SEC chromatograph was reconfigured to develop HT-2DLC instrumentation. Two LC-20AD pumps from Shimadzu were connected to the injector valve through a binary mixer. The first dimension HPLC column (D1) was connected between the injector and a 10 input switch valve (Valco Inc.). The second dimension SEC column (D2) was connected between the 10-inlet valve and IR (concentration and composition, IR (refractive index), and IR (intrinsic viscosity) LS detectors) (Varian Inc.). and IV were detectors built into GPVC2000. The IR5 detector was supplied by PolymerChar, Valencia, Spain.
[0104] [0104] Columns: Column D1 was a high temperature graphite column HYPERCARB (2.1 x 100 mm) purchased from Thermo Scientific. Column D2 was a PLRapid-H column purchased from Varian (10 x 100 mm).
[0105] [0105] Reagents: HPLC grade trichlorobenzene (TCB) was purchased from Fischer Scientific. Dean, 1-decanol and 2,6-ditherciobutyl-4-methyl-phenol (IONOL) were purchased from Aldrich.
[0106] [0106] Sample preparation: 0.01-0.15 g of polyolefin sample was placed in a small 10 ml vial of Waters automatic sample collector. Then, 7 ml of 1-decanol or decane with 200 ppm IONOL was added to the small flask. After spraying helium in the small sample vial for about 1 minute, the small sample vial was placed on a heated shaker with a temperature set at 160 ° C. Dissolution was carried out by shaking the small flask at 160 ° C for 2 hours. Then, the small vial was transferred by injection to the automatic sample collector. Note that the actual volume of the solution was greater than 7 mL due to the thermal expansion of the solvent.
[0107] 1. 490 min: fluxo= 0,01 min; //Manter a taxa de fluxo constante de 0,01 mL/min de 0-490 min. 2. 491 min: fluxo= 0,20 min; //Aumentar a taxa de fluxo para 0,20 mL/min. 3. 492 min: % de B= 100; // Aumentar a composição de fase móvel para 100% de TCB. 4. 502 min: % de B= 0; // Lavar a coluna usando 2 mL de TCB. Etapas de equilíbrio:5. 503 min: % de B= 0; // Mudar a composição de fase móvel para 100% de 1-decanol ou decano6. 513 min: % de B= 0; // Equilibrar a coluna usando 2 mL de eluente fraco.7. 514 min: fluxo= 0,2 mL/min; // Manter o fluxo constante de 0,2 mL/min de 491-514 min.8. 515 min: fluxo= 0,01 mL/min; // Diminuir a taxa de fluxo para 0,01 mL/min.[0107] HT-2DLC: The flow rate of D1 was 0.01 ml / min. The composition of the mobile phase was 100% of the weak eluent (1-decanol or decane) for the first 10 minutes of the run. Then, the composition was increased to 60% strong eluent (TCB) in 489 min. The data were collected for 489 min as the duration of the crude chromatogram. The 10-inlet valve was changed every three minutes producing 489/3 = 163 SEC chromatograms. A post-operation gradient after the data acquisition time of 489 min was used to clean and balance the column for the following operation: Cleaning steps: 1. 490 min: flow = 0.01 min; // Keep the flow rate constant at 0.01 mL / min from 0-490 min. 2. 491 min: flow = 0.20 min; // Increase the flow rate to 0.20 mL / min. 3. 492 min:% B = 100; // Increase the mobile phase composition to 100% TCB. 4. 502 min:% B = 0; // Wash the column using 2 mL of TCB. Balance steps: 5. 503 min:% B = 0; // Change the mobile phase composition to 100% 1-decanol or decane 6. 513 min:% B = 0; // Balance the column using 2 ml of weak eluent. 7. 514 min: flow = 0.2 ml / min; // Maintain a constant flow of 0.2 mL / min for 491-514 min. 8. 515 min: flow = 0.01 ml / min; // Decrease the flow rate to 0.01 mL / min.
[0108] [0108] After step 8, the flow rate and mobile phase composition were the same as the initial conditions of the operating gradient.
[0109] [0109] The flow rate of D2 was 2.51 ml / min. Two 60 µL rings were installed on the 10-port switch valve. 30 µL of column eluent D1 was loaded onto the SEC column with each valve switch.
[0110] [0110] The IR, LS15 (15 ° light scattering signal), LS90 (90 ° light scattering signal), and IR (intrinsic viscosity) signals were collected by EZChrom via an analog conversion box for digital SS420X. The chromatograms were exported in ASCII format and imported in a MATLAB domestic software for data reduction. An appropriate calibration curve of polymer composition and retention volume, of polymers which are similar in nature to the hard and soft blocks contained in the composite blocks under analysis, is used. Calibration polymers must be narrow in composition (both in molecular weight and in chemical composition) and cover a reasonable range of molecular weights to cover the composition of interest during analysis. The analysis of the raw data was calculated as follows: the HLPC chromatogram of the first dimension was reconstructed by plotting the IR signal of each cut (from the total chromatogram of the SEC of the cut IR) as a function of the elution volume. The IR against D1 elution volume was normalized by total IR signal to obtain the weight fraction graph against D1 elution volume. The methyl / IR measurement ratio of the reconstructed IR measurement and IR methyl chromatograms was obtained. The ratio was converted into composition using a calibration curve of% by weight of PP (per NMR) against methyl / measure obtained from SEC experiments. The Mw was obtained from the reconstructed IR and LS measurement chromatograms. The ratio was converted to Mw after calibration of both IR and LS detectors using a PE standard.
[0111] [0111] The percentage by weight of isolated PP is measured as the area corresponding to the hard block composition based on the isolated peak and retention volume determined by a composition calibration curve. Dynamic mechanical spectroscopy (DMS)
[0112] [0112] The dynamic-mechanical measures (loss and storage module against temperature) are measured in ARES from TA Instruments. Dynamic modulus measurements are performed in torsion on a solid bar of ca. 2 mm thick, 5 mm wide and approx. 10 mm in length. The data is recorded at a constant frequency of 10 rad / s and a heating / cooling rate of 5 ° C / min. Temperature scans are performed from -90 ° C to 190 ° C at 5 ° C / min. Transmission electron microscopy (TEM)
[0113] [0113] Polymer films are prepared by compression molding followed by quick quenching. The polymer is pre-melted at 190 ° C for 1 minute at 1000 psi and then pressed for 2 minutes at 500 psi and then quenched between chilled plates (15-20 ° C) for 2 minutes.
