WO2015009474A1 - Compositions copolymères d'éthylène-propylène avec de longues séquences de méthylène - Google Patents

Compositions copolymères d'éthylène-propylène avec de longues séquences de méthylène Download PDF

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WO2015009474A1
WO2015009474A1 PCT/US2014/045542 US2014045542W WO2015009474A1 WO 2015009474 A1 WO2015009474 A1 WO 2015009474A1 US 2014045542 W US2014045542 W US 2014045542W WO 2015009474 A1 WO2015009474 A1 WO 2015009474A1
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ethylene
propylene copolymer
branched
branched ethylene
previous
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PCT/US2014/045542
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Mun Fu Tse
Jo Ann M. Canich
Charles J. Ruff
Daniel BILBAO
Carlos U. Degracia
Ian C. Stewart
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Exxonmobil Chemical Patents Inc.
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Priority to US14/895,807 priority Critical patent/US20160122452A1/en
Publication of WO2015009474A1 publication Critical patent/WO2015009474A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts
    • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
    • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
    • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
    • C08F4/62—Refractory metals or compounds thereof
    • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
    • C08F4/659—Component covered by group C08F4/64 containing a transition metal-carbon bond
    • C08F4/65908—Component covered by group C08F4/64 containing a transition metal-carbon bond in combination with an ionising compound other than alumoxane, e.g. (C6F5)4B-X+
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F255/00—Macromolecular compounds obtained by polymerising monomers on to polymers of hydrocarbons as defined in group C08F10/00
    • C08F255/02—Macromolecular compounds obtained by polymerising monomers on to polymers of hydrocarbons as defined in group C08F10/00 on to polymers of olefins having two or three carbon atoms
    • C08F255/04—Macromolecular compounds obtained by polymerising monomers on to polymers of hydrocarbons as defined in group C08F10/00 on to polymers of olefins having two or three carbon atoms on to ethene-propene copolymers
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F4/00—Polymerisation catalysts

Definitions

  • Branched ethylene-propylene copolymers with a high degree of branching (g' of less than 1) and having 50 to 55 weight percent ethylene content as measured by 13 C NMR are described.
  • the copolymers can be used as compatibilizers for polymer blends.
  • Alpha-olefins especially those containing 6 to 20 carbon atoms, have been used as intermediates in the manufacture of detergents or other types of commercial products. Such alpha-olefins have also been used as monomers, especially in linear low density polyethylene. Commercially produced alpha-olefins are typically made by oligomerizing ethylene. Longer chain alpha-olefins, such as vinyl-terminated polyethylenes are also known and can be useful as building blocks following functionalization or as macromonomers.
  • Branched amorphous ethylene-propylene oligomers and polymers, and compositions comprising such branched amorphous ethylene-propylene oligomers and polymers are described.
  • the branched ethylene-propylene copolymers include one or more of the following: at least 50% ethylene content by weight as determined by FTIR; a g' v i s of less than 0.98; a M w of 150,000 to 250,000; a methylene sequence length of 6 or greater as determined by 13 C NMR, wherein the percentage of sequences of the length of 6 or greater is more than 32%; and greater than 50% vinyl chain end functionality.
  • Processes for making the branched ethylene-propylene oligomers and polymers are described, wherein the processes comprise contacting ethylene and propylene with a catalyst system, comprising an activator and at least one metallocene.
  • Figure 1 provides mEPCs made by catalyst 1/activator 1 have much higher melting points than mEPCs made by catalyst 2/activator 2.
  • Figure 2 demonstrates that mEPCs made by catalyst 1/activator 1 have higher heats of fusion than mEPCs made by catalyst 2/activator 2.
  • Figure 4 (a-c) is a GPC-3D curve for sample 2 prepared with catalyst 1/activator
  • Figure 6 are representative stress-strain curves of mEPCs measured at room temperature and a pull rate of 5.08 cm/min.
  • Figure 7a provides Van Gurp-Palmen plots of mEPCs prepared with catalyst 1/activator 1.
  • Figure 7b provides Van Gurp-Palmen plots of mEPCs prepared with catalyst 2/activator 2.
  • Figure 8a provides the complex viscosity versus frequency of mEPCs prepared with catalyst 1/activator 1.
  • Figure 8b provides the complex viscosity versus frequency of mEPCs prepared with catalyst 2/activator 2.
  • Branched as used herein means a polyolefin having a g' v i s of 0.98 or less. These branched polyolefins having high amounts of allyl chain ends may find utility as macromonomers for the synthesis of polyolefins, such as linear low density polyethylene, block copolymers, and as additives, for example, as additives to, or blending agents in, lubricants, waxes, and adhesives.
