Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
• • 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
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
  • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
• • 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
  • C08F2/00—Processes of polymerisation
  • C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
• • 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
  • C08F2/12—Polymerisation in non-solvents
• • 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
  • C08F2/12—Polymerisation in non-solvents
  • C08F2/16—Aqueous medium
  • C08F2/18—Suspension polymerisation
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L23/00—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers
  • C08L23/02—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers not modified by chemical after-treatment
  • C08L23/04—Homopolymers or copolymers of ethene
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L23/00—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers
  • C08L23/02—Compositions of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Compositions of derivatives of such polymers not modified by chemical after-treatment
  • C08L23/04—Homopolymers or copolymers of ethene
  • C08L23/06—Polyethene
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00002—Chemical plants
  • B01J2219/00027—Process aspects
  • B01J2219/0004—Processes in series
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
  • B65D—CONTAINERS FOR STORAGE OR TRANSPORT OF ARTICLES OR MATERIALS, e.g. BAGS, BARRELS, BOTTLES, BOXES, CANS, CARTONS, CRATES, DRUMS, JARS, TANKS, HOPPERS, FORWARDING CONTAINERS; ACCESSORIES, CLOSURES, OR FITTINGS THEREFOR; PACKAGING ELEMENTS; PACKAGES
  • B65D41/00—Caps, e.g. crown caps or crown seals, i.e. members having parts arranged for engagement with the external periphery of a neck or wall defining a pouring opening or discharge aperture; Protective cap-like covers for closure members, e.g. decorative covers of metal foil or paper
  • B65D41/02—Caps or cap-like covers without lines of weakness, tearing strips, tags, or like opening or removal devices
  • B65D41/04—Threaded or like caps or cap-like covers secured by rotation
• • 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
  • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
  • C08F2500/01—High molecular weight, e.g. >800,000 Da.
• • 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
  • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
  • C08F2500/02—Low molecular weight, e.g. <100,000 Da.
• • 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
  • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
  • C08F2500/05—Bimodal or multimodal molecular weight distribution
• • 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
  • C08F2500/00—Characteristics or properties of obtained polyolefins; Use thereof
  • C08F2500/18—Bulk density
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L2205/00—Polymer mixtures characterised by other features
  • C08L2205/02—Polymer mixtures characterised by other features containing two or more polymers of the same C08L -group
  • C08L2205/025—Polymer mixtures characterised by other features containing two or more polymers of the same C08L -group containing two or more polymers of the same hierarchy C08L, and differing only in parameters such as density, comonomer content, molecular weight, structure
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L2205/00—Polymer mixtures characterised by other features
  • C08L2205/03—Polymer mixtures characterised by other features containing three or more polymers in a blend
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08L—COMPOSITIONS OF MACROMOLECULAR COMPOUNDS
  • C08L2207/00—Properties characterising the ingredient of the composition
  • C08L2207/06—Properties of polyethylene
  • C08L2207/068—Ultra high molecular weight polyethylene

Definitions

• the present invention relates to a reactor system for a multimodal polyethylene polymerization process, a process for producing a multimodal polyethylene composition using said reactor system, a multimodal polyethylene composition obtainable this way including a screw cap comprising said multimodal polyethylene composition and the use thereof.
• multimodal polyethylene polymerization is employed to produce polymers having different molecular weights by creating each resin fraction in separated reactors.
• a low molecular weight fraction is produced in a reactor using an excess of hydrogen to control the molecular weight of the polymer suitable for providing good processability of the final polymer.
• a high molecular weight fraction which has an influence on the physical properties and is produced under polymerization conditions with low hydrogen concentration. It is well known in the art that low molecular weight polymer is preferably produced in a first reactor. To obtain a multimodal polymer with good physical properties, all hydrogen from the first reactor should be removed before the polymerized slurry polymer is passed to a second reactor in which the production of high molecular weight polymer takes place.
• US2010/0092709 A 1 describes a process for preparing bimodal polyethylene copolymers.
• the polymerization in a second reactor is operated at a high temperature with a low comonomer-to-ethylene-ratio and low hydrogen-to-ethylene-ratio to obtain resins having improved stress crack resistance and melt strength.
