WO2020167399A1 - Procédés de polymérisation biphasiques et polyoléfines à base d'éthylène obtenues par ces derniers - Google Patents

Procédés de polymérisation biphasiques et polyoléfines à base d'éthylène obtenues par ces derniers Download PDF

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WO2020167399A1
WO2020167399A1 PCT/US2020/013674 US2020013674W WO2020167399A1 WO 2020167399 A1 WO2020167399 A1 WO 2020167399A1 US 2020013674 W US2020013674 W US 2020013674W WO 2020167399 A1 WO2020167399 A1 WO 2020167399A1
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polymerization mixture
maintaining
ethylene
less
polymerization
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PCT/US2020/013674
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English (en)
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Gabor Kiss
Thomas T. Sun
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Exxonmobil Chemical Patents Inc.
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Publication of WO2020167399A1 publication Critical patent/WO2020167399A1/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
    • C08F2/00—Processes of polymerisation
    • C08F2/04—Polymerisation in solution
    • C08F2/06—Organic solvent
    • 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
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • 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
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/02—Ethene
    • 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
    • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
    • 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
    • C08F2420/00—Metallocene catalysts
    • C08F2420/10—Heteroatom-substituted bridge, i.e. Cp or analog where the bridge linking the two Cps or analogs is substituted by at least one group that contains a heteroatom
    • 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+

Definitions

  • Embodiments of the invention are directed toward biphasic polymerization processes, and in certain embodiments biphasic polymerization processes that produce ethylene-based polyolefins with narrow molecular weight distributions.
  • Continuous solution polymerization processes generally involve the addition of catalyst to monomer and solvent mixture at conditions that keep the polymer product dissolved in the biphasic reaction medium.
  • the mixture may be back-mixed to provide a uniform polymer in an environment with substantially no concentration gradients.
  • WO 94/00500 (Pannell, et al.) describes a solution polymerization using metallocene in a continuous stirred tank reactor, which may be in a series reactor arrangement to make a variety of products.
  • the heat of the polymerization reaction can be absorbed by the polymerization mixture, causing an exotherm; i.e., a temperature rise of the reaction medium.
  • the heat of reaction can be removed by a cooling system, by external cooling of the walls of the reactor vessel, or by internally arranged heat exchange surfaces cooled by a heat exchange fluid.
  • phase separation depends on the selection of the polymerization solvent.
  • appropriate monomer conversions especially of the volatile monomers, temperatures, and pressures, are selected for given polymer/solvent combination to avoid unwanted phase separation inside the reactor.
  • Solvents such as hexane may require an elevated pressure in excess of 50 bar to avoid two-phase conditions for olefin polymerization; solvents such as octane can maintain homogeneous one-phase conditions at lower pressures.
  • phase separation is often exploited after the reaction step to separate volatile solvent and unreacted monomer components on the one hand, and polymer on the other hand.
  • separations at temperatures well above the lower critical separation temperature allow the polymer to form a concentrated phase.
  • Embodiments of the invention are directed toward a continuous process for preparing an ethylene-based polyolefin, the process comprising maintaining a polymerization mixture at a temperature at or above the lower critical phase separation temperature of the polymerization mixture, while, during said step of maintaining, maintaining the polymerization mixture at steady state, where the polymerization mixture is substantially uniform in temperature, pressure, and concentration, where the polymerization mixture includes solvent, monomer including ethylene and optionally monomer copolymerizable with ethylene, a single site catalyst system, and polymer resulting from the polymerization of the monomer, where the monomer and the polymer are dissolved in the solvent, and where the polymer is an ethylene- based polyolefin having a molecular weight distribution (Mw/Mn) of less than 2.30.
  • Mw/Mn molecular weight distribution
  • Other embodiments of the invention are directed toward a method for preparing ethylene-based polyolefin, the method comprising (i) providing a polymerization vessel; (ii) continuously charging the polymerization vessel with monomer including ethylene and olefin monomer copolymerizable with ethylene, a solvent, and a single-site catalyst system, to thereby form a polymerization mixture; (iii) maintaining the polymerization mixture within the vessel at a temperature at or above the lower critical phase separation temperature of the polymerization mixture; (iv) mixing the polymerization within the vessel so that the temperature, pressure, and concentration of the polymerization mixture within the vessel is substantially uniform; and (v) continuously removing monomer, polymer formed by the polymerization of monomer, solvent, and single-site site catalyst system from the polymerization vessel at a rate substantially constant to the rate of continuously charging monomer, a solvent, and a single-site catalyst system, to thereby form a polymerization mixture, where the polymer continuously removed from the
  • Still other embodiments of the invention are directed toward a polymeric solution comprising ethylene -based polyolefin dissolved in solvent at a temperature and pressure above the lower critical separation temperature of the polymer solution, where the ethylene-based polyolefin has a molecular weight distribution, Mw/Mn, of less than 2.3, where the solution is a biphasic solution including a first liquid phase including greater than 10 wt % ethylene -based polyolefin, based on the total weight of the first liquid phase, and a second liquid phase including less than 10,000 ppm ethylene-based polyolefin, based on the total weight of the second liquid phase.
  • Embodiments of the invention are based, at least in part, on the discovery of a continuous process for solution polymerizing ethylene, optionally together with comonomer, at a pressure and temperature above the lower critical separation temperature (LCST) to thereby produce an ethylene-based polyolefin having a molecular weight distribution, Mw/Mn, of less than 2.3.
  • this continuous solution polymerization process employs a single-site catalyst that is soluble within the polymerization mixture, and the polymerization mixture is uniform and maintained at steady state.
  • the prior art contemplates the polymerization of ethylene using a single-site catalyst at temperatures and pressures above the LCST
  • the ethylene-based polyolefins produced by the prior art have a molecular weight distribution, Mw/Mn, that is greater than, or equal to, 2.3.
  • Mw/Mn molecular weight distribution
  • aspects of the present invention advantageously provide polymer with narrower molecular weight distribution, which has unexpectedly been achieved by the appropriate selection of process parameters. Embodiments of the invention are therefore directed toward these polymerization processes, as well as the biphasic, liquid-liquid, polymerization mixtures that are utilized by and produced by these processes.
  • a polymerization mixture which may be referred to as a reaction medium that upon polymerization of monomer also includes ethylene -based polyolefin.
  • the polymerization mixture is maintained at a temperature and pressure above the LCST as a uniform polymerization system operated at steady state while a portion of the polymerization mixture is continuously removed from the reactor.