[0114] [0114] Compression-molded films are ground so that they can be collected close to the film core. The rectified samples are cold-polished before staining by removing sections of the blocks at -60 ° C to prevent improper splashing of dye from the elastomer phases. The cold-polished blocks are dyed with the vapor phase of an aqueous solution of 2% ruthenium tetroxide for 3 hours at room temperature. The dyeing solution is prepared by weighing 0.2 g of hydrated ruthenium (III) chloride (RuCl3.xH2O) in a glass bottle with a screw cap and adding 10 mL of 5.25% aqueous sodium hypochlorite solution to the bottle. The samples are placed in the glass bottle using a glass slide having double-sided tape. The slide is placed in the bottle to suspend the blocks about 1 inch above the dyeing solution. Sections approximately 90 nm thick are collected at room temperature using a diamond knife on a Leica EM UC6 microtome and placed on virgin 600 mesh TEM screens for observation.
[0115] [0115] Image collection - TEM images are collected on a JEOL JEM-1230 operated at an acceleration voltage of 100 kV and collected on Gatan-791 and 794 digital cameras. Scanning electron microscopy with backscattering (BS-SEM)
[0116] [0116] A small rectangular piece was cut in the center of each of the compression-molded plates so that sections could be collected parallel to the direction of injection molding in the core. The pieces were trimmed and cold-polished before dyeing by removing sections of the blocks at -120 ° C to prevent staining. The cold-polished blocks were colored with the vapor phase of an aqueous solution of ruthenium tetroxide for 40 minutes at room temperature. The dye solution was prepared by weighing 0.2 g of hydrated ruthenium (III) chloride (RUCI3.XH2O) in a screw-top glass bottle and adding 10 mL of 5.25% aqueous sodium hypochlorite solution to the bottle. The samples were placed in a glass bottle using a glass slide having a double-sided tape with the film side adhered to the tape to prevent over-staining of the outer surface. The slide was placed in the bottle in order to suspend the blocks about 1 inch above the dyeing solution. Approximately 300 nm sections were removed from the block phases at -120 ° C using a histology diamond knife on a Leica UCT microtome equipped with an FCS cryoscopic section chamber. Material was removed from the blocks until sections without fractures could be collected indicating that brittle and over-dyed regions were eliminated. The cryopolished blocks were subjected to cathodic sublimation with an iridium plasma using a K575X turbo cathodic sublimation coating machine for 20 seconds to make them conductors for electron microscopy.
[0117] [0117] Backscattered electronic images (BEI) were collected in an scanning electron microscope An FEI Nano 600 operated at an acceleration voltage of 10 kV, a working distance of 5 mm and a spot size of 5.0. The immersion mode with a solid state backscattering detector was used to capture BEI images of the core of the faces of cryopolished blocks. Analysis by fractionation of soluble xylene
[0118] [0118] A heavy amount of resin is dissolved in 200 ml of o-xylene under reflux conditions for 2 hours. Then, the solution is cooled in a water bath with a temperature controlled at 25 ° C to allow crystallization of the insoluble fraction in xylene (XI). When the solution cools and the insoluble fraction precipitates out of the solution, the separation of the xylene-soluble fraction (XS) from the xylene-insoluble fraction (XI) is carried out by filtration through a paper filter. The remaining o-xylene solution is evaporated from the filtrate. Both fractions XS and XI are dried in a vacuum oven at 100 ° C for 60 minutes and then weighed. Alternatively, if the temperature of crystallization of the soft-block polymer solution is greater than the ambient temperature, the fractionation step can be performed at a temperature of 10-20 ° C above the temperature of crystallization of soft blocks, but below the temperature of crystallization of hard blocks. The separation temperature can be determined by measures of TREF and CRYSTAF described in the reference "TREF and CRYSTAF Technologies for Polymer Characterization", "Encyclopedia of Analitical Chemistry, published in 2000, pages 8074-8094. This fractionation can be carried out in a laboratory heated filtration and dissolution apparatus or in a fractionation instrument such as PREPARATORY mc 2 (obtainable from PolymerChar, Valencia, Spain). Toughness
[0119] [0119] Shore A hardness was measured by ASTM D2240. This test method allows for hardness measurements based on the initial notch or notch after a specified period of time, or both. In this case, a specified time of 10 seconds was used. Traction test
[0120] [0120] Traction data is measured using ASTM D 1708 which is a micro-traction method with a traction rate of 5 inch / min in the flow direction of the compression molded plate. Compression deformation
[0121] [0121] Deformation by compression was measured according to ASTM D 395 at room temperature, 40 ° C and 70 ° C. The sample was prepared by stacking round disks with a diameter of 25.4 mm cut from compression-molded plates with a thickness of 0.125 "until a total thickness of 12.7 mm was reached EXAMPLES General examples
[0122] [0122] Catalyst-1 ([[rel-2 ', 2 "' - [(1R, 2R) -1,2-cyclohexanediyl bis (methylene oxy-KO)] bis [3- (9H-carbazol-9 -yl) -5-methyl [1,1'-biphenyl] -2-olate-KO]] (2-) dimethyl-hafnium) and co-catalyst 1, a mixture of di di (C14-18 alkyl) salts ) tetrakis borate ammonium (penta-fluorine phenyl), prepared by reaction with a long-chain trialkylamine (ARMEEN ™ M2HT, obtainable from Akzo-Nobel, Inc.), HCl and Li [B (C6F5) 4], substantially such as disclosed in USP 5,919,983, Example 2, are purchased from Boulder Scientific and used without further purification CSA-1 (diethyl zinc or TEN) and modified methyl aluminoxane (MMAO) were purchased from Akzo Nobel and used without further purification. solvent for polymerization reactions is a hydrocarbon mixture (SBP 100/140) obtainable from Shell Chemical Company and purified through 13-X molecular sieve beds before use.
[0123] [0123] All examples except A1, E1, U1 and Y1 have an iPP hard block. Series B to D have a soft block of semi-crystalline ethylene / propylene containing 60-65% by weight of C2 while series F to H have a soft block of amorphous ethylene / propylene containing 40% by weight of C2. With an increase in the alphabetical order, the weight fraction and length of the iPP hard block are independently controlled from 30 to 60 percent by weight, increasing the production rate in the reactor (in this case, reactor 2).