• U.S. Pat. No. 6,716,936 B1 describes a process for producing bimodal polyethylene copolymers.
• a second reactor is operated under hydrogen depleted polyethylene polymerization by directing a polyethylene slurry stream from a first reactor to a hydrogen removal system.
• Polymerization in both the first and the second reactors is operated at the bubble point by using propane or isobutane as a light solvent.
• the process is suitable for the production of a bimodal polyethylene for highly homogeneous high molecular weight resins.
• U.S. Pat. No. 6,291,601 B1 describes a process for producing a bimodal copolymer with relatively high molecular weight polyethylene.
• a hydrogenation catalyst is introduced into a second reactor to consume residual hydrogen gas from first reactor by converting hydrogen into ethane leading to a low hydrogen concentration in the second reactor.
• the cost of raw material consumption of both hydrogen and ethylene are increased due to converting of unreacted gases.
• US 2003/0191251 A1 discloses a process for removing residual hydrogen from a polymer slurry by using two flash drums placed between cascade reactors which use light solvent as a diluent.
• the addition of make-up solvent to the first flash I outlet is required to prevent a slurry transfer pump blocking. Furthermore, warm make-up solvent is necessary before transferring slurry into the next flash drum.
• EP 1655 334 A1 discloses the multimodal production of an ethylene polymer which is produced in a multistage process with a MgCl 2 -based Ziegler-Natta catalyst.
• the polymerization stages are performed in the following order to achieve firstly an ultra high molecular weight polymer, followed by achieving a low molecular weight polymer, and finally achieving high molecular weight polymer in the last step.
• the polymerization catalyst is charged to a prepolymerization step to make an ultra high molecular weight fraction.
• WO 2013/144328 describes a composition of multimodal high density polyethylene which is produced using a Ziegler-Natta catalyst for use in molding applications. A small fraction of ultra-high polyethylene of less than 15% by weight is produced in a third reactor.
• US 2009/0105422 A 1 describes a process for producing a multimodal polyethylene.
• the polymerization is carried out in three cascade reactors, wherein the molecular weight of the polymer in each reactor is controlled by the presence of hydrogen.
• the concentration of the hydrogen in each reactor is reduced subsequently by providing the highest hydrogen concentration in the first reactor and the lowest hydrogen concentration in the third reactor.
• WO 2013/113797 describes a process for polyethylene preparation comprising three main subsequent steps of polymerized ethylene and at least one other ⁇ -olefin to get the polyethylene with, respectively, a lower molecular weight ethylene polymer, a first higher molecular weight ethylene polymer and a second higher molecular weight ethylene polymer in accordance with the sequence of a first reactor, a second reactor and a third reactor.
• Screw caps for example beverage screw caps and other closures, which are in particularly used to cap beverage bottles, especially bottles for carbonated soft drinks, are known in the art.
• polyethylene compositions for preparing such screw caps are known in the art.
• WO 2009/077142 A1 discloses a polyethylene molding composition for producing injection-molded screw caps and closures, in particular for use together with containers for carbonated beverage products.
• WO 2007/003530 A1 discloses polyethylene molding compositions for producing injection-molded finished parts.
• the composition is described to be suitable for producing, for example, closures and bottles. Further described is a use of a multimodal polyethylene composition.
• U.S. Pat. No. 8,759,448 B2 is related to a polyethylene molding composition having a multimodal molecular weight distribution. It is proposed to use the disclosed composition for preparing caps and closures, transport packaging, houseware and thin wall packaging applications.
• EP 2365995 B1 discloses a multimodal polyethylene composition and the use thereof for preparing a single-piece bottle cap.
• the multimodal polyethylene composition add nucleating agent to get faster crystallization rate and altered stress cracking resistance.
• a reactor system for a multimodal polyethylene polymerization process comprising;
• the depressurization equipment allows to adjust the operating pressure in the hydrogen removal unit to a pressure in the range of 103-145 kPa (abs), preferably 104-130 kPa (abs), most preferably 105 to 115 kPa (abs).
• the hydrogen removal unit further contains a stripping column for the separation of hydrogen and a liquid diluent.