  • monomer includes ethylene and optionally additional monomer(s) polymerizable with ethylene, the latter of which may be referred to as comonomer.
  • monomers copolymerizable with ethylene include, but are not limited to, propylene, alpha-olefins (which include C4 or higher 1-alkenes), vinyl aromatics, vinyl cyclic hydrocarbons, and dienes such as cyclic dienes and alpha-omega dienes.
  • the alpha-olefin includes a C 4 to C 12 alpha-olefin.
  • the alpha-olefin monomer other than ethylene includes, but is not limited to, 1-butene, 1-hexene, 1-octene, 1-decene, 1-dodecene, 4-methyl- 1-pentene, and 3- methyl- 1 -pentene .
  • vinyl cyclic hydrocarbons include vinyl cycloalkanes, such as vinyl cyclohexane and vinyl cyclopentane.
  • vinyl aromatics include styrene and substituted styrene such as alphamethylstyrene.
  • Exemplary cyclic dienes include vinylnorbomene, norbomadiene, ethylidene norbornene, divinylbenzene, cyclopentadiene, dicyclopentadiene or higher ring containing diolefins with or without substituents at various ring positions.
  • alpha-omega dienes examples include butadiene, 1 ,4-pentadiene, 1,5-hexadiene, 1,6-heptadiene, 1,7-octadiene, 1,8-nonadiene, 1,9-decadiene, 1,10-undecadiene, 1,11- dodecadiene, 1,12-tridecadiene, 1,13-tetradecadiene, 1,14-pentadecadiene, 1,15- hexadecadiene, 1,16-heptadecadiene, 1,17-octadecadiene, 1,18-nonadecadiene, 1,19- icosadiene, 1,20-heneicosadiene, 1,21-docosadiene, 1 ,22-tricosadiene, 1,23-tetracosadiene, 1,24-pentacosadiene, 1,25-hexacosadiene, 1,26-heptaco
  • the ethylene concentration within the reactor (which exists in the polymerization mixture and the reactor headspace) relative to the total monomer content (i.e., ethylene plus all comonomer) is greater than 45 wt %, in other embodiments greater than 50 wt %, in other embodiments greater than 55 wt %, in other embodiments greater than 60 wt %, in other embodiments greater than 65 wt %, in other embodiments greater than 70 wt %, in other embodiments greater than 75 wt %, in other embodiments greater than 80 wt %, in other embodiments greater than 85 wt %, in other embodiments greater than 90 wt %, and in other embodiments greater than 95 wt % of the total weight of monomer. In one or more embodiments, considering that the molecular weight of ethylene is lower than the molecular weight of comonomer, the concentration of ethylene will be greater than 50 mol %.
  • one or more dienes are present in the polymerization mixture.
  • the polymerization mixture may include at up to 10 wt %, or 0.00001 to 1.0 wt %, or 0.002 to 0.5 wt %, or 0.003 to 0.2 wt %, based upon the total weight of the monomer.
  • 500 ppm or less of diene is added to the polymerization mixture, or 400 ppm or less, preferably, or 300 ppm or less.
  • at least 50 ppm of diene is added to the polymerization mixture, or 100 ppm or more, or 150 ppm or more.
  • the polymerization mixture is devoid of diene monomer.
  • useful solvents include non-coordinating, inert liquids that dissolve the single-site catalyst, the monomer, and the resulting polymer.
  • useful solvents provide a solution polymerization system wherein the single-site catalyst, monomer, and polymer are molecularly dispersed.
  • Examples of useful solvents include straight and branched-chain paraffinic hydrocarbons, such as butane, isobutane, pentane, isopentane, hexanes, isohexane, heptane, isoheptane, octane, isooctane, dodecane, and mixtures thereof; cyclic and alicyclic hydrocarbons, such as cyclopentane, cyclohexane, cycloheptane, methylcyclopentane, methylcyclohexane, methylcycloheptane, and mixtures thereof, such as can be found commercially (IsoparTM); perhalogenated hydrocarbons, such as perfluorided C 4- 10 alkanes, chlorobenzene, and aromatic and alkylsubstituted aromatic compounds, such as benzene, toluene, mesitylene, and xylene.
  • paraffinic hydrocarbons such as but
  • the solvent is non-aromatic.
  • aromatics are present in the solvent at less than 1 wt %, or less than 0.5 wt %, or less than 0.1 wt % based upon the weight of the solvents.
  • the solvent is essentially free of benzene.
  • a single-site catalyst refers to an active catalyst system that includes a transition metal center (e.g., a metal of group 3 to 10 of the Periodic Table) and at least one ligand that can be abstracted and thereby allow for insertion of the ethylene or comonomer.
  • the active catalyst system i.e., active single-site catalyst system
  • the active catalyst system is formed by combining a transition metal precursor compound (such as a metallocene compound) with an activator compound.
  • transition metal precursor compound such as a metallocene compound
  • the active catalyst may be present as an ion pair of a cation and an anion, where the cation derives from the transition metal precursor compound (e.g., metallocene compound) and the anion derives from the activator compound (e.g., the transition metal is in its cationic state and is stabilized by the activator compound or an anionic species thereof).
  • the ligand remains bonded to the transition metal during polymerization.
  • the mono-anionic ligands are displaceable by a suitable activator to permit insertion of a polymerizable monomer at the vacant coordination site of the transition metal component.
  • a single, single-site catalyst is included with the polymerization.
  • a single transition metal precursor species is combined with a single activator species.
  • the precursor compound can include a metallocene compound, or it may include a non-metallocene transition metal compound.
  • the transition metal precursor compound is a metallocene compound.
  • Metallocene compounds include compounds with a central transition metal and at least two ligands selected from cyclopentadienyl ligands and ligands that are isolobal to cyclopentadienyl ligands.
  • Exemplary transition metals include Group 4 (also known as Group IV) of the Periodic table, such as titanium, hafnium or zirconium.
  • Exemplary cyclopentadienyl ligands, or ligands isolobal thereto include, but are not limited to, cyclopentadienyl ligands, cyclopentaphenanthrenyl ligands, indenyl ligands, benzindenyl ligands, fluorenyl ligands, octahydrofluorenyl ligands, cyclooctatetraenyl ligands, cyclopentacyclododecene ligands, azenyl ligands, azulene ligands, pentalene ligands, phosphoyl ligands, phosphinimine ligands (WO 99/40125), pyrrolyl ligands, pyrazolyl ligands, carbazolyl ligands, borabenzene ligands and the like, including hydrogenated versions thereof, for example tetrahydr
  • ligands may include one or more heteroatoms, for example, nitrogen, silicon, boron, germanium, sulfur and phosphorus, in combination with carbon atoms to form an open, acyclic, or a fused, ring or ring system, for example, a heterocyclopentadienyl ancillary ligand.