[0124] [0124] Examples V1, W1, X1 and Y1, Z1, AA are similar in design to B, C, D, but prepared under different reactor conditions. Later, the effect of greater conversion of propylene and reactor temperature will be discussed.
[0125] [0125] All examples are run without hydrogen. The concentration of CSA in Reactor 1 for all examples is 153 mmol / kg. The concentration of MMAO in Reactor 2 for all examples is 6 mmol / kg. Samples A1-D1
[0126] [0126] Inventive propylene / ethylene copolymers were prepared using two continuous agitated tank reactors (CSTR) connected in series. Each reactor is hydraulically filled and adjusted to operate under steady state conditions. Sample A1 is prepared by flowing monomers, solvent, catalyst-1, co-catalyst-1, and CSA-1 for the first reactor according to the process conditions outlined in Table 1. To prepare sample B1, the contents of the first reactor described in Table 1A flowed to a second reactor in series. More catalyst-1 and co-catalyst-1 were added to the second reactor, as well as a small amount of MMAO as a purger. Samples C1 and D1 were prepared by controlling the conditions of the two reactors as described in Tables 1A and 1B. Samples E1-AB1
[0127] [0127] Each set of samples from F1-H1, V1-X1, Y1-AB1 diblocks was prepared as above for Examples B1-D1, but according to the process conditions outlined in Tables 1A and 1B. For each set, a first reactor product (E1, U1, Y1) is prepared for the first block composition. Table 1A. First reactor process conditions for producing copolymers in B1-D1, F1-H1, V1-X1, Z1-AB1 diblocks
[0128] [0129] Two to four grams of polymer are dissolved in 200 ml of o-xylene under reflux conditions for 2 hours. Then, the solution is cooled in a 25 ° C temperature-controlled water bath to allow crystallization of the insoluble fraction in xylene. When the solution cools and the insoluble fraction precipitates out of the solution, the separation of the xylene-soluble fraction from the xylene-insoluble fraction is carried out by filtration through a paper filter. The remaining o-xylene solution is evaporated from the filtrate. Both fractions XS (soluble in xylene) and XI (insoluble in xylene) are dried in a vacuum oven at 100 ° C for 60 minutes and then weighed.
[0129] [0130] For each set of samples, the number "2" is given to the fraction insoluble in xylene and the number "3" to the fraction soluble in xylene. For example, sample B1 is subjected to the extraction procedure to produce sample B2 (the fraction insoluble in xylene) and sample B3 (the fraction soluble in xylene).
[0130] [0131] Table 2 shows the analytical results for series B1 through AB1. The molecular weight distributions of the polymers are relatively narrow with Mw / Mn ranging from 2.1-2.3 for samples B1 to D1, and 2.2-2.8 for samples F1 through H1. For samples V1 through AB1, Mw / Mn ranges from 2.1-2.5. For the corresponding insoluble and soluble xylene fractions for each of the series (designated by the number 2 or 3), Mw / Mn ranges from 2.0 to 2.8.
[0131] [0132] Table 2 also shows the percentage by weight of isolated PP identified by separation by high temperature liquid chromatography. The amount of PP isolated indicates the amount of PP that is not incorporated in the block copolymer. The weight fraction of isolated PP and the weight fraction of soluble in xylene subtracted from 1 can be related to the polymer yield in diblocks produced.
[0132] [0133] Table 3 shows the analytical results for the B1, C1, D1 and F1, G1, H1 series.
[0133] [0134] The molecular weight distributions of the polymers are relatively narrow with Mw / Mn ranging from 2.1-2.3 for samples B to D, and varying from 2.2-2.8 for samples F to H. Table 2 - Analytical summary of Examples B1-AB1 and fractions
[0134] [0135] Figure 1 shows the DSC melting curve for sample B1. The peak at 130 ° C corresponds to the "hard" polymer of iPP and the broadest peak at 30 ° C corresponds to the "soft" polymer of EP; the glass transition temperature at -46 ° C also corresponds to the "soft" polymer of EP containing 64% by weight of ethylene (C2).
[0135] [0136] Figure 2 shows the DSC melting curve for the F1 sample. The peak at 135 ° C corresponds to the "hard" polymer of iPP and the absence of crystallinity below room temperature corresponds to the "soft" polymer of EP containing 40% by weight of C2. At -50 ° C Tg confirms the presence of the "soft" EP polymer containing 40% by weight of C2.
[0136] [0137] The presence of block copolymer can alter the crystallization characteristics of a polymeric chain if measured by TREF or solution fractionation. Figure 3 compares the TREF profiles of sample B1 to D1. The TREF profiles are consistent with the DSC results, showing a very crystalline fraction (elution above 40 ° C) and a soluble low crystallinity fraction (remaining material that elutes below 40 ° C). The elution temperature increases with the amount of iPP present. An EP block attached to an iPP block can improve the solubility of chains in the solvent and / or interfere with the crystallization of the iPP block.
[0137] [0138] Figures 4 and 5 show the corresponding DSC curves of the fractions of B2, B3 and F2, F3.
[0138] [0139] In this analysis, the fraction soluble in xylene is an estimate of the amount of non-crystallizable soft polymer. For the xylene-soluble fractions of B1-D1 samples, the percentage by weight of ethylene is between 61 and 65% by weight of ethylene without detection of residual isotactic propylene. The DSC of the xylene-soluble fraction confirms that no high crystallinity polypropylene is present.
[0139] [0140] On the other hand, the insoluble fraction (designated as number 2) may contain an amount of iPP polymer and iPP / EP diblocks. Since the crystallization and elution of the polymer chain are governed by its longer crystallizable propylene sequence, the diblock copolymer will precipitate along with the iPP polymer. This is verified by the NMR and DSC analyzes that show an appreciable, and on the other hand inexplicable, amount of ethylene present in the "insoluble" fraction. In a typical separation of a mixture of iPP and EP rubber it will be completely separated by this analysis. The fact that there is additional ethylene present in the insoluble fraction, confirms that a fraction of diblocks is present. By calculating the total mass balance of monomer between the fractions, one can estimate the composite composite index.