  • the branched nature of these polyolefins may improve rheological properties in molten state and desired mechanical properties by allowing optimal thermoforming and molding at lower temperatures, thereby reducing energy consumption of the film forming process, as compared to linear polyolefin analogues. Additionally, the high amounts of allyl chain ends of these branched polyolefins provides a facile path to functionalization.
  • the functionalized branched polyolefins may be also useful as additives or blending agents.
  • the branched ethylene-propylene copolymers include one or more of the following: at least 50% ethylene content by weight as determined by FTIR; a g' v i s of less than 0.98; a M w of 150,000 to 250,000; a methylene sequence length of 6 or greater as determined by 13 C NMR, wherein the percentage of sequences of the length of 6 or greater is more than 32%; and greater than 50% vinyl chain end functionality.
  • the ethylene-propylene copolymer comprise ethylene derived units, as determined by FTIR, within the range of from 30 or 40 or 50 wt% to at least 55 or 60 or 65 wt% by weight of the copolymer, or alternatively the weight percent of ethylene in the ethylene-propylene copolymer is at least 50 wt%, more particularly from 50 wt% to 55 wt%, the remainder being propylene-derived units.
  • an "olefin,” alternatively referred to as “alkene,” is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond.
  • alkene is a linear, branched, or cyclic compound of carbon and hydrogen having at least one double bond.
  • olefin including, but not limited to ethylene and propylene
  • the olefin present in such polymer or copolymer is the polymerized form of the olefin.
  • a copolymer when a copolymer is said to have an "ethylene" content of 50 wt% to 55 wt%, it is understood that the mer unit in the copolymer is derived from ethylene in the polymerization reaction and said derived units are present at 50 wt% to 55 wt%, based upon the weight of the copolymer.
  • a "polymer” has two or more of the same or different mer units.
  • a “homopolymer” is a polymer having mer units that are the same.
  • a “copolymer” is a polymer having two or more mer units that are different from each other.
  • a “terpolymer” is a polymer having three mer units that are different from each other.
  • oligomer is typically a polymer having a low molecular weight (such an Mn of less than 25,000 g/mol, preferably less than 2,500 g/mol) or a low number of mer units (such as 75 mer units or less).
  • branched oligomer or branched polymer is defined as the polymer molecular architecture obtained when an oligomer (or a polymer) chain (also referred to as macromonomer) with reactive polymerizable chain ends is incorporated into another oligomer/polymer chain during the polymerization of the latter to form a structure comprising a backbone defined by one of the oligomer chains with branches of the other oligomer chains extending from the backbone.
  • a linear oligomer differs structurally from the branched oligomer because of lack of the extended side arms.
  • the oligomer with a reactive polymerizable chain end can be generated in-situ and incorporated into another growing chain to form a homogeneous branched oligomers in a single reactor.
  • a linear polymer has a branching index (g' v is) of 0.98 or more, preferably 0.99 or more, preferably 1.0 (1.0 being the theoretical limit of g' vjs ).
  • inventive ethylene-propylene polymers disclosed herein are branched, having a branching index (g' v i s ) °f l ess man 0.98 (preferably 0.95 or less, preferably 0.90 or less, even more preferably 0.85 or less).
  • inventive copolymers also have a methylene sequence length of 6 or greater as determined by 13 C NMR, wherein the percentage of sequences of the length of 6 or greater is more than 32%.
  • the heat of fusion of the ethylene-propylene copolymer has a heat of fusion (AH f ) of from 5 or 10 or 12 or 16 J/g to 30 or 40 or 50 J/g.
  • the inventive ethylene- propylene copolymer also have at least 50% allyl chain ends, relative to total unsaturated chain ends (preferably 60% or more, preferably 70% or more, preferably 75% or more, preferably 80% or more, preferably 90% or more, preferably 95% or more).
  • the ethylene-propylene copolymers described herein can also have one or more of the following characteristics.
  • the branched ethylene-propylene copolymers described herein have a Mw/Mn range of from 2.2 to 2.6. Preferably, the Mw/Mn is less than 2.4. Both Mn and Mw are determined using GPC-DRI.
  • the branched ethylene-propylene copolymers described herein have a Mooney viscosity (ML) ML (1 + 4) at 125°C of from 29 to 100 MU (preferably from 40 to 82; preferably from 50 to 68), where MU is Mooney Units.