  • Other ligands include but are not limited to porphyrins, phthalocyanines, corrins and other polyazamacrocycles.
  • the metallocene compounds may be bridged or unbridged, or they may be substituted or unsubstituted.
  • substituted means that a hydrogen group has been replaced with a hydrocarbyl group, a heteroatom, or a heteroatom containing group.
  • methyl cyclopentadiene is a ligand group substituted with a methyl group.
  • useful metallocene compounds may be defined by the formula: L A L B LC i MDE where, L A is a substituted cyclopentadienyl or hetero- cyclopentadienyl ligand p-bonded to M; L B is a member of the class of ligands defined for L A , or is J, a hetero-atom ligand ⁇ -bonded to M; the L A and L B ligands may be covalently bridged together through a Group 14 element linking group; L C i is an optional neutral, non-oxidizing ligand ( i equals 0 to 3); M is a Group 4 or 5 transition metal; and, D and E are independently mono-anionic labile ligands, each having a ⁇ -bond to M, optionally bridged to each other or L A or L.
  • metallocenes that are biscyclopentadienyl derivatives of a Group IV transition metal, such as zirconium or hafnium. See e.g. W09941294. These may advantageously be derivatives containing a fluorenyl ligand and a cyclopentadienyl ligand connected by a single carbon and silicon atom. See e.g. W09945040 and WO9945041.
  • the cyclopentadienyl ligand (Cp) is unsubstituted and/or the bridge contains alkyl substituents, in certain embodiments alkylsilyl substituents, to assist in the alkane solubility of the metallocene. See W00024792 and W00024793.
  • Other possible metallocenes include those in WOOl/58912.
  • metallocenes may be bisfluorenyl derivatives or unbridged indenyl derivatives, which may be substituted at one or more positions on the fused ring with moieties that have the effect of increasing the molecular weight and so indirectly permit polymerization at higher temperatures such as described in EP693506 and EP780395.
  • the transition metal precursor is a non-metallocene transition metal compound.
  • Representative non-metallocene transition metal compounds useful for forming a single-site catalyst include tetrabenzyl zirconium, tetra bis(trimethylsiylmethyl) zirconium, oxotris(trimethlsilylmethyl) vanadium, tetrabenzyl hafnium, tetrabenzyl titanium, bis(hexamethyl disilazido)dimethyl titanium, tris(trimethyl silyl methyl) niobium dichloride, and tris(trimethylsilylmethyl) tantalum dichloride.
  • the activator compound which may be referred to simply as an activator, may be an alumoxane, such as methylalumoxane.
  • the alumoxanes may have an average degree of oligomerization of from 4 to 30, as determined by vapor pressure osmometry.
  • the alumoxane may be modified to provide solubility in linear alkanes or be used in a slurry (e.g. may include a toluene solution). These solutions may include unreacted trialkyl aluminum, and the alumoxane concentration is generally indicated as mol A1 per liter, which figure includes any trialkyl aluminum that has not reacted to form an oligomer.
  • the alumoxane, when used as an activator compound is generally used in molar excess, at a mol ratio of 50 or more, or 100 or more, or 1000 or less, or 500 or less, relative to the transition metal precursor compound.
  • the activator compound is a compound (i.e. activator precursor) that gives rise to a non-coordinating anion, which is a ligand that weakly coordinates with the metal cation center of the transition metal compound.
  • a non-coordinating anion includes weakly coordinating anions.
  • the coordination of the non-coordinating anion should be sufficiently weak to permit the insertion of the unsaturated monomer component.
  • the activator precursor for the non-coordinating anion may be used with a metallocene supplied in a reduced valency state.
  • the activator precursor may undergo a redox reaction.
  • the precursor may be an ion pair of which the precursor cation is neutralized and/or eliminated in some manner.
  • the precursor cation may be an ammonium salt as in EP-277003 and EP-277004.
  • the precursor cation may be a triphenylcarbonium derivative.
  • the activator precursor may include borates or metal alkyls.
  • the non-coordinating anion can be a halogenated, tetra- aryl-substituted Group 10-14 non-carbon element-based anion, especially those that are have fluorine groups substituted for hydrogen atoms on the aryl groups, or on alkyl substituents on those aryl groups.
  • effective Group 10-14 element activator complexes may be derived from an ionic salt including a 4-coordinate Group 10-14 element anionic complex.
  • the anion can be represented as: [(M)Q 1 Q 2 . . .
  • M is one or more Group 10-14 metalloid or metal, (e.g. boron or aluminum), and each Q is a ligand effective for providing electronic or steric effects rendering [(M)Q 1 Q 2 . . . Q n ]- suitable as a non-coordinating anion as that is understood in the art, or a sufficient number of Q are such that [(M)Q 1 Q 2 . . . Q n ]- as a whole is an effective non-coordinating or weakly coordinating anion.
  • M is one or more Group 10-14 metalloid or metal, (e.g. boron or aluminum)
  • each Q is a ligand effective for providing electronic or steric effects rendering [(M)Q 1 Q 2 . . . Q n ]- suitable as a non-coordinating anion as that is understood in the art, or a sufficient number of Q are such that [(M)Q 1 Q 2 . . . Q n ]- as a whole is an effective non-coordinating or weakly
  • Exemplary Q substituents specifically include fluorinated aryl groups, (e.g., perfluorinated aryl groups), and include substituted Q groups having substituents additional to the fluorine substitution, such as fluorinated hydrocarbyl groups.
  • exemplary fluorinated aryl groups include phenyl, biphenyl, naphthyl and derivatives thereof.
  • the non-coordinating anion may be used in approximately equimolar amounts relative to the transition metal component, such as at least 0.25, or at least 0.5, or at least 0.8, or at least 1.0, or at least 1.05. In these or other embodiments, non-coordinating anion may be used in approximately equimolar amounts relative to the transition metal component and such as no more than 4, preferably 2 and especially 1.5.
  • the polymerization mixture may additionally include a scavenger compound, which may include an organometallic compound.
  • a scavenger compound which may include an organometallic compound.
  • these compounds are effective for removing polar impurities from the reaction environment and/or for increasing catalyst activity.
  • impurities can be inadvertently introduced to the polymerization mixture (e.g., with any of the polymerization reaction components, solvent, monomer and catalyst), which can adversely affect catalyst activity and stability.