[0140] [0141] Another indication of the presence of diblocks is the increase in the molecular weight of the insoluble fractions with the increase in the amount of iPP. Since the polymer chains are coupled in a coordinated manner during the transition from the first reactor to the second reactor, the molecular weight of the polymer is expected to increase. Table 3 shows that the molecular weight of the soluble fractions remains relatively constant (120 140 kg / mol). This is expected because the reactor conditions to prepare the EP soft block have not changed from series to series. However, the molecular weight of insoluble fractions increases with the increase in the production rate of reactor 2 to create longer iPP blocks. Calculation of the composite composite index
[0141] [0142] The inventive examples show that insoluble fractions contain an appreciable amount of ethylene which, on the contrary, would not be present if the polymer were simply a mixture of iPP homopolymer and EP copolymer. To explain this "extra ethylene", a mass balance can be performed to calculate a block composite index of the amount of insoluble and soluble xylene fractions and the percentage by weight of ethylene present in each of the fractions.
[0142] [0143] The sum of the percentages by weight of ethylene for each fraction according to Equation 1 results in the percentage by weight of total ethylene (in the polymer). This mass balance equation can also be used to determine the amount of each component in a binary mixture or extended to a quaternary mixture, or even to a mixture of "n" components. % by weight of C2total winsoluble (% by weight of C2insoluble) + wsoluble (% by weight of C2soluble) Equation 1
[0143] [0144] Applying Equations 2 to 4, the amount of the soft block (providing the source of extra ethylene) present in the insoluble fraction is calculated. By substituting the weight percentage of C2 of the insoluble fraction in the first member of equation 2, one can calculate the weight percentage of hard iPP and the weight percentage of soft EP using Equations 3 and 4. Note that the percentage in ethylene weight in the soft EP is adjusted to be equal to the weight percentage of ethylene in the xylene-soluble fraction. The weight percentage of ethylene in the iPP block is set to zero or if otherwise known from your DSC melting point or other composition measure, the value can be put in place. % by weight of C2total or insoluble in xylene hard wipp (% by weight of C2iPP) + soft wEP (% by weight of C2EP soft) Equation 2
[0144] [0145] After explaining the "additional" ethylene present in the insoluble fraction, the only way to have an EP copolymer present in the insoluble fraction, the polymeric EO chain must be linked to an iPP polymer block (or differently it the fraction soluble in xylene would have been extracted). Therefore, when the iPP block crystallizes, it prevents the EP block from solubilizing.
[0145] [0146] To calculate the composite index in blocks, the relative quantity of each block must be taken into account. To approach this, the ratio between the soft EO and iPP duct is used. The ratio of the soft EP polymer to hard iPP polymer can be calculated using Equation 2 of the total ethylene mass balance measured in the polymer. Alternatively, it can also be calculated from the mass balance of monomer and comonomer consumption during polymerization. Table 3 refers to the calculated ratio of iPP and EP present in the copolymer in diblocks for all series. The weight fraction of the hard iPP and the weight fraction of the soft EP are calculated using Equation 2 and it is assumed that the hard iPP does not contain any ethylene. The ethylene weight percentage of the soft EP is the amount of ethylene present in the xylene-soluble fraction. Table 3 - Block composite index calculations for Examples B1 to AB3
[0146] [0148] For example, if an inventive iPP / EP polymer contains a total of 47% by weight of C2 and is prepared under the conditions to produce a soft EP polymer with 67% by weight of C2 and an iPP homopolymer containing zero of ethylene, the amount of soft EP and iPP duct will be 70% by weight and 30% by weight, respectively (calculated using Equations 3 and 4). If the percentage of EP is 70% by weight and that of iPP is 30% by weight, the relative ratio of the EP: iPP blocks can be expressed as 2.33: 1.
[0147] [0149] Therefore, if a person skilled in the art, performs a polymer extraction with xylene and recover 40% by weight of insoluble and 60% by weight of soluble, this would be an unexpected result and would lead to the conclusion that a fraction of the block copolymer inventive was present. If the ethylene content of the insoluble fraction is subsequently measured to be 25% by weight of C2, Equations 2 to 4 can be resolved to account for this additional ethylene and result in 37.3% by weight of EP soft polymer and 62.7% by weight of iPP hard polymer present in the insoluble fraction.
[0148] [0150] Since the insoluble fraction contains 37.3% by weight of EP copolymer, it would bind to an additional 16% by weight of iPP polymer based on the EP: iPP block ratio of 2.33: 1. This leads to an estimated amount of diblocks in the insoluble fraction of 53.3% by weight. For all polymer (unfractionated), the composition is described as having 21.3% by weight of iPP / EP diblocks, 18.7% by weight of iPP polymer, and 60% by weight of EP polymer . As the compositions of these polymers are new, the term block composite index (BCI) is defined here as being equal to the percentage of diblocks weight divided by 100% (ie, weight fraction). The value of the composite block index can vary from 0 to 1, where 1 would be equal to 100% of inventive diblocks and zero would be for a material such as a traditional mixture or random copolymer. For the example described above, the block composite index for the block composite is 0.213. For the insoluble fraction, the BCI is 0, 533, and for the soluble fraction the BCI is designated by the value zero.
[0149] [0151] Depending on the estimates made of the total polymeric composition and the error in the analytical measures that are used to estimate the composition of the hard and soft blocks, a relative error of 5 to 10% in the computed value of the composite composite index is possible. Such estimates include the percentage by weight of C2 in the iPP hard block measured from the DSC melting point, NMR analysis, or process conditions, the average percentage by weight of C2 in the estimated soft block of the composition of the soluble in xylene, or by NMR, or by soft block DSC melting point (if detected). But the calculation of the global block composite index is reasonably responsible for the unexpected amount of "additional" ethylene present in the insoluble fraction, the only way to have an EP copolymer present in the insoluble fraction, the EP polymer chain must bond to an iPP polymer block (or else it would have been extracted in the xylene-soluble fraction).