  • the branched ethylene-propylene copolymers described herein have a Mooney large relaxation area (MLRA) of from 100 to 1000 (preferably from 175 to 610; preferably from 275 to 545; preferably from 325 to 530).
  • MLRA Mooney large relaxation area
  • the branched ethylene-propylene copolymers described herein have a melting point (Tm) within the range of from -30 or -20 or -10°C to 10 or 20 or 30 or 40°C.
  • the branched ethylene-polymer copolymers described herein have an elongation (break) of 150% or greater and/or a nomial stress range of from 0.22 MPa to 0.32 MPa at 50% strain and/or 0.15 MPa to 0.2 MPa at 150% strain, at a pull rate of 5.08 centimeters/minute.
  • the branched ethylene-propylene copolymers described herein have a phase angle of 50° at 8000 G*Pa and 25° at 500,000 G*Pa at 190°C.
  • the branched ethylene-propylene copolymers herein have a phase angle of 45° at 10,000 G*Pa and a range of 25° to 35° at 100,000 G*Pa at 190°C.
  • the branched ethylene-propylene copolymers herein have an average sequence length for methylene sequences two and longer of from 8 to 9.
  • the branched ethylene-propylene copolymers herein have an average sequence length for methylene sequences six and longer of from 12 to
  • the branched ethylene-propylene copolymers have an ri3 ⁇ 4 of from 2.7 to 2.8.
  • the branched polymers have 50% or greater allyl chain ends (preferably 60% or more, preferably 70% or more, preferably 80% or more, preferably 90% or more, preferably 95% or more).
  • Branched polymers generally have a chain end (or terminus) which is saturated and/or an unsaturated chain end.
  • the unsaturated chain end of the inventive polymers comprises "allyl chain ends.”
  • An allyl chain end is represented by the formula:
  • the unsaturated chain ends may be further characterized by using bromine electrometric titration, as described in ASTM D 1159.
  • the bromine number obtained is useful as a measure of the unsaturation present in the sample.
  • branched polyolefins have a bromine number which, upon complete hydrogenation, decreases by at least 50% (preferably by at least 75%).
  • the inventions described herein relate to branched ethylene-propylene polymers and polymerization processes to produce them, wherein the formation of polymers with an allyl chain end and reinsertion of oligomers with allyl chain ends into another oligomer take place in the same polymerization zone or in the same reactor.
  • a single catalyst system is used, more preferably two different metallocene catalysts are used in combination, and most preferably, two different metallocene catalysts wherein one is a symmetrical metallocene (meaning that both cyclopentadienyl groups are the same) and the other unsymmetrical (meaning that each of the two cyclopentadienyl groups are different).
  • the catalyst system is capable of producing an oligomer with allyl chain end and reinserting the oligomer into another oligomer to form a branched polymer.
  • Processes for making the branched ethylene- propylene oligomers and polymers are described, wherein the processes comprise contacting ethylene and propylene with a catalyst system, comprising an activator and at least one metallocene.
  • Suitable indenyl metallocene catalysts, activators and catalyst systems useful herein are those described herein below as well as those described in attorney docket number 2013EM185 filed concurrently herewith.
  • Suitable catalysts include, for example, rac-tetramethylenesilylene-bis(2,4,7- trimethylindenyl)hafnium (IV) dimethyl.
  • Suitable activators include, for example, dimethylanilinium tetrakisperfluoronaphthylborate.
  • Conversion is the amount of monomer and comonomers that are converted to polymer products, and is reported as weight percent and is calculated based on the polymer yield and the amount of monomer fed into the reactor.
  • Catalyst activity is a measure of amount of polymer product produced by unit weight of the catalyst in a given time period. For a continuous process, the catalyst activity is reported as the kilogram of polymer product (P) produced per kilogram of catalyst (cat) used (kgP/kgcat). In a batch process, catalyst activity is reported as the grams of polymer product produced per gram of catalyst and per hour (g P/g cat Hr).
  • temperatures and pressures suitable for commercial production of the branched ethylene-propylene polymers include a temperature greater than 35°C (preferably in the range of from 35 to 150°C, from 40 to 140°C, from 60 to 140°C, or from 80 to 130°C) and a pressure in the range of from 0.1 to 10 MPa (preferably from 0.5 to 6 MPa or from 1 to 4 MPa).
  • the processes described herein have a residence time suitable for commercial production of the branched ethylene-propylene polymers.
  • the residence time of the polymerization process is up to 300 minutes, preferably in the range of from 5 to 300 minutes, preferably from 10 to 250 minutes, preferably from 10 to 120 minutes, or preferably from 10 to 60 minutes.