  • these impurities can include, without limitation, water, oxygen, heteroatom- containing polar organic compounds, metal impurities, etc.
  • Exemplary scavengers include organometallic compounds such as the Group 13 organometallic compounds. Specific examples include triethyl aluminum, triethyl borane, tri- isobutyl aluminum, tri-n-octyl aluminum, methylalumoxane, and isobutyl alumoxane. Alumoxane also may be used in scavenging amounts with other means of activation, e.g., methylalumoxane and tri-isobutyl-aluminoxane with boron-based activators.
  • organometallic compounds such as the Group 13 organometallic compounds. Specific examples include triethyl aluminum, triethyl borane, tri- isobutyl aluminum, tri-n-octyl aluminum, methylalumoxane, and isobutyl alumoxane.
  • Alumoxane also may be used in scavenging amounts with other means of activation
  • the amount of scavenger used with catalyst compounds of the inventions is minimized during polymerization reactions to that amount effective to enhance activity (and with that amount necessary for activation of the catalyst compounds if used in a dual role) since excess amounts may act as catalyst poisons.
  • Useful scavengers are disclosed in U.S. Patent Nos. 5,153,157 and 5,241,025, as well as International Publications WO 91/09882, WO 94/03506, WO 93/14132, and WO 95/07941.
  • the single-site catalyst may be formed by combining the precursor compound with the activator compound, optionally together with a scavenger, prior to introducing the single-site catalyst to the monomer to be polymerized.
  • a scavenger for introducing the single-site catalyst to the monomer to be polymerized.
  • the single-site catalyst may be formed in situ within the reactor in which the polymerization of monomer takes place.
  • the precursor compound and the activator compound may be introduced to the reactor separately and individually (e.g., via separate feed streams).
  • ethylene-based polyolefins include polyethylene homopolymer, polyethylene copolymers, and mixtures thereof.
  • Polyethylene copolymers are copolymers including ethylene-derived units and comonomer-derived units. In other words, the polyethylene copolymers are prepared from the polymerization of ethylene and one or more comonomer(s), which comonomer(s) are described herein above.
  • the ethylene-based polyolefins may be characterized by the amount of comonomer-derived units, other than ethylene-derived units, within the composition.
  • the amount of comonomer- derived units i.e., non-ethylene units
  • NMR analysis nuclear magnetic resonance analysis
  • the ethylene-based polyolefin may include greater than 0.5, in other embodiments greater than 1, and in other embodiments greater than 3 mol % comonomer-derived units other than ethylene-derived units, with the balance including ethylene-derived units.
  • the ethylene-based polyolefins may include less than 20, in other embodiments less than 15, in other embodiments less than 10, and in other embodiments less than 7 mol % comonomer-derived units other than ethylene- derived units, with the balance including ethylene-derived units.
  • the polyethylene composition of the present invention may include from about 0.5 to 20 mol %, in other embodiments from 1 to 15 mol %, and in other embodiments from 3 to 10 mol % comonomer-derived units other than ethylene-derived units, with the balance including ethylene-derived units.
  • the ethylene-based polyolefins of the present invention may be characterized by their number average molecular weight (Mn), which may be measured by using the technique set forth below.
  • Mn number average molecular weight
  • the ethylene-based polyolefins may have a Mn of greater than 10,000, in other embodiments greater than 12,000, in other embodiments greater than 15,000, and in other embodiments greater than 20,000 g/mol.
  • the ethylene-based polyolefins may have a Mn of less than 200,000, in other embodiments less than 100,000, in other embodiments less than 80,000, and in other embodiments less than 60,000 g/mol.
  • the ethylene- based polyolefins have a Mn of from about 10,000 to about 200,000, in other embodiments from about 12,000 to about 100,000, in other embodiments from about 15,000 to about 80,000, and in other embodiments from about 20,000 to about 60,000 g/mol.
  • the ethylene-based polyolefins of the present invention may be characterized by their number average molecular weight (Mw), which may be measured by using the technique set forth below.
  • Mw number average molecular weight
  • the ethylene-based polyolefins may have a Mw of greater than 40,000, in other embodiments greater than 80,000, in other embodiments greater than 90,000, and in other embodiments greater than 100,000 g/mol.
  • the ethylene-based polyolefins may have a Mw of less than 500,000, in other embodiments less than 400,000, in other embodiments less than 300,000, in other embodiments less than 250,000, in other embodiments less than 200,000, and in other embodiments less than 180,000 g/mol.
  • the ethylene -based polyolefins have a Mw of from about 40,000 to about 500,000, in other embodiments from about 80,000 to about 500,000, in other embodiments from about 80,000 to about 400,000, in other embodiments from about 90,000 to about 200,000, and in other embodiments from about 100,000 to about 180,000 g/mol.
  • the ethylene-based polyolefins of the present invention may be characterized by their molecular weight distribution (Mw/Mn), which may also be referred to as polydispersity, where Mw and Mn may be measured by using the technique set forth below.
  • Mw/Mn molecular weight distribution
  • the ethylene-based polyolefins have a Mw/Mn of less than 2.30, in other embodiments less than 2.25, in other embodiments less than 2.20, in other embodiments less than 2.10, and in other embodiments essentially equal to 2.00.
  • the ethylene-based polyolefins have an Mw/Mn of from about 2.00 to about 2.28, in other embodiments from about 2.05 to about 2.25, and in other embodiments from about 2.10 to about 2.23.
  • Mw, Mn and Mw/Mn may be determined by using a High Temperature Gel Permeation Chromatography (Agilent PL-220), equipped with three in-line detectors, a differential refractive index detector (DRI), a light scattering (LS) detector, and a viscometer. Experimental details, including detector calibration, are described in: T. Sun, P. Brant, R. R. Chance, and W. W. Graessley, Macromolecules, Volume 34, Number 19, pp. 6812-6820, (2001) and references therein. Three Agilent PLgel 10 pm Mixed-B LS columns are used. The nominal flow rate is 0.5 mL/min, and the nominal injection volume is 300 pL.
  • Agilent PLgel 10 pm Mixed-B LS columns Three Agilent PLgel 10 pm Mixed-B LS columns are used. The nominal flow rate is 0.5 mL/min, and the nominal injection volume is 300 pL.
  • the various transfer lines, columns, viscometer and differential refractometer (the DRI detector) are contained in an oven maintained at 145 °C.