[0150] [0152] More specifically, Example H1 contains a total of 14.8% by weight of C2 and the percentage by weight of C2 in xylene soluble (H3) was measured to be 38.1% by weight (as a representation of composition of EP soft polymer) and an iPP homopolymer containing zero ethylene, the amount of EP soft and iPP hard is 61% by weight and 39% by weight, respectively (calculated using Equations 3 and 4). If the percentage of EP is 61% by weight and that of iPP is 39% by weight, the relative ratio of EP: iPP blocks can be expressed as 1.56: 1.
[0151] [0153] After extraction of polymer H1 with xylene, 60.6% by weight of insoluble polymer (H2) and 39.4% by weight of soluble polymer (B3) are recovered. Subsequently, the insoluble fraction B2 is measured to have 4.4% by weight of C2, Equations 2 to 4 can be solved to be responsible for this additional ethylene and result in 11.5% by weight of EP soft polymer and 88.5% by weight of iPP hard polymer.
[0152] [0154] Since the insoluble fraction contains 11.5% by weight of EP copolymer, it would bind to an additional 7.35% by weight of iPP polymer based on the EP: iPP block ratio of 1, 56: 1. This leads to an estimated amount of diblocks in the insoluble fraction of 29.6% by weight. For all polymer (unfractionated), the composition is described as having 18% by weight of iPP / EP diblocks, 42.6% by weight of iPP polymer, and 39.4% by weight of EP polymer . For example H1 described above, the block composite index for the block composite is 0.18. For the insoluble fraction (H2), the BCI is 0.29, and for the soluble fraction the BCI is designated by the value zero.
[0153] [0155] Table 3 and figure 6 show the composite indices in blocks for the series B1 to AB1. For the B1, C1, and D1 series, the BCI values are, respectively, 0, 16, 0.17, and 0.22. For the xylene-insoluble fractions associated with B2, C2, and D2, the BCI values are 0.42, 0.34, and 0.35, respectively. For the F1, G1, and H1 series, the BCI values are 0.10, 0.5, and 0.18, respectively. For the associated xylene-insoluble fractions, fractions F2, G2, and H2, the BCI values are, respectively, 0.29, 0.29, and 0.29.
[0154] [0156] Table 3 and figure 7 show for the V1, W1, X1 series that increasing the conversion of propylene reactor from 90 to 95% increases the BCI from 0.03 to 0.09 to result in BCI values of 0 , 18, 0.24, and 0.25.
[0155] [0157] Table 3 and figure 7 show that for the Z1, AA1, AB1 series, the increase in the reactor temperature from 90 to 120 ° C resulted in BCI values of 0.12, 0.18, and 0.24 , respectively. Dynamic mechanical analysis
[0156] [0158] Figure 8 shows the dynamic-mechanical properties of samples B1 to D1; the values of G 'and tangent of delta against temperature are shown. By increasing the quantity of iPP, the G 'module increases and the high temperature plateau extends. Sample D1 shows that the module decreases with increasing temperature to about 140 ° C before completely softening after its melting transition.
[0157] [0159] For each sample, the delta tangent curve shows a characteristic Tg between -48 to -50 ° C for the ethylene / propylene copolymer and a second Tg in about 0 ° C of isotactic polypropylene. Above 50 ° C, the delta tangent response remains constant until melting begins and the modulus decreases rapidly.
[0158] [0160] Figure 9 shows the dynamic-mechanical properties of samples F1 to H1; the values of G 'and tangent of delta against temperature are shown. Similar to the case of 65% by weight of C2, increasing the amount of iPP, the G 'module increases and the high temperature plateau extends. Sample H1 shows that the module decreases with increasing temperature to about 140 ° C before completely softening after its melting transition.
[0159] [0161] For these examples, the delta tangent curves also show a characteristic Tg between -48 to -50 ° C for the ethylene / propylene copolymer and a second Tg at about 0 ° C for isotactic polypropylene. Above 50 ° C, the delta tangent response remains constant for samples G1 and H1 until fusion starts and the modulus decreases rapidly. Discussion of morphology
[0160] [0162] The samples are analyzed by TEM to observe the influence of the diblocks on the total morphology of iPP / EPR rubber. Figure 10 shows the TEM image of the ProFax Ultra SG853 impact copolymer (Lyondell Basell Polyolefins) consisting of a continuous phase of isotactic PP and a rubber phase of 17% by weight, containing 58% by weight of C2 in the rubber.
[0161] [0163] The TEM micrograph shown on a 5 µm scale shows large RPE domains ranging from 2 to 5 µm.
[0162] [0164] At 1 mm magnification, the EPR domain has a heterogeneous distribution of ethylene and propylene composition as shown by the light and dark colored domains present within the particle. This is a classic example of a dispersed morphology comprising two phases (iPP and EP rubber) that are immiscible with each other.
[0163] [0165] Figure 11 shows TEM micrographs of films molded by compression of B1, C1, and D1, in the scales of 2, 1, and 0.5 µm. In complete contrast to the image of the impact copolymer, all three polymers show a finer dispersion of particles with very small domains. For B1, a continuous phase of EPR is observed together with elongated PP domains of the order of 80-100 nm in width. For C1, there was a mixed continuity between the phases of iPP and EPR with domain sizes in the range of 200-250 nm. For D1, a continuous phase of PP is observed together with spherical and some elongated EPR domains of size 150-300 nm.
[0164] [0166] Figure 12 shows TEM micrographs of films molded by compression of F1, G1, and H1, in the scales of 2, 1, and 0.5 µm. In complete contrast to the image of the impact copolymer, all three polymers show a finer dispersion of particles with very small domains. For F1, a continuous phase of EPR is observed together with elongated PP domains of the order of 200-400 nm in width. For G1, there was a mixed continuity between the phases of iPP and EPR with domain sizes on the order of 200-300 nm. For H1, a continuous phase of PP is observed together with spherical and some elongated EPR domains of size 150-300 nm.