• the object is further achieved by a process for producing a multimodal polyethylene composition in an inventive reactor system, comprising (in this sequence);
• step (c) polymerizing ethylene and optionally C4-12 ⁇ -olefin comonomer in the second reactor in the presence of a catalyst system, selected from Ziegler-Natta catalyst or metallocene, and in the presence of hydrogen in an amount obtained in step (b) to obtain a first high molecular weight polyethylene having a weight average molecular weight of more than 150,000 to 1,000,000 g/mol or a first ultra high molecular weight polyethylene having a weight average molecular weight of more than 1,000,000 to 5,000,000 g/mol in the form of a homopolymer or a copolymer and transferring a resultant mixture to the third reactor; and
• a catalyst system selected from Ziegler-Natta catalyst or metallocene
• “Substantial absence” in this regard means that hydrogen is only comprised in the third reactor in an amount which cannot be avoided by technical means.
• the slurry mixture obtained from the first reactor and subjected to the step of removing hydrogen in the hydrogen removal unit contains all of the solid and liquid constituents obtained in the first reactor, in particular the low molecular weight polyethylene or the medium molecular weight polyethylene. F ore, the slurry mixture obtained from the first reactor is saturated with hydrogen regardless the amount of hydrogen used in the first reactor.
• the removing is removing of 98.0 to 99.8% by weight of the hydrogen, and more preferable 98.0 to 99.5% by weight, most preferred 98.0 to 99.1.
• the ⁇ -comonomer comprised in the second reactor and/or in the third reactor is selected from 1-butene and/or 1-hexene.
• the operation pressure of the hydrogen removal unit is in the range of 103-145 kPa (abs) and more preferably 104-130 kPa (abs), most preferred 105 to 115 kPa (abs).
• step (a) results in the low molecular weight polyethylene or medium molecular weight polyethylene
• step (c) results in high molecular weight polyethylene or the ultra high molecular weight polyethylene
• step (d) results in high molecular weight polyethylene or the ultra high molecular weight polyethylene.
• the weight average molecular weight (Mw) of the low molecular weight polyethylene, the medium molecular weight polyethylene, the high molecular weight polyethylene and the ultra high molecular weight polyethylene described herein are in the range of 20,000-90,000 g/mol (low), more than 90,000-150,000 g/mol (medium), more than 150,000-1,000,000 g/mol (high) and more than 1,000,000-5,000,000 g/mol (ultra high), respectively.
• the molecular weight distribution of the multimodal polyethylene composition is from 10 to 60, preferably 10 to 25, preferably 10 to 20, determined by Gel Permeation Chromatography;
• the isothermal crystallization half-time of the multimodal polyethylene composition at temperature of 123° C. is 7 min or less, preferably 6 min or less, preferably 2-6 min, according to Differential Scanning Calorimetry;
• a spiral flow length at a temperature of 220° C. is at least 200 mm, preferably 250-400 mm.
• the spiral flow length at a temperature of 220° C. is 250-370 mm.
• the multimodal polyethylene composition has a weight average molecular weight from 80,000 to 1,300,000 g/mol, preferably 80,000 to 250,000 g/mol, preferably 80,000 to 200,000 g/mol, measured by Gel Permeation Chromatography.
• the multimodal polyethylene composition has a number average molecular weight from 5,000 to 30,000 g/mol, preferably 5,000 to 25,000 g/mol, preferably 6,000 to 20,000 g/mol, measured by Gel Permeation Chromatography.
• the multimodal polyethylene composition has a Z average molecular weight from 700,000 to 6,000,000 g/mol, preferably 700,000 to 2,500,000 g/mol, preferably 700,000 to 2,000,000 g/mol, and more preferably 700,000 to 1,500,000 g/mol measured by Gel Permeation Chromatography.
• the multimodal polyethylene composition has a density 0.950 to 0.965 g/cm 3 , preferably 0.953 to 0.960 g/cm 3 , according to ASTM D 1505 and/or MI 2 from 0.1 to 20 g/10 min, preferably from 0.3 to 17 g/10 min, according to ASTM D 1238.
• the object is further achieved by a screw cap comprising the multimodal polyethylene composition according to the invention.