  • Solvent for the experiment is prepared by dissolving 6 grams of butylated hydroxytoluene as an antioxidant in 4 liters of Aldrich reagent grade 1,2,4-trichlorobenzene (TCB). The TCB mixture is then filtered through a 0.1 pm Teflon filter. The TCB is then degassed with an online degasser before entering the GPC-3D.
  • Polymer solutions are prepared by placing dry polymer in a glass container, adding the desired amount of TCB, then heating the mixture at 160 °C with continuous shaking for about 2 hours. All quantities are measured gravimetrically.
  • the TCB densities used to express the polymer concentration in mass/volume units are 1.463 g/ml at room temperature and 1.284 g/ml at 145 °C.
  • the injection concentration is from 0.5 to 2.0 mg/ml, with lower concentrations being used for higher molecular weight samples.
  • the DRI detector and the viscometer Prior to running each sample, the DRI detector and the viscometer are purged. Flow rate in the apparatus is then increased to 0.5 ml/minute, and the DRI is allowed to stabilize for 8 hours before injecting the first sample.
  • the LS laser is turned on at least 1 to 1.5 hours before running the samples.
  • the concentration, c, at each point in the chromatogram is calculated from the baseline- subtracted DRI signal, I DRI using the following equation: c K DRI I DRI /( (dn/dc), where K DRI is a constant determined by calibrating the DRI, and (dn/dc) is the refractive index increment for the system.
  • Units on parameters throughout this description of the GPC-3D method are such that concentration is expressed in g/cm 3 , molecular weight is expressed in g/mole, and intrinsic viscosity is expressed in dL/g.
  • the LS detector is a Wyatt Technology High Temperature DAWN HELEOS.
  • M molecular weight
  • the molecular weight, M, at each point in the chromatogram is 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):
  • DR(q) is the measured excess Rayleigh scattering intensity at scattering angle Q
  • c is the polymer concentration determined from the DRI analysis
  • a 2 is the second virial coefficient.
  • R(q) is the form factor for a monodisperse random coil
  • K o is the optical constant for the system:
  • N A is Avogadro’s number
  • (dn/dc) is the refractive index increment for the system, which take the same value as the one obtained from DRI method.
  • a high temperature Viscotek Corporation viscometer which has four capillaries arranged in a Wheatstone bridge configuration with two pressure transducers, is used to determine specific viscosity.
  • 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, h s for the solution flowing through the viscometer is calculated from their outputs.
  • the intrinsic viscosity, [h] at each point in the chromatogram is calculated from the following equation:
  • the polymerization mixtures may be formed within and the polymerization reaction conducted within a suitable reactor.
  • suitable reactors include continuous stirred tank reactors (CSTRs), continuous loop reactors with sufficient circulation rate, and boiling pool reactors.
  • CSTRs continuous stirred tank reactors
  • the process of the invention may employ one or more reactors. When more than one reactor is deployed in the process, they may be of the same or different reactor type, but at least one of the more than one reactors will be suitable for the process of the present invention; i.e., at least one of the reactors can accommodate a polymerization mixture maintained above the lower critical separation temperature and provide a homogeneous polymerization mixture maintained at steady state.
  • the reactors may be fully liquid filled or may be partially filled with liquid, the second phase being a gas filled with the vapors in equilibrium with the liquid phase.
  • the reactors may operate at the same or different conditions with the same or different feeds.
  • they may be of the same or different reactor type, but at least one of the more than one reactors will be suitable for the process of the current disclosure and will produce a polymer with narrow molecular weight distribution, and in case of copolymers narrow composition distribution, in a liquid-liquid phase separated solution medium. They may be connected in series or in parallel, or any other combination when more than two reactors are employed.
  • the polymerization mixture is maintained at a temperature and pressure above the lower critical separation temperature (LCST).
  • LCST critical separation temperature
  • the polymerization mixture is a liquid-liquid, biphasic reaction medium. While the LCST of any given polymerization mixture can depend on several factors, such as the solvent used and the concentration of the monomer and polymer within the system, those having skill in the art can readily determine, without undue experimentation or calculation, the LCST of any given polymerization mixture at a specified pressure.
  • the processes of the present invention include maintaining the polymerization mixture under a pressure of less than 70 atm, in other embodiments less than 60 atm, in other embodiments less than 50 atm, in other embodiments less than 45 atm, and in other embodiments less than 40 atm. In one or more embodiments, the processes of the present invention includes maintaining the polymerization mixture under a pressure of from about 40 to about 70 atm, in other embodiments from about 50 to about 68 atm, and in other embodiments from about 60 to about 65 atm.
  • the processes of the present invention includes maintaining the polymerization mixture at a temperature that is greater than 130 °C, in other embodiments greater than 140 °C, in other embodiments greater than 145 °C, in other embodiments greater than 150 °C, in other embodiments greater than 155 °C, in other embodiments greater than 160 °C, in other embodiments greater than 165 °C, and in other embodiments greater than 170 °C.
  • the polymerization mixture is maintained, in combination with the above-described pressures, in the temperature range of from about 130 to about 170 °C, in other embodiments from about 150 to about 168 °C, and in other embodiments from about 155 to about 165 °C.
  • the polymerization mixture is maintained under steady state conditions of temperature and pressure during polymerization of the monomer.
  • steady state refers to maintaining substantially constant reactor feed and effluent compositions, temperature and pressure within a specified time domain (i.e. over a given period of time).
  • the time domain is the time duration in which the monomer undergoes polymerization.
  • the time domain is the residence time that the polymerization mixture is in the polymerization reactor. In these or other embodiments, this time duration refers to the time at which the polymerization mixture is above the LCST.
  • substantially constant temperature and pressure refers to maintaining the polymerization mixture within those temperature and pressure fluctuations that yield less than appreciable changes in the polymerization of monomer, especially with regard to the molecular weight distribution of the resulting polymer.
  • the temperature and pressure of polymerization mixture is maintained, with respect to the relevant time domain, at temperatures and pressures that have a relative percent difference of less than 10 %, in other embodiments less than 8 %, in other embodiments less than 6 %, and in other embodiments less than 4 %.
  • Relative percent difference is calculated by obtaining two measurements (e.g. two temperature measurements) at two different times during the relative time domain (e.g. during the residence time of the polymerization), calculating the absolute difference, if any, between the measurements, dividing the difference by the average of the two measurements, and then multiplying by 100%.
  • this calculation can be described for reactor temperature by the following formula
  • the polymerization mixture is maintained, over the relevant time domain (e.g. during the residence time within the polymerization reactor) so as to maintain temperature fluctuations of less than 15 °C, in other embodiments less than 10 °C, and in other embodiments less than 5 °C.