[0165] [0167] It is surprising to observe such small and well-dispersed domains shown in these polymer micrographs that have been molded by compression from pellets. Usually, to obtain fine morphology (not close to the scales shown here), specialized composition and extrusion histories are required. Even if size scales are approximated using blending, the morphologies may not be stable; grain growth and phase agglomeration can occur with thermal aging, shown by the impact copolymer in which the rubber domains are elongated and some of them connected to each other by the chains.
[0166] [0168] The morphology of the copolymer in diblocks was further investigated by examining the polymeric fractions obtained from xylene fractionation. As explained above, the insoluble fraction contains diblocks of iPP / EP and free iPP homopolymer while the soluble fraction contains non-crystallizable EP rubber.
[0167] [0169] Figure 13 shows TEM micrographs of the insoluble fractions of B1 and D1 and also the soluble fraction of B1. Notably, the morphology observed in the insoluble fraction is even finer and more distinct from that observed in the whole polymer. The insoluble fraction of B1 shows a mixture of spherical and spiral EPR domains, in the 50 nm width scale. The insoluble fraction of D1 shows small spherical domains that also have a diameter of about 50 nm. For reference, the xylene-soluble fraction of B1 shows the typical granular lamellar structure that is expected from an EP elastomer containing 65% by weight of C2. Again, the morphologies of the insoluble fractions are distinct and appear to be separated by microphases.
[0168] [0170] It is interesting to observe the TEM micrographs of the insoluble fraction of B1, figure 15, with those of a sPP / EP / sPP triblock containing 71% by weight of sPP, such as that shown in Figure 7 of Macromolecules, volume 38 , no. 3, page 857, 2005. In this figure, the sPP / EP / sPP triblock was produced via anionic polymerization and the micrograph is a film annealed at 160 ° C for about a week. The sample was annealed on melting for a total of 8 days - the first 4 days at 200 ° C to erase any previous thermal history and then the additional 4 days at a final temperature of 160 ° C. High vacuum furnaces (<10 mbar) were used to prevent degradation by oxidation. Melt morphology was preserved by quickly tempering the samples after annealing. The authors of the article associated the microstructure separated by phases to cylinders packed in a hexagonal manner (figure 14). Soft compound studies
[0169] [0171] Example 1 is prepared by mixing 80% by weight of Example C1 with 20% by weight of HYDROBRITE ™ 550 paraffinic oil in a Haake vat at 190 ° C. Comparative Example 1 is prepared by mixing 30% by weight of NORDEL ™ 3722 EPDM copolymer (Mw = 120000 g / mol, Mw / Mn = 4.7) (The Dow Chemical Company), 40% by weight of hPP 5E16S ( MFR = 35, Mw = 181,000 g / mol, Mw / Mn = 3.4) (The Dow Chemical Company), and 20% by weight of HYDROBRITE ™ 550 paraffinic oil in a Haake vat.
[0170] [0172] Example 2 is prepared by mixing 60% by weight of Example C1 with 40% by weight of HYDROBRITE ™ 550 paraffinic oil (Sonneborn Inc.) in a Haake vat at 190 ° C. Comparative Example D is prepared by mixing 53.6% by weight of NORDEL ™ 3722 EPDM copolymer (Mw = 120000 g / mol, Mw / Mn = 4.7) (The Dow Chemical Company), 26.4% by weight hPP 5E16S (MFR = 35, Mw = 181,000 g / mol, Mw / Mn = 3.4) (The Dow Chemical Company), and 20% by weight of HYDROBRITE ™ 550 paraffinic oil in a Haake vat. Prepare Comparative Example E by mixing 30% by weight of NORDEL ™ 3722 EPDM copolymer (Mw = 120000 g / mol, Mw / Mn = 4.7) (The Dow Chemical Company), 30% by weight of hPP 5E16S ( MFR = 35, Mw = 181,000 g / mol, Mw / Mn = 3.4) (The Dow Chemical Company), and 40% by weight of HYDROBRITE ™ 550 paraffinic oil in a Haake vat.
[0171] [0173] Figures 15-18 show SEM images of Comparative Example 1 and Example 1 on a 200 µm scale, on a 100 µm scale, on a 10 µm scale and on a 5 µm scale, respectively.
[0172] [0174] In Figure 15, it can be seen that Comparative Example 1 shows a continuous matrix of iPP having very thick dispersed EPDM elastomer domains ranging from 1 to more than 300 µm in length. On the other hand, at the same magnification, the phases observed for Example 1 were very small.
[0173] [0175] At larger magnifications, it appears that Example 1 comprises a more continuous iPP matrix phase with more dispersed lower density EP fractions. In some areas, the EP fractions appeared to be encapsulated by iPP, in other places, they appeared more interconnected.
[0174] [0176] Larger magnification images, shown in Figure 19 on the 4 µm scale, show more clearly some of the spherical lower density EP fractions that appeared encapsulated by a more continuous iPP matrix. The smaller EP domains ranged from 100 nm to 300 nm in diameter.
[0175] [0177] Figure 20 shows the comparison of tensile properties of the control sample against the inventive sample 1 (using the polymer of Example C1 with 20% oil). It is evident that the inventive sample is superior, not only in its tensile properties, but also in compression strain shown in Table 4. Comparative A is an ENGAGE ™ 8150 ethylene / octene elastomer (density = 0.865 g / cm3 and MI = 0.5) (The Dow Chemical Company) mixed with 20% by weight of oil. Comparative B is an INFUSE ™ OBC 9007 ethylene / octene block copolymer (density = 0.866 g / cm3 and MI = 0.5) (The Dow Chemical Company) mixed with 20% by weight of oil.
[0176] [0178] Example 2 shows a Shore A 62 compound that exhibits less compression strain than the control sample and significantly greater final elongation. Table 4 - Mechanical properties of compounds
[0177] [0179] Although the invention has been described with respect to a limited number of embodiments, the specific characteristics of an embodiment should not be attributed to other embodiments of the invention. No single embodiment represents all aspects of the invention. In some embodiments, the compositions or methods may include numerous compounds or steps not mentioned here. In other embodiments, the compositions or methods do not include, or are substantially free of any compounds or steps not listed here. From the described incorporations there are variations and modifications. Finally, any number disclosed herein must be constructed to mean approximate, regardless of whether the term "about" or "approximately" is used in the description of the number. The appended claims are intended to cover all those modifications and variations as falling within the scope of the invention.