  • long residence time may increase the monomer conversion, thereby increasing the oligomer concentration and decreasing the monomer concentration in a reactor. This will enhance the level of branching of the oligomer.
  • the residence time is used to control the branching level and to optimize the branching structures for specific end-uses.
  • the polymer product can be recovered from solution at the completion of the polymerization by any of the techniques well known in the art such as steam stripping followed by extrusion drying or by devolatilizing extrusion. Separated solvent/diluent and monomers can be recycled back in the reactor.
  • two different metallocene/activator systems rac- tetramethylenesilylene-bis(2,4,7-trimethylindenyl)hafnium (IV) dimethyl (catalyst 1)/ dimethylanilinium tetrakisperfluoronaphthylborate (activator 1) and bis(para- triethylsilylphenyl)methylene(2,7-di-tert-butyl-fluoren-9-yl)(cyclopentadienyl)hafnium(IV) dimethyl (catalyst 2)/dimethylanilinium tetrakisperfluorophenylborate (activator 2), were used to prepare ethylene-propylene copolymers.
  • the mEPC prepared with catalyst 1/activator 1 has, on average, longer methylene sequences based on 13 C NMR studies, leading to a melting point (T m ) of 30°C higher than the mEPC prepared with catalyst 2/activator 2.
  • the former copolymer also has better tensile properties, a higher melt strength and a higher degree of shear thinning due to the presence of branching, as demonstrated by Mooney viscosity, GPC-3D, and l H NMR.
  • the number of vinyl chain ends, vinylidene chain ends and vinylene chain ends is determined using NMR using deuterated tetrachloroethane as the solvent on an at least 250 MHz NMR spectrometer, and in selected cases, confirmed by 13 C NMR.
  • Proton NMR data was collected at either room temperature or 120°C (for purposes of the claims, 120°C shall be used) in a 5 mm probe using a Varian spectrometer with a ⁇ H frequency of at least 400 MHz. Data was recorded using a maximum pulse width of 45°C, 8 seconds between pulses and signal averaging 120 transients.
  • Spectral signals were integrated and the number of unsaturation types per 1000 carbons was calculated by multiplying the different groups by 1000 and dividing the result by the total number of carbons.
  • the number averaged molecular weight (Mn) was calculated by dividing the total number of unsaturated species into 14,000, assuming one unsaturation per polyolefin chain.
  • the chain end unsaturations are measured as follows.
  • the vinyl resonances of interest are between from 5.0 to 5.1 ppm (VRA), the vinylidene resonances between from 4.65 to 4.85 ppm (VDRA), the vinylene resonances from 5.31 to 5.55 ppm (VYRA), the trisubstituted unsaturated species from 5.1 1 to 5.30 ppm (TSRA) and the aliphatic region of interest between from 0 to 2.1 ppm (IA).
  • the number of vinyl groups/1000 Carbons is determined from the formula: (VRA * 500) / (((IA +VRA + VYRA + VDRA)/2) + TSRA).
  • the number of vinylidene groups / 1000 Carbons is determined from the formula: (VDRA * 500) / (((IA +VRA + VYRA + VDRA)/2) + TSRA), the number of vinylene groups / 1000 Carbons from the formula (VYRA * 500) / (((IA +VRA + VYRA + VDRA)/2) + TSRA) and the number of trisubstituted groups from the formula (TSRA * 1000) / (((IA +VRA + VYRA + VDRA)/2) + TSRA).
  • VRA, VDRA, VYRA, TSRA and IA are the integrated normalized signal intensities in the chemical shift regions defined above.
  • Molecular weights (number average molecular weight (Mn), weight average molecular weight (Mw), and z-average molecular weight (Mz)) were determined using a Polymer Laboratories Model 220 high temperature SEC equipped with on-line differential refractive index (DRI), light scattering (LS), and viscometer (VIS) detectors. It used three Polymer Laboratories PLgel 10 m Mixed-B columns for separation using a flow rate of 0.54 ml/min and a nominal injection volume of 300 ⁇ The detectors and columns were contained in an oven maintained at 135 °C. The stream emerging from the SEC columns was directed into a miniDAWN optical flow cell and then into the DRI detector.
  • DRI differential refractive index
  • LS light scattering
  • VIS viscometer
  • the DRI detector was an integral part of the Polymer Laboratories SEC.
  • the viscometer was inside the SEC oven, positioned after the DRI detector.