• a screw cap (or screw closure) is a mechanical device which is screwed on and off a “finish” on a container. It must be engineered to provide an effective seal (and barrier), to be compatible with the contents, to be easily opened by the consumer, often to be recloseable, and to comply with product and package.
• a screw cap is a common type of closure for bottles, jars and tubes.
• the screw cap is obtained by injection molding or compression molding.
• the screw cap substantially comprises the inventive multimodal polyethylene composition, which means that the screw cap does comprise further constituents only in amounts which do not affect the cap performances regarding processability (in particular cycle time), flowability, stiffness and stress crack resistance.
• the screw cap is consisting of the inventive multimodal polyethylene composition.
• the inventive process and the inventive multimodal polyethylene composition “comprising” is “consisting of”.
• parts by weight is “percent by weight”.
• the invention concerns a reactor system for multimodal polyethylene polymerization.
• the system comprises a first reactor, a second reactor, a third reactor and a hydrogen removal unit placed between the first reactor and the second reactor.
• the hydrogen depleted polyethylene from the first reactor affects the polymerization of high molecular weight in the subsequent reactors.
• high molecular weight leads to improved mechanical properties of polyethylene that is the advantage for various product application includes injection molding, blow molding and extrusion.
• the catalyst for producing the multimodal polyethylene resin of this invention is selected from a Ziegler-Natta catalyst, a single site catalyst including metallocene-bases catalyst and non- metallocene-bases catalyst or chromium based might be used, preferably conventional Ziegler-Natta catalyst or single site catalyst.
• the catalyst is typically used together with cocatalysts which are well known in the art.
• Innert hydrocarbon is preferably aliphatic hydrocarbon including hexane, isohexane, heptane, isobutane.
• hexane most preferred n-hexane
• Coordination catalyst, ethylene, hydrogen and optionally ⁇ -olefin comonomer are polymerized in the first reactor.
• the entire product obtained from the first reactor is then transferred to the hydrogen removal unit to remove 98.0 to 99.8% by weight of hydrogen, unreacted gas and some volatiles before being fed to the second reactor to continue the polymerization.
• the polyethylene obtained from the second reactor is a bimodal polyethylene which is the combination of the product obtained from the first reactor and that of the second reactor. This bimodal polyethylene is then fed to the third reactor to continue the polymerization.
• the final multimodal (trimodal) polyethylene obtained from the third reactor is the mixture of the polymers from the first, the second and the third reactor.
• the polymerization in the first, the second and the third reactor is conducted under different process conditions. These can be the variation in concentration of ethylene and hydrogen in the vapor phase, temperature or amount of comonomer being fed to each reactor. Appropriate conditions for obtaining a respective homo- or copolymer of desired properties, in particularly of desired molecular weight, are well known in the art. The person skilled in the art is enabled on basis of his general knowledge to choose the respective conditions on this basis. As a result, the polyethylene obtained in each reactor has a different molecular weight. Preferably, low molecular weight polyethylene or medium molecular weight polyethylene is produced in the first reactor, while high molecular weight polyethylene or ultra high molecular weight polyethylene is produced in the second and third reactor respectively.
• first reactor refers to the stage where the low molecular weight polyethylene (LMW) or the medium molecular weight polyethylene (W) is produced.
• second reactor refers to the stage where the first high or ultra high molecular weight polyethylene (HMW1) is produced.
• third reactor refers to the stage where the second high molecular weight polyethylene or ultra high molecular weight (HMW2) is produced.
• LMW refers to the low molecular weight polyethylene polymer polymerized in the first reactor having a weight average molecular weight (Mw) of 20,000-90,000 g/mol.
• LMW refers to the medium molecular weight polyethylene polymer polymerized in the first reactor having a weight average molecular weight (Mw) of more than 90,000-150,000 g/mol.
• HMW1 refers to the high or ultra high molecular weight polyethylene polymer polymerized in the second reactor having a weight average molecular weight w)of more than 150,000 to 5,000,000 g/mol.
• HMW2 refers to the high or ultra high molecular weight polyethylene polymer polymerized in the third reactor having the weight average molecular weight (Mw) of more than 150,000 to 5,000,000 g/mol .