权利要求:
Claims (4)
[0001]
Elastomer composition, characterized by the fact that it comprises: (a) a block composite; (b) an oil and, optionally; (c) a charge; or (d) a polyolefin; and the composition has Shore A from 50 to 90, The block composite being polymers comprising a soft copolymer, a hard polymer and a block copolymer having a soft segment and a hard segment that form chemically distinct blocks bonded end-to-end with respect to the polymerized ethylene functionality in the block copolymer , the hard segment of the block copolymer having the same composition as the hard polymer in the block composite and the soft segment of the block copolymer having the same composition as that of the soft copolymer of the block composite, and the elastomer composition having a thin dispersed phase morphology having a more restricted dimension of less than 100 nm.
[0002]
Composition according to claim 1, characterized in that the block copolymers are diblock copolymers having isotactic polypropylene blocks and ethylene / propylene blocks.
[0003]
Composition according to claim 2, characterized in that the ethylene / propylene blocks comprise more than or equal to 10 mol% and less than 70 mol% of ethylene.
[0004]
Composition, according to claim 2, characterized by the fact that the isotactic polypropylene blocks are

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引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

---

US4045517A|1975-11-24|1977-08-30|Rohm And Haas Company|Polyacrylic hot melt adhesives|

---

JPS6325621B2|1980-07-17|1988-05-26|Mitsubishi Petrochemical Co|

---

US4491652A|1981-05-13|1985-01-01|Uniroyal, Inc.|Sequentially prepared thermoplastic elastomer and method of preparing same|

---

DE3784235T2|1986-12-26|1993-09-09|Mitsubishi Petrochemical Co|METHOD FOR PRODUCING CROSSLINKED BLOCK COPOLYMERS OF OLEFINS.|

---

JPH0517640A|1990-11-16|1993-01-26|Mitsubishi Petrochem Co Ltd|Thermoplastic elastomer composition|

---

US5763534A|1994-08-25|1998-06-09|Solvay Engineered Polymers|Thermoplastic polypropylene blends with mixtures of ethylene/butene and ethylene/octene copolymer elastomers|

---

JPH08208941A|1995-02-02|1996-08-13|Showa Denko Kk|Propylene resin composition and molding made therefrom|

---

JPH08208944A|1995-02-02|1996-08-13|Showa Denko Kk|Multilayer laminate|

---

EP0889912B1|1996-03-27|2000-07-12|The Dow Chemical Company|Highly soluble olefin polymerization catalyst activator|

---

US5977251A|1996-04-01|1999-11-02|The Dow Chemical Company|Non-adiabatic olefin solution polymerization|

---

US5783512A|1996-12-18|1998-07-21|The Dow Chemical Company|Catalyst component dispersion comprising an ionic compound and solid addition polymerization catalysts containing the same|

---

US6103657A|1997-07-02|2000-08-15|Union Carbide Chemicals & Plastics Technology Corporation|Catalyst for the production of olefin polymers|

---

US6319989B1|1997-07-21|2001-11-20|The Dow Chemical Company|Broad MWD, compositionally uniform ethylene interpolymer compositions, process for making the same and article made therefrom|

---

JP2003517487A|1997-09-19|2003-05-27|ザダウケミカルカンパニー|Ethylene interpolymer compositions exhibiting narrow MWD with optimized composition, methods of making the same, and articles made therefrom|

---

WO2002046249A2|2000-11-07|2002-06-13|Symyx Technologies, Inc.|Methods of copolymerizing ethylene and isobutylene and polymers made thereby|

---

JP2002194098A|2000-12-25|2002-07-10|Mitsubishi Chemicals Corp|Cover for storing air-bag|

---

US6960635B2|2001-11-06|2005-11-01|Dow Global Technologies Inc.|Isotactic propylene copolymers, their preparation and use|

---

US6953764B2|2003-05-02|2005-10-11|Dow Global Technologies Inc.|High activity olefin polymerization catalyst and process|

---

US7608668B2|2004-03-17|2009-10-27|Dow Global Technologies Inc.|Ethylene/α-olefins block interpolymers|