  • the details of these detectors as well as their calibrations have been described by, for example, T. Sun, P. Brant, R. R. Chance, and W. W. Graessley, in Macromolecules, Volume 34, Number 19, 6812-6820, (2001), incorporated herein by reference.
  • Solvent for the SEC experiment was prepared by dissolving 6 grams of butylated hydroxy toluene as an antioxidant in 4 liters of Aldrich reagent grade 1, 2, 4-trichlorobenzene (TCB). The TCB mixture was then filtered through a 0.7 ⁇ glass pre-filter and subsequently through a 0.1 ⁇ Teflon filter. The TCB was then degassed with an online degasser before entering the SEC. Polymer solutions were prepared by placing dry polymer in a glass container, adding the desired amount of TCB, then heating the mixture at 160°C with continuous agitation for 2 hours. All quantities were measured gravimetrically.
  • the TCB densities used to express the polymer concentration in mass/volume units were 1.463 g/mL at room temperature and 1.324 g/mL at 135°C.
  • the injection concentration was from 1.0 to 2.0 mg/mL, with lower concentrations being used for higher molecular weight samples.
  • Prior to running each sample the DRI detector and the injector were purged. Flow rate in the apparatus was then increased to 0.5 mL/minute, and the DRI was allowed to stabilize for 8 to 9 hours before injecting the first sample.
  • the concentration, c, at each point in the chromatogram was calculated from the baseline-subtracted DRI signal, I D RJ, using the following equation:
  • the light scattering detector was a high temperature mini DAWN (Wyatt Technology, Inc.).
  • the primary components are an optical flow cell, a 30 mW, 690 nm laser diode light source, and an array of three photodiodes placed at collection angles of 45°, 90°, and 135°.
  • the molecular weight, M, at each point in the chromatogram was determined by analyzing the LS output using the Zimm model for static light scattering (M.B. Huglin, LIGHT SCATTERING FROM POLYMER SOLUTIONS Academic Press, 1971):
  • AR(9) is the measured excess Rayleigh scattering intensity at scattering angle ⁇
  • c is the polymer concentration determined from the DRI analysis
  • (dn/dc) 0.104 for propylene polymers, 0.098 for butene polymers and 0.1 otherwise
  • ⁇ ( ⁇ ) is the form factor for a monodisperse random coil
  • K 0 is the optical constant for the system:
  • a high temperature viscometer from Viscotek Corporation was used to determine specific viscosity.
  • the viscometer has four capillaries arranged in a Wheatstone bridge configuration with two pressure transducers. One transducer measures the total pressure drop across the detector, and the other, positioned between the two sides of the bridge, measures a differential pressure.
  • the specific viscosity, n s for the solution flowing through the viscometer was calculated from their outputs.
  • the intrinsic viscosity, [ ⁇ ], at each point in the chromatogram was calculated from the following equation:
  • the branching index (g' v i s ) is defined as the ratio of the intrinsic viscosity of the branched polymer to the intrinsic viscosity of a linear polymer of equal molecular weight and same composition, and was calculated using the output of the SEC-DRI-LS-VIS method as follows.
  • ] aV g, of the sample was calculated by:
  • the branching index g' v i s is defined as:
  • M v is the viscosity-average molecular weight based on molecular weights determined by LS analysis. See Macromolecules, 2001, 34, pp.
  • Viscosity was measured using a Brookfield Viscometer according to ASTM D- 3236.
  • Peak melting point, Tm, (also referred to as melting point), peak crystallization temperature, Tc, (also referred to as crystallization temperature), glass transition temperature (Tg), heat of fusion ( ⁇ 3 ⁇ 4), and percent crystallinity were determined using the following DSC procedure according to ASTM D3418-03. Differential scanning calorimetric (DSC) data were obtained using a TA Instruments model Q200 machine. Samples weighing approximately 5-10 mg were sealed in an aluminum hermetic sample pan. The DSC data were recorded by first gradually heating the sample to 200°C at a rate of 10°C/minute.
  • the sample was kept at 200°C for 2 minutes, then cooled to -90°C at a rate of 10°C/minute, followed by an isothermal for 2 minutes and heating to 200°C at 10°C/minute. Both the first and second cycle thermal events were recorded. Areas under the endothermic peaks were measured and used to determine the heat of fusion and the percent of crystallinity. The percent crystallinity is calculated using the formula, [area under the melting peak (Joules/gram) / B (Joules/gram)] * 100, where B is the heat of fusion for the 100% crystalline homopolymer of the major monomer component.