• the LMW or MMW is produced in the first reactor in the absence of comonomer in order to obtain a homopolymer.
• ethylene is polymerized in the first reactor in the absence of comonomer in order to obtain high density LMW polyethylene or MMW polyethylene having density >0.965 g/cm 3 and MI 2 in the range of 10 to 1000 g/10 min for LMW and 0.1 to 10 g/10 min for MMW.
• the polymerization conditions are controlled and adjusted.
• the temperature in the first reactor ranges from 70-90° C., preferably 80-85° C.
• Hydrogen is fed to the first reactor so as to control the molecular weight of the polyethylene.
• the first reactor is operated at pressure between 250 and 900 kPa, preferably 400-850 kPa.
• An amount of hydrogen present in the vapor phase of the first reactor is in the range of 0.1-95% by mole, preferably 0.1-90% by mol.
• the slurry obtained from the first reactor containing LMW or MMW polyethylene preferably in hexane is transferred to a hydrogen removal unit which may have a flash drum connected with depressurization equipment preferably including one or the combination of vacuum pump, compressor, blower and ejector where the pressure in the flash drum is reduced so that volatile, unreacted gas, and hydrogen are removed from the slurry stream.
• the operating pressure of the hydrogen removal unit typically ranges from 103-145 kPa (abs), preferably 104-130 kPa (abs) in which 98.0 to 99.8% by weight of hydrogen can be removed, preferably 98.0 to 99.5% by weight and most preferred 98.0 to 99.1% by weight.
• the polymerization conditions of the second reactor are notably different from that of the first reactor.
• the temperature in the second reactor ranges from 65-90° C., preferably 68-80° C.
• the molar ratio of hydrogen to ethylene is not controlled in this reactor since hydrogen is not fed into the second reactor.
• Hydrogen in the second reactor is the hydrogen left over from the first reactor that remains in slurry stream after being flashed at the hydrogen removal unit.
• Polymerization pressure in the second reactor ranges from 100-3000 kPa, preferably 150-900 kPa, ore preferably 150-400 kPa.
• Hydrogen removal is the comparison result of the amount of the hydrogen present in the slurry mixture before and after passing through the hydrogen removal unit.
• the calculation of hydrogen removal is performed according to the measurement of gas composition in the first and the second reactor by gas chromatography.
• slurry from the hydrogen removal unit is transferred to the second reactor to continue the polymerization.
• ethylene can be polymerized with or without ⁇ -olefin comonomer to form HMW1 polyethylene in the presence of the LMW polyethylene or MMW polyethylene obtained from the first reactor.
• the ⁇ -olefin comonomer that is useful for the copolymerization includes C 4-12 , preferably 1-butene and 1-hexene.
• the slurry obtained is transferred to the third reactor to continue the polymerization.
• the HMW2 is produced in the third reactor by copolymerizing ethylene with optionally ⁇ -olefin comonomer at the presence of LMW or MMW and HWM1 obtained from the first and second reactor.
• the ⁇ -olefin comonomer that is useful for the copolymerization include C 4-12 , preferably 1-butene and/or 1-hexene.
• the polymerization conditions are controlled and adjusted.
• the polymerization conditions of the third reactor are notably different from the first and second reactor.
• the temperature in the third reactor ranges from 68-90° C. preferably 68-80° C.
• Hydrogen is fed to the third reactor so as to control the molecular weight of polyethylene.
• Polymerization pressure in the third reactor ranges from 150-900 kPa, preferably 150-600 kPa, and is controlled by the addition of inert gas such as nitrogen.
• the amount of LMW or MMW present in the multimodal polyethylene composition of the present invention is 30-65 parts by weight.
• HMW1 present in the polyethylene of the present invention is 5-40 p by weight and HMW2 present in the polyethylene of the present invention is 10-60 parts by weight. It is possible that HMW1>HMW2 or HMW1 ⁇ HMW2 depending on the polymerization conditions employed.
• the final (free-flow) multimodal polyethylene composition is obtained by separating hexane from the slurry discharged from the third reactor.
• the resultant polyethylene powder may then be mixed with antioxidants and optionally additives before being extruded and granulated into pellets.