  • the polymerization mixture is maintained, over the relevant time domain (e.g. during the residence time within the polymerization reactor), so as to maintain pressure fluctuations of less than 10 atm, in other embodiments less than 7 atm, and in other embodiments less than 4 atm.
  • the skilled person will be able to readily maintain the temperature and pressure of the polymerization mixture, during the relevant time domain, within the parameters of this invention without the exercise of undue calculation or experimentation.
  • conventional means exist to manipulate and maintain the pressure of a polymerization reactor such as a continuously-stirred tank reactor (CSTR).
  • CSTR continuously-stirred tank reactor
  • the temperature can be controlled by employing conventional techniques such as, but not limited to, cooling jackets by adjusting the catalyst feed rate to the reactor, which adjusts the catalyst concentration in the reactor.
  • the polymerization mixture is mixed or otherwise agitated to achieve at least two polymerization mixture characteristics.
  • the polymerization mixture is sufficiently mixed to achieve a polymerization mixture that has one or more uniform properties.
  • the polymerization mixture is sufficiently mixed and/or agitated to achieve a fine dispersion of the first liquid domain within the second liquid domain of the liquid-liquid biphasic medium.
  • the polymerization mixture is sufficiently mixed to achieve uniformity with respect to temperature. This includes the absence of a significant temperature gradient within the polymerization mixture in the reactor (i.e. relative to the spatial domain).
  • the polymerization mixture is sufficiently agitated to achieve a relative percent difference for temperature, between any two locations within the polymerization mixture in the reactor, of less than 15 %, in other embodiments less than 10 %, and in other embodiments less than 5 %.
  • Relative percent difference is calculated by obtaining two measurements (e.g., temperature) at two different locations within the relevant spatial domain (i.e., within the reactor), determining the absolute difference, if any, between the measurements, dividing the difference by the average of the two measurements, and multiplying by 100 percent. Reference can be made to the above formula for calculating relative percent difference.
  • the polymerization mixture is sufficiently mixed or otherwise maintained to achieve a relative percent difference in pressure, between any two locations within the polymerization mixture, of less than 10 %, in other embodiments less than 6 %, and in other embodiments less than 3 %.
  • the polymerization mixture is sufficiently mixed to achieve a relative percent difference in the concentration of dissolved or solubilized solids (e.g. catalyst, monomer, and polymer), between any two locations within the polymerization mixture, of less than 10 %, in other embodiments less than 5 %, and in other embodiments less than 3 %.
  • concentration of dissolved or solubilized solids e.g. catalyst, monomer, and polymer
  • the first liquid domain which is dispersed in the second liquid domain, has a size, which is the diameter or longest dimension of the domain, that is less than 1 ,000 mm, in other embodiments less than 100 mm, and in other embodiments less than 10 mm.
  • the requisite mixing or agitation for practice of the present invention can be achieved by employing conventional mixing techniques. Indeed, those skilled in the art appreciate how to achieve well-mixed reactors. For example, mixing can be accomplished by employing mechanical agitators, by circulation through a loop reactor, or by the churn created by a boiling reaction medium.
  • the respective liquid phases of the liquid-liquid biphasic system may have unique compositional characteristics.
  • one phase may have a higher concentration of ethylene-based polyolefin relative to the second phase.
  • reference may be made to polymer-rich phase and polymer- lean phase, respectively.
  • the polymer-lean phase includes less than 10,000 ppm by weight, in other embodiments less than 5,000 ppm by weight, in other embodiments less than 1,000 ppm by weight, and in other embodiments less than 500 ppm by weight polymer (i.e., ethylene -based polyolefin).
  • the polymer-rich phase may include greater than 10, in other embodiments greater than 15, in other embodiments greater than 20, in other embodiments greater than 25, in other embodiments greater than 30, in other embodiments greater than 35, in other embodiments greater than 40 % by weight polymer (i.e., ethylene- based polyolefin).
  • the polymer rich phase is the dispersed phase and the polymer- lean phase is the continuous phase of the liquid-liquid biphasic system.
  • the polymer-rich phase and the polymer-lean phase generally have similar concentrations of monomer.
  • the respective monomer concentrations of the polymer-rich phase and the polymer-lean phase vary by less than 10 wt %, in other embodiments by less than 5 wt %, and in other embodiments by less than 1 wt %.
  • the polymerization mixture is removed from the vessel in which the polymerization was conducted, and then the resultant ethylene-based polyolefin can be separated from the polymerization mixture (i.e. it is separated from the solvent and unreacted monomer).
  • the two or more polymerization mixtures may be blended (i.e. solution blended off line). This may be particularly useful where multiple polymerization processes are conducted in series or in parallel. As the skilled person will appreciate, these polymer blends may be made for the purpose of improving polymer melt processability or for improving polymer performance for a particular use.
  • ethylene-based bimodal orthogonal composition distributions (BOCD) products in which the high MW component contains higher concentration of comonomers than the low MW component, are known to have improved crack resistance in injection molded products.
  • BOCD products can be made by blending a high MW component made in one reactor with a low MW component from another reactor.
  • melt processability of the polymers of the current disclosure can be improved by broadening the MWD by blending two components of different MW and/or by blending in at least one polymer component that has long-chain branching.
  • the blends may or may not show bimodal (in case of two different blend components) or multimodal (in case of more than two different blend components) molecular weight and/or compositional distribution.
  • the envelopes of their analytical traces may overlap so much that they appear to have a single component, though with broadened distribution. Nonetheless, they are bi- or multimodal in their essence even if the analytical techniques cannot clearly show it.
  • the polymerization mixture can be subjected to any conventional process for the separation of the polymer product from the solvent and monomer.
  • devolatization processes may include the use of devolatizing extruders, which typically heat and mechanically manipulate the polymerization mixture to separate the solvent and monomer as a volatiles stream. In one or more embodiments, this stream can be further treated or otherwise directly recycled back to the polymerization reactor.
  • the ethylene-based polyolefins of the present invention can be fabricated into various articles for a variety of uses.
  • the ethylene-based polyolefins can be injection molded or cast into films.
  • Paragraph A A continuous process for preparing an ethylene -based polyolefin, the process comprising maintaining a polymerization mixture at a temperature at or above the lower critical phase separation temperature of the polymerization mixture, while, during said step of maintaining, maintaining the polymerization mixture at steady state, where the polymerization mixture is substantially uniform in temperature, pressure, and concentration, where the polymerization mixture includes solvent, monomer including ethylene and optionally monomer copolymerizable with ethylene, a single-site catalyst system, and polymer resulting from the polymerization of the monomer, where the monomer and the polymer are dissolved in the solvent, and where the polymer is an ethylene-based polyolefin having a molecular weight distribution (Mw/Mn) of less than 2.30.