  • Ethylene and propylene monomers were purified on-line by passing the feed streams through beds of 3A mole sieves, and metered to a mixing manifold using mass flow controllers (Brooks), where they were combined with the isohexane solvent prior to entering the reactor.
  • mass flow controllers Brooks
  • scavenger tri-n-octyl aluminum in isohexane
  • catalyst premixed with activator in toluene
  • Nominal reactor residence times were on the order of 10 minutes, after which the continuous reactor effluent was collected and first air-dried in a hood to evaporate most of the solvent and unreacted monomers, and then dried in a vacuum oven at a temperature of 80°C for 12 hours. The vacuum oven dried samples were then weighed to obtain the final polymer yield which could then be used to calculate catalyst activity (also referred as to catalyst productivity) based on the ratio of yield to catalyst feed rate.
  • the polymer C 2 wt% was measured by FTIR, ASTM D3900.
  • LS and DRI denote the methods of light scattering and differential refractive index used in the GPC-3D experiment, respectively.
  • ML is the Mooney viscosity and MLRA is the Mooney large relaxation area for 100 s, both measured at 125°C.
  • Mooney viscosity is a property used to monitor the quality of both natural and synthetic rubbers. It measures the resistance of rubber to flow at a relatively low shear rate.
  • the highly branched compositions herein have a Mooney viscosity ML (1 + 4) at 125°C of 30 to 100 MU (preferably 40 to 100; more preferably 50 to 100; even more preferably 60 to 100), where MU is Mooney Units.
  • the Mooney viscosity indicates the plasticity of the rubber
  • the Mooney relaxation area provides a certain indication of the effects of molecular weight distribution and elasticity of the rubber.
  • the highly branched compositions also have a MLRA of 100 to 1000 (preferably 200 to 1000; more preferably 300 to 1000; even more preferably 450 to 950).
  • the highly branched compositions of this invention preferably have an MLRA/ML ratio greater than 5, preferably greater than 6, preferably greater than 7 and most preferably greater than 8, preferably for mEPCs with a Mw/Mn from 2 to 3 or 4, higher than the precursor mEPDM rubber, or desirably, the MLRA/ML ratio is within a range of from 5 or 6 to 10 or 12 or 14.
  • Mooney viscosity and Mooney relaxation area are measured using a Mooney viscometer, operated at an average shear rate of 2 s "1 , according to the following modified ASTM D1646.
  • ASTM D1646 was modified as follows: A square of sample is placed on either side of the rotor. The cavity is filled by pneumatically lowering the upper platen. The upper and lower platens are electrically heated and controlled at 125°C. The torque to turn the rotor at 2 rpm is measured by a torque transducer. The sample is preheated for 1 minute after the platens were closed. The motor is then started and the torque is recorded for a period of 4 minutes. Results are reported as ML (1 + 4) at 125°C, where M is Mooney viscosity number, L denotes the large rotor, 1 is the sample preheat time in minutes, 4 is the sample run time in minutes after the motor starts, and 125°C is the test temperature.
  • the MLRA data is obtained from the Mooney viscosity measurement when the rubber relaxed after the rotor is stopped.
  • the MLRA is the integrated area under the Mooney torque-relaxation time curve from 1 to 100 seconds.
  • the MLRA can be regarded as a stored energy term which suggests that, after the removal of an applied strain, the longer or branched polymer chains can store more energy and require longer time to relax. Therefore, the MLRA value of a bimodal rubber (the presence of a discrete polymeric fraction with very high molecular weight and distinct composition) or a long chain branched rubber are larger than a broad or a narrow molecular weight rubber when compared at the same Mooney viscosity values.
  • the sample was first cooled to -90°C at 20°C/min.
  • the sample was heated to 220°C at 10°C/min and melting data (first heat) were acquired. This provides information on the melting behavior under "as-received" conditions, which can be influenced by thermal history as well as sample preparation method.
  • the sample was then equilibrated at 220°C to erase its thermal history.
  • Crystallization data (first cool) were acquired by cooling the sample from the melt to -90°C at 10°C/min and equilibrated at -90°C. Finally, the sample was heated again to 220°C at 10°C/min to acquire additional melting data (second heat). The endothermic melting transition (second heat) was analyzed for peak temperature as Tm and for area under the peak as heat of fusion (Hf).
  • the mEPCs made by catalyst 1/activator 1 have higher values of T m and H f than the mEPCs made by catalyst 2/activator 2.