• MI Melt flow index
• Density of polyethylene was measured by observing the level to which a pellet sinks in a liquid column gradient tube, in comparison with standards of known density. This method is determination of the solid plastic after annealing at 120° C. follow ASTM D 1505.
• Molecular weight and Polydispersity index (PDI): The weight average molecular weight (Mw), the number average molecular weight (Mn) and the Z average molecular weight (M Z ) in g/mol in g/mol were analysed by gel permeation chromatography (GPC). Polydispersity index was calculated by Mw/Mn. Around 8 mg of sample was dissolved in 8 ml of 1,2,4-trichlorobenzene at 160° C. for 90 min. Then the sample solution, 200 ⁇ l, was injected into the high temperature GPC with IR5, an infared detector (Polymer Char, Spain) with flow rate of 0.5 ml/min at 145° C. in column zone and 160° C. in detector zone. The data was processed by GPC One® software, Polymer Char, Spain.
• Intrinsic Viscosity The test method covers the determination of the dilute solution viscosity of polyethylene at 135° C. or an ultra high molecular weight polyethylene (UHMWPE) at 150° C.
• the polymeric solution was prepared by dissolving polymer in Decalin with 0.2% wt/vol stabilizer (Irganox 1010 or equivalent). The details are given for the determination of IV according to ASTM D 2515.
• Comonomer content The comonomer content was determined by high resolution 13 C-NMR. 13C-NMR spectra were recorded by 500 MHz ASCENDTM, Bruker, with cryogenic 10 mm probe. TCB was used as major solvent with TCE-d2 as locking agent in the ratio of 4:1 by volume. The NMR experiments were carried on at 120° C., and the inverse gate 13C (zgig) of pulse program with 90° for pulse angle were used. The delay time (D1) was set to 10 seconds for full-spin recovery.
• Crystallinity The crystallinity is frequently used for characterization by Differential Scanning Calorimetry (DSC) follow ASTM D 3418. Samples were identified by peak temperature and enthalpy, as well as the % crystallinity was calculated from the peak area.
• Shear Thinning Index It gives an indication as molecular weight distribution of material. A common measurement runs viscosity at 190° C. using Dynamic rheometer using 25 mm diameter plate and plate geometry 1 mm gap. SHI (1/100) was calculated by viscosities at a constant shear stress at 1 kPa and 100 kPa. Generally materials have high SHI means better flowability of material.
• Viscosity at angular frequency 0.01 [1s] ( ⁇ 0.01 ) Rheological parameters are determined by using controlled stress rheometer model MCR-301 from Anton-Paar. The geometry is Plate-Plate 25 mm diameter at the measurement gap 1 mm. The dynamic oscillatory shear performs at angular frequency ( ⁇ ) 0.01-600 rad/s at 190° C. under nitrogen atmosphere. The sample preparation is performed to circular disk 25 mm by compression molding at 190° C. Viscosity at 0.01 [1/s] ( ⁇ 0.01 ) is obtained from complex viscosity at a specific shear rate 0.01 [1/s].
• Isothermal Crystallization Half-Time (ICHT) and Crystal growth rate constant (K) The isothermal crystallization half-time at 123° C. was measured by differential scanning calorimetry (DSC) to determine the crystallization rate of the sample. The sample was heated from 30° C. to 200° C. at a heating rate of 50° C./min and held for 5 min. Then, it was cooled down to 123° C. at cooling rate 50° C./min and held for 60 min. The crystal growth rate constant (K) and n were determined by fitting the data of logarithmic expression of Avrami equation.
• Spiral flow length Spiral flow test was carried out by Fanuc Roboshot S2000i 100B injection molding machine (Screw diameter 36 mm) with spiral mould at temperature 220° C. and constant injection pressure 1000 bar. The thickness of specimen is 1 mm. After conditioning sample for 24 hr, the spiral flow length (mm) was measured.
• Charpy impact strength The compressed specimen according to ISO 293 was prepared. Charpy impact strength is determined according to ISO179 at 23° C. and shown in the unit kJ/m 2 .
• Flexural Modulus The compressed specimen according to ISO 1872-2 was prepared and performed the test follow ISO 178. The flexural tests were done using a universal testing machine equipped with three point bending fixture.