  • Mw/Mn molecular weight distribution
  • Paragraph B The process of Paragraph A, where said step of maintaining a polymerization mixture includes maintaining the polymerization mixture at a pressure of less than 70 atm.
  • Paragraph C The process of one or more of Paragraphs A and B, where said step of maintaining a polymerization mixture includes maintaining the polymerization mixture at a pressure of less than 50 atm.
  • Paragraph D The process of one or more of Paragraphs A-C, where said step of maintaining a polymerization mixture includes maintaining the polymerization mixture at a temperature greater than 130 °C.
  • Paragraph E The process of one or more of Paragraphs A-D, where said step of maintaining a polymerization mixture includes maintaining the polymerization mixture at a temperature greater than 150 °C.
  • Paragraph F The process of one or more of Paragraphs A-E, where, during said step of maintaining, maintaining the polymerization mixture at temperature fluctuations of less than 15 °C.
  • Paragraph G The process of one or more of Paragraphs A-F, where, during said step of maintaining, maintaining the polymerization mixture at temperature fluctuations of less than 10 °C.
  • Paragraph H The process of one or more of Paragraphs A-G, where, during said step of maintaining, maintaining the polymerization mixture at pressure fluctuations of less than 10 atm.
  • Paragraph I The process of one or more of Paragraphs A-H, where, during said step of maintaining, maintaining the polymerization mixture at pressure fluctuations of less than 7 atm.
  • Paragraph J The process of one or more of Paragraphs A-I, where, during said step of maintaining, maintaining the temperature and pressure of the polymerization mixture at a relative percent difference of less than 10 %.
  • Paragraph K The process of one or more of Paragraphs A-J, where, during said step of maintaining, maintaining the temperature and pressure of the polymerization mixture at a relative percent difference of less than 6 %.
  • Paragraph L The process of one or more of Paragraphs A-K, where the ethylene- based polyolefin has a molecular weight distribution (Mw/Mn) of less than 2.25.
  • Paragraph M The process of one or more of Paragraphs A-L, where the ethylene- based polyolefin has a molecular weight distribution (Mw/Mn) of less than 2.20.
  • Paragraph N The process of one or more of Paragraphs A-M, where the single-site catalyst is prepared by combining a metallocene compound and an activator compound.
  • Paragraph O The process of one or more of Paragraphs A-N, where the polymerization mixture is biphasic liquid- liquid system including a first liquid phase dispersed within a second liquid phase.
  • Paragraph P The process of one or more of Paragraphs A-O, where the first liquid phase is in the form of liquid domains having a diameter of less than 1,000 mm.
  • Paragraph Q The process of one or more of Paragraphs A-P, where the first liquid phase is in the form of liquid domains having a diameter of less than 100 pm.
  • Paragraph R A method for preparing ethylene-based polyolefin, the method comprising (i) providing a polymerization vessel; (ii) continuously charging the polymerization vessel with monomer including ethylene and olefin monomer copolymerizable with ethylene, a solvent, and a single-site catalyst system, to thereby form a polymerization mixture; (iii) maintaining the polymerization mixture within the vessel at a temperature at or above the lower critical phase separation temperature of the polymerization mixture; (iv) mixing the polymerization mixture within the vessel so that the temperature, pressure, and concentration of the polymerization mixture within the vessel is substantially uniform; and (v) continuously removing monomer, polymer formed by the polymerization of monomer, solvent, and single site site catalyst system from the polymerization vessel at a rate substantially constant to the rate of continuously charging monomer, a solvent, and a single-site catalyst system, where the polymer continuously removed from the polymerization mixture is ethylene-based polyolefin having a
  • Paragraph S The method of Paragraph R, where said step of maintaining the polymerization mixture within the vessel includes maintaining the polymerization mixture at a temperature greater than 130 °C.
  • Paragraph T The method of one or more of Paragraphs R and S, further comprising the step maintaining the polymerization mixture within the vessel at a pressure of less than 70 atm.
  • Paragraph U The method of one or more of Paragraphs R-T, where said step of mixing maintains the polymerization mixture within the vessel at a temperature and pressure at a relative percent difference of less than 10 %, and where said step of mixing maintains the concentration of dissolved solids within the polymerization mixture at a relative percent difference of less than 10%.
  • Paragraph V The method of one or more of Paragraphs R-U, where the ethylene- based polyolefin has a molecular weight distribution (Mw/Mn) of less than 2.25.
  • Paragraph X The process of one or more of Paragraphs R-W, where the first liquid phase is in the form of liquid domains having a diameter of less than 1,000 mm.
  • Paragraph Y A polymer solution comprising ethylene-based polyolefin dissolved in solvent at a temperature and pressure above the lower critical separation temperature of the polymer solution, where the ethylene-based polyolefin has a molecular weight distribution, Mw/Mn, of less than 2.3, where the solution is a biphasic solution including a first liquid phase including greater than 10 wt % ethylene-based polyolefin, based on the total weight of the first liquid phase, and a second liquid phase including less than 10,000 ppm ethylene-based polyolefin, based on the total weight of the second liquid phase.
  • Ethylene-based polyolefins were prepared in isohexane. In certain samples, the polymerization mixtures were maintained above the LCST, and in other samples the mixtures were maintained below the LCST.
  • CSTR continuous stirred tank reactor
  • the reactor was designed to operate at a maximum pressure and temperature of 2000 bar (30 kpsi) and 225 °C, respectively.
  • the nominal reactor vessel volume was 150 mL.
  • the reactor was equipped with a magnetically coupled mechanical stirrer (Magnedrive).
  • a pressure transducer measured the pressure in the reactor.
  • the reactor temperature was measured using two type-K thermocouples. The reported values are the averages of the two readings.
  • a flush- mounted rupture disk located on the side of the reactor provided protection against catastrophic pressure failure. All product lines were heated to ⁇ 120-150 °C to prevent fouling.
  • the reactor had an electric heating band that was controlled by a programmable logic control (PLC) computer to maintain the desired reactor temperature. Except for the heat losses to the environment, the reactor did not have cooling (nearly adiabatic operations). [00102]
  • PLC programmable logic control
  • the conversion in the reactor was monitored by an on-line gas chromatograph (GC) that sampled both the feed and the effluent.