  • the mEPC prepared with catalyst 1/activator 1 has a longer methylene sequence than that prepared with catalyst 2/activator 2 based on 13 C NMR studies, Table 2. This leads to a T m of 30°C higher for the mEPC prepared with catalyst 1/activator 1 compared to samples from the catalyst 2/activator 2 catalyst system.
  • Table 2 the values of wt% C 2 of mEPC determined by 13 C NMR and FTIR are close, at least for these 3 copolymers.
  • the difference is less than or equal to 0.5 wt%.
  • the values of ri and r 2 denote the reactivity ratios, which represent the ratios of the rate constants describing the addition of a like monomer relative to an unlike monomer. If the rir 2 value is less than unity as measured for sample 1, it represents more alternating or random sequences. If ri and 3 ⁇ 4 are both large but not infinite, as shown for sample 2 and sample 3, then block or blocky copolymers will be produced, or perhaps some homopolymers may be present, depending on how large the reactivity ratios are and the relative concentration of the monomers in the feed.
  • Catalyst Activity (g/g) 74,700 114,863 96,187 80,550 66,488 109,286 115,500
  • Tables 2 and 2a contain chain punctuation data determined from C NMR spectra. Chain punctuation can be evaluated using the Run# which represents the number of times that a comonomer changes from one type to the other per 100 monomers. At a given comonomer level a lower Run# indicates that the comonomer is more blocked. Blockiness can also be evaluated by calculating an average methylene sequence length which is determined by dividing the methylene content by the total number of sequences. Therefore, at a particular methylene concentration the average sequence length will necessarily be longer with a lower number of methylene runs or sequences. In Table 2 average sequence length for all methylene sequences 2 and longer and 6 and longer are shown.
  • Sample 1 made with the catalyst 2/activator 2 catalyst system has shorter methylene sequences on average than samples made with catalyst 1/activator 1.
  • the longer sequences in the catalyst 1/activator 1 polymers correlate with their higher level of crystallinity relative to the catalyst 2/activator 2 sample.
  • Table 2a contains the methylene sequence length distribution in the copolymers determined by 13 C NMR.
  • Sample 1 made with catalyst 2/activator 2 has a more even distribution of sequences relative the catalyst 1/activator 1 polymers.
  • Catalyst 1/activator 1 samples have a lower percentage of shorter sequences and a higher amount of longer ones compared to the catalyst 2/activator 2 polymer.
  • the greater proportion of longer sequences in the catalyst 1/activator 1 polymers is consistent with them having more crystallinity compared to the catalyst 2/activator 2 polymer.
  • Figures 3-5 show the GPC-3D traces of the 3 mEPCs described in Table 2. No shoulders or extra peaks that would cause the higher T m values for the two mEPCs prepared with catalyst 1/activator 1 were noted.
  • Table 3 shows the GPC-3D, ML and MLRA results of a set of mEPCs made by catalyst 2/activator 2 or catalyst 1/activator 1. These mEPCs have similar molecular weights or ML and similar C2 contents. These copolymers have essentially no gel because the values of GPC-3D mass recovery are all greater than or equal to 90%.
  • the mEPCs made by catalyst 1/activator 1 show more branching, as indicated by small values of g' and a larger values of MLRA.
  • the larger MLRA is due to the fact that, after the release of an applied deformation in the Mooney rheometer, the branched mEPC takes a longer time to relax relative to a linear mEPC, leading to a larger relaxation area under the Mooney torque curve.
  • the mEPCs prepared with catalyst 1/activator 1 also have larger values of tensile strength and elongation at break than the mEPC prepared with catalyst 2/activator 2, Figure 6.
  • N [(vinyls/1,000 C)/1,000] (M n /14)
  • the N value of mEPC made using catalyst 1/activator 1 is much higher than that from the catalyst 2/activator 2 sample. There are 75 chains containing the terminal double bond in every 100 chains of the catalyst 1/activator 1 -derived mEPC. For the mEPC made with the catalyst 2/activator 2 catalyst system, there are only 4 chains containing the terminal double bond in every 100 chains. The greater number of chains terminating with a double bond can result in more branching by increasing the probability of polymer reincorporation during polymerization.
  • FIG. 7a and 7b Another method to detect the existence of branch structure in these mEPCs is based on small-strain rheology as shown in Figures 7a and 7b for the samples prepared using the catalyst 1/activator 1 and catalyst 2/activator 2 catalyst, respectively.
  • the test temperature was 190°C and the shear strain applied was 10%.
  • the complex modulus (G*), the phase angle ( ⁇ ), and the complex viscosity ( ⁇ *) were measured as the frequency was varied from 0.01 to 100 rad/s.