---

US7858706B2|2004-03-17|2010-12-28|Dow Global Technologies Inc.|Catalyst composition comprising shuttling agent for ethylene multi-block copolymer formation|

---

US7355089B2|2004-03-17|2008-04-08|Dow Global Technologies Inc.|Compositions of ethylene/α-olefin multi-block interpolymer for elastic films and laminates|

---

US7714071B2|2004-03-17|2010-05-11|Dow Global Technologies Inc.|Polymer blends from interpolymers of ethylene/α-olefins and flexible molded articles made therefrom|

---

AR048104A1|2004-03-17|2006-03-29|Dow Global Technologies Inc|CATALYZING COMPOSITION THAT INCLUDES A LINK AGENT FOR THE FORMATION OF OLEFIN'S TOP COPOLYMERS IN MULTIPLE BLOCKS|

---

JP5165183B2|2004-07-22|2013-03-21|三菱化学株式会社|Olefin-based thermoplastic elastomer composition and method for producing the same|

---

JP6138408B2|2005-09-15|2017-05-31|ダウ グローバル テクノロジーズ エルエルシー|Catalytic olefin block copolymer with controlled block sequence distribution|

---

BRPI0812643B1|2007-07-13|2019-01-15|Dow Global Technologies Inc|ethylene / α-olefin interpolymer|

---

EP2170993B1|2007-07-13|2019-05-15|Dow Global Technologies LLC|Catalytic olefin block copolymers with controlled block sequence distribution and at least one low crystallinity hard block|

---

JP5259384B2|2007-12-26|2013-08-07|三井化学株式会社|Thermoplastic elastomer composition, method for producing the same, and molded article|

---

US8106139B2|2008-01-30|2012-01-31|Dow Global Technologies Llc|Propylene/alpha-olefin block interpolymers|

---

EP2238184B1|2008-01-30|2019-01-16|Dow Global Technologies LLC|Propylene/ -olefin block interpolymers|

---

EP2238185B1|2008-01-30|2019-01-16|Dow Global Technologies LLC|Butene/ -olefin block interpolymers|

---

BRPI0905769B1|2008-01-30|2019-11-05|Dow Global Technologies Inc|ethylene / α-olefin block interpolymer composition, article and process for polymerizing one or more addition polymerizable monomers|

---

CN101983214A|2008-01-30|2011-03-02|陶氏环球技术公司|Ethylene/alpha-olefin block interpolymers|

---

CN101981074A|2008-01-30|2011-02-23|陶氏环球技术公司|Butene/alpha-olefin block interpolymers|

---

ES2628340T3|2008-10-06|2017-08-02|Dow Global Technologies Llc|Polyolefin Polymers Chromatography|

---

DE202008014218U1|2008-10-24|2010-03-04|Rehau Ag + Co|Thermoplastic elastomers|

---

US8716400B2|2009-10-02|2014-05-06|Dow Global Technologies Llc|Block composites and impact modified compositions|JP5964833B2|2011-08-11|2016-08-03|住友化学株式会社|Process for producing olefin block polymer using group 4 transition metal complex|

---

WO2013090396A1|2011-12-14|2013-06-20|Dow Global Technologies Llc|Functionalized block composite and crystalline block composite compositions|

---

US9303156B2|2011-12-14|2016-04-05|Dow Global Technologies Llc|Functionalized block composite and crystalline block composite compositions as compatibilizers|

---

EP2831171B1|2012-03-30|2016-05-18|Dow Global Technologies LLC|Polyolefin elastomer formulations|

---

US9982122B2|2012-04-12|2018-05-29|Dow Global Technologies Llc|Polyolefin blend composition and articles made therefrom|

---

EP3058407B1|2013-10-18|2020-07-29|Dow Global Technologies LLC|Optical fiber cable components|

---

CA2927060C|2013-10-18|2021-03-30|Dow Global Technologies Llc|Optical fiber cable components|

---

KR101394119B1|2013-11-04|2014-05-14|화인케미칼 주식회사|Composition for 3d printer filament|

---

US20150204027A1|2014-01-22|2015-07-23|Dow Global Technologies Llc|Artificial turf filaments, and articles made therefrom|

---

KR20170018894A|2014-06-16|2017-02-20|다우 글로벌 테크놀로지스 엘엘씨|Acrylic composition with olefin block copolymer|

---

US10648750B2|2014-10-29|2020-05-12|Dow Global Technologies Llc|Olefin block composite thermally conductive materials|

---

US20190127890A1|2016-04-22|2019-05-02|Basell Poliolefine Italia S.R.L.|Propylene terpolymer for filament for 3d printer|

---

CN109071723B|2016-04-22|2020-12-29|巴塞尔聚烯烃意大利有限公司|Propylene-based filaments for three-dimensional printers|

---

WO2017206043A1|2016-05-31|2017-12-07|Dow Global Technologies Llc|Thermoplastic polyolefin blends including block composites as compatibilizers|

---

US10458576B2|2016-10-13|2019-10-29|Teknor Apex Company|Hose assembly with modified thermoplastic inner tube|

---

EP3395885B1|2017-04-27|2021-06-09|Sumitomo Chemical Company, Ltd|Propylene polymer composition|

法律状态:
2020-08-25| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|

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2020-09-24| B06U| Preliminary requirement: requests with searches performed by other patent offices: procedure suspended [chapter 6.21 patent gazette]|

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2021-01-12| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|

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2021-03-23| B16A| Patent or certificate of addition of invention granted|Free format text: PRAZO DE VALIDADE: 10 (DEZ) ANOS CONTADOS A PARTIR DE 23/03/2021, OBSERVADAS AS CONDICOES LEGAIS. |

优先权:

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申请号 | 申请日 | 专利标题

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US24816009P| true| 2009-10-02|2009-10-02|

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US61/248,160|2009-10-02|

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PCT/US2010/051159|WO2011041698A1|2009-10-02|2010-10-01|Block copolymers in soft compounds|

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