  • GC on-line gas chromatograph
  • Feed purification traps were used to control impurities carried by the monomer feed.
  • the purification traps were placed before the ethylene feed compressor and comprised of two separate beds in series: activated copper (reduced in flowing H 2 at 225 °C and 1 bar) for O 2 removal followed by a molecular sieve (5A, activated in flowing N 2 at 270 °C) for water removal.
  • Purified liquid monomer feed was fed by a single-barrel ISCO pump (model 500D) in neat form or diluted by the same solvent as used in polymerization.
  • the liquid monomer feeds were purified by filtration through an activated basic alumina bed followed by the addition of ⁇ 3 mL of trioctylaluminum solution (Aldrich #38,655-3)/2 L of liquid monomer feed.
  • the catalyst feed solution was prepared inside an argon- filled dry box (Vacuum Atmospheres). The atmosphere in the glove box was purified to maintain ⁇ 1 ppm O 2 and ⁇ 1 ppm water. All glassware was oven-dried for a minimum of at least 4 hours at 110 °C and transferred hot to the antechamber of the dry box before bringing them to the box. Stock solutions of the catalyst precursor and the activator were prepared using purified toluene that was stored in amber bottles inside the dry box. Aliquots were taken to prepare fresh activated catalyst solutions. The activated catalyst solution was charged inside the argon-filled dry box to a heavy-walled glass reservoir (Ace Glass, Inc.
  • HPLC grade hexane (95% n-hexane, J.T. Baker) or isohexane (South Hampton Resources, Dallas, TX) was used as solvent. It was purged with argon for a minimum of four hours and was sent through an activated copper and a molecular sieve (5 A) bed, then filtered once over activated basic alumina. The filtered hexane or isohexane was stored in a heavy- wall 4-liter glass vessel (Ace Glass, Vineland, NJ) inside an argon-filled dry box.
  • the solvent feed was further purified by adding ⁇ 3-5 mL of trioctylaluminum solution (Aldrich #38,655- 3) to the 4-liter reservoir of filtered hexane. 5-10 psig head pressure of argon was applied to the glass vessel to send the scavenger-containing hexane to a metal feed vessel from which the hexane was delivered to the reactor by a two-barrel continuous ISCO pump (model 500D).
  • the reactor was first preheated to ⁇ 10-15 °C below that of the desired reaction temperature. Once the reactor reached the preheat temperature, the solvent pump was turned on to feed the solvent to the reactor. This solvent stream entered the reactor through a port on the top of the stirrer assembly to keep the polymer from fouling the stirrer. The monomers were fed to the reactor through a single side port. The activated catalyst solution was fed by syringe pump. The catalyst solution was mixed with the stream of flowing solvent upstream of the reactor. During the reactor line-out period the catalyst feed rate was adjusted to reach and maintain the target monomer conversion, the latter of which monitored by GC sampling.
  • the products were collected in a dedicated collection vessel for a time sufficient to collect the desired amounts of product. This stage of the run was called the balance period as it was used to collect the product while measuring and recording the exact feed flow rates and the length of the ran.
  • the polymer made during the balance period under steady state conditions was collected at the end of each run and weighed after vacuum-drying overnight at 50-70 °C.
  • the total feed during the balance period combined with the product yield and composition data were used to compute monomer concentrations and monomer conversions. Aliquots of the products were used for characterization without homogenizing the entire product yield.
  • the heat associated with phase transitions was measured on heating and cooling the polymer samples from the solid state and melt, respectively, using a TA Instruments Discovery series DSC.
  • the data were analyzed using the analysis software provided by the vendor. Typically, 3 to 10 mg of polymer was placed in an aluminum pan and loaded into the instrument at room temperature. The sample was cooled to -40 °C and then heated to 210 °C at a heating rate of 10 °C/min to evaluate the glass transition and melting behavior for the as-received polymers. Crystallization behavior was evaluated by cooling the sample from 210 to -40 °C at a cooling rate of 10 °C/min. Second heating data were measured by heating this melt- crystallized sample at 10 °C/min.
  • the second heating data thus provide phase behavior information for samples crystallized under controlled thermal history.
  • the endothermic melting transition (first and second melt) and exothermic crystallization transition were analyzed for onset of transition and peak temperature.
  • the melting temperatures are the peak melting temperatures from the second melt unless otherwise indicated. Areas under the DSC curve were used to determine the heat of fusion (DH f ).
  • MFR Melt Flow Rate
  • the molecular weights and Mw/Mn values were determined using GPC with triple detector using techniques described hereinabove.
  • the instrument was an Agilent PL 220 GPC pump and autoliquid sampler with the Wyatt HELEOS-II detector system, 10mm PD; the column was a 3 PLGel Mixed "B" ( linear range from 500 to 10,000,000 MW PS) having a length of 300 mm and an I.D.
  • SAFT-1 statistical associating fluid theory
  • Mn is the number average molecular weight and the SAFT-1 parameters are defined in the reference above.
  • SAFT-1 parameters are defined in the reference above.
  • Table 3 values were used, which values were obtained by Supercritical Fluids Inc. (Wyoming).
  • compositions, an element or a group of elements are preceded with the transitional phrase“comprising,” it is understood that we also contemplate the same composition or group of elements with transitional phrases “consisting essentially of,”“consisting of,”“selected from the group of consisting of,” or“I” preceding the recitation of the composition, element, or elements and vice versa, e.g., the terms “comprising,”“consisting essentially of,”“consisting of’ also include the product of the combinations of elements listed after the term.

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Abstract

L'invention concerne un procédé continu de préparation d'une polyoléfine à base d'éthylène, le procédé consistant à maintenir un mélange de polymérisation à une température supérieure ou égale à la température de séparation de phase critique inférieure du mélange de polymérisation, tout en maintenant, pendant ladite étape de maintien, le mélange de polymérisation à l'état stable, le mélange de polymérisation étant sensiblement uniforme en température, en pression et en concentration, le mélange de polymérisation comprenant un solvant, un monomère contenant de l'éthylène et éventuellement un monomère copolymérisable avec l'éthylène, un système de catalyseur à site unique, et un polymère résultant de la polymérisation du monomère, le monomère et le polymère étant dissous dans le solvant, et le polymère étant une polyoléfine à base d'éthylène ayant une polydispersité (Mw/Mn) inférieure à 2,30.
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WO2021126443A3 (fr) * 2019-12-17 2021-07-29 Exxonmobil Chemical Patents Inc. Procédé de polymérisation en solution pour fabriquer une ramification à longue chaîne de polyéthylène haute densité

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