  • the plots of phase angle versus the complex modulus in Figures 7a and 7b are known as the Van Gurp-Palmen plots (Please see M. Van Gurp, J. Palmen, Rheol.
  • the mEPC prepared with catalyst 1 /activator 1 will be a better compatibilizer for the blends of ethylene-based polymers or copolymers and propylene-based polymers or copolymers than the mEPC prepared with catalyst 2/activator 2 because the former type of mEPC has both a longer ethylene sequence and a branched topology.

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Abstract

L'invention concerne des procédés de préparation et des compositions concernant les copolymères éthylène-propylène ramifiés qui comprennent au moins 50 % en poids d'éthylène d'après un spectromètre infrarouge à transformée de Fourier (FTIR) ; une valeur g'vis inférieure à 0,95 ; un poids moléculaire Mw de 150 000 à 250 000 ; une séquence de méthylène d'une longueur de 6 ou plus d'après 13C RMN, le pourcentage de séquences de longueur 6 ou plus étant supérieur à 32 % ; et pouvant avoir une fonctionnalité terminale à chaîne vinyle de plus de 50 %.
PCT/US2014/045542 2013-07-17 2014-07-07 Compositions copolymères d'éthylène-propylène avec de longues séquences de méthylène WO2015009474A1 (fr)

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US9796795B2 (en) 2015-01-14 2017-10-24 Exxonmobil Chemical Patents Inc. Tetrahydroindacenyl catalyst composition, catalyst system, and processes for use thereof
US9803037B1 (en) 2016-05-03 2017-10-31 Exxonmobil Chemical Patents Inc. Tetrahydro-as-indacenyl catalyst composition, catalyst system, and processes for use thereof
US10640583B2 (en) 2015-04-20 2020-05-05 Exxonmobil Chemical Patents, Inc. Catalyst composition comprising fluorided support and processes for use thereof
US10703838B2 (en) 2017-10-31 2020-07-07 Exxonmobil Chemical Patents Inc. Mixed catalyst systems with four metallocenes on a single support
US10717790B2 (en) 2015-04-20 2020-07-21 Exxonmobil Chemical Patents Inc. Catalyst composition comprising fluorided support and processes for use thereof
EP4103629A4 (fr) * 2020-02-11 2024-06-05 ExxonMobil Chemical Patents Inc. Compositions de polyéthylène obtenues à l'aide de complexes de catalyseur de bis(phénolate) de métal de transition et procédé homogène pour la production de celles-ci

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EP3484984B1 (fr) 2016-07-14 2022-08-03 ExxonMobil Chemical Patents Inc. Compositions d'huile lubrifiante comprenant des compositions de copolymères bimodaux, catalysés par un métallocène double, utiles en tant que modificateurs de viscosité
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WO2016114914A1 (fr) * 2015-01-14 2016-07-21 Exxonmobil Chemical Patents Inc. Procédé de production de compositions polymères
US10253173B2 (en) 2015-01-14 2019-04-09 Exxonmobil Chemical Patents Inc. Polymer compositions and processes for their production
US10385198B2 (en) 2015-01-14 2019-08-20 Exxonmobil Chemical Patents Inc. Polymer compositions with improved rheological properties
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US10538656B2 (en) 2015-01-14 2020-01-21 Exxonmobil Chemical Patents Inc. Polymer compositions and processes for their production
US10717790B2 (en) 2015-04-20 2020-07-21 Exxonmobil Chemical Patents Inc. Catalyst composition comprising fluorided support and processes for use thereof
US10640583B2 (en) 2015-04-20 2020-05-05 Exxonmobil Chemical Patents, Inc. Catalyst composition comprising fluorided support and processes for use thereof
US9803037B1 (en) 2016-05-03 2017-10-31 Exxonmobil Chemical Patents Inc. Tetrahydro-as-indacenyl catalyst composition, catalyst system, and processes for use thereof
US11345766B2 (en) 2016-05-03 2022-05-31 Exxonmobil Chemical Patents Inc. Tetrahydro-as-indacenyl catalyst composition, catalyst system, and processes for use thereof
US10703838B2 (en) 2017-10-31 2020-07-07 Exxonmobil Chemical Patents Inc. Mixed catalyst systems with four metallocenes on a single support
EP4103629A4 (fr) * 2020-02-11 2024-06-05 ExxonMobil Chemical Patents Inc. Compositions de polyéthylène obtenues à l'aide de complexes de catalyseur de bis(phénolate) de métal de transition et procédé homogène pour la production de celles-ci

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