• FNCT Full Notch Creep Test
• the medium or high density polyethylene preparation was carried out in three reactors in series. Ethylene, hydrogen, hexane, catalyst and TEA (triethyl aluminum) co-catalyst were fed into a first reactor in the amounts shown in Table 1. A commercial available Ziegler-Natta catalyst was used. The catalyst preparation is for example described in Hungary patent application 0800771r.
• the polymerization in first reactor was carried out to make a low molecular weight polyethylene or medium molecular weight polyethylene. All of polymerized slurry polymer from first reactor was then transferred to a hydrogen removal unit to remove unreacted gas and some of hexane from polymer.
• the operating pressure in the hydrogen removal unit was be varied in a range of 100 to 115 kPa (abs) where residual hydrogen was removed more than 98% by weight but not more than 99.8% by weight from hexane before transferring to a second polymerization reactor.
• Some fresh hexane, ethylene and/or comonomer were fed into second reactor to produce first high molecular weight polyethylene (HMW1).
• All of polymerized polymer from second reactor was fed into the third reactor which produce second high molecular weight polyethylene (HMW2).
• Ethylene, comonomer, hexane and/or hydrogen were fed into the third reactor.
• a homopolymer was produced in first reactor to obtain a low molecular weight portion before transferring such polymer to hydrogen removal unit.
• Reactant mixture was introduced into the hydrogen removal unit to separate the unreacted mixture from the polymer. Residual hydrogen was removed 97.6% by weight when hydrogen removal unit was operated at pressure of 150 kPa (abs).
• the low molecular weight polymer was then transferred to the second reactor to produce a first high molecular weight polymer.
• produced polymer from second reactor was transferred to the third reactor to create a second high molecular weight polymer.
• a copolymerization was carried out by feeding 1-butene as a comonomer.
• Example 1 was carried out in the same manner as Comparative Example 1 except that the hydrogen removal unit was operated at pressure of 115 kPa (abs). The residual of hydrogen from first reactor was removed 98.0% by weight. Characteristic properties of these multimodal polymers are shown in Table 2. As it can be seen, an improvement of stiffness-impact balance was observed when the percentage of removed hydrogen residual increased compared with the properties of Comparative Example 1.
• Example 2 was carried out in the same manner as Comparative Example 1 except that the hydrogen removal unit was operated at pressure of 105 kPa (abs). The residual hydrogen from the first reactor was removed to an extend of 99.1% by weight. The operational of hydrogen removal unit under this pressure leads to an expansion of a polymer properties range. As seen in Table 2, a final melt flow rate of E2 was lower than a final melt flow rate of CE1 resulted in an improvement of Charpy impact while still maintained the flexural modulus.
• Comparative Example 2 was carried out in the same manner as Comparative Example 1 except that the hydrogen removal unit was operated at pressure of 102 kPa (abs). The residual of hydrogen from first reactor was removed to an extend of 99.9% by weight. The operational of hydrogen removal unit under this pressure leads to an expansion of a polymer properties range. As seen in Table 2, the final melt flow rate and a density of CE2 were quite similar to a final melt flow rate and a density of E2. A decay of Charpy impact was showed in CE2 compared to E2.
• a homopolymer was produced in a first reactor to obtain a low molecular weight portion before transferring the polymer to a hydrogen removal unit.
• Reactant mixture was introduced into the hydrogen removal unit to separate the unreacted mixture from the polymer. Hydrogen residual was removed to an extend of 97.9% by weight when hydrogen removal unit was operated at pressure of 150 kPa (abs).
• the low molecular weight polymer was then transferred to a second reactor to produce a first high molecular weight polymer.
• a copolymerization was carried out by feeding 1-butene as a comonomer.
• in-situ bimodal copolymer from second reactor was transferred to a third reactor to create a second high molecular weight copolymer portion. Characteristic properties of this multimodal polymers is shown in Table 2. A significant improvement in Charpy impact at room temperature could be obtained by decreasing a density of final polymer when co-polymer was produced in both the second and the third reactor.
• Example 3 was carried out in the same manner as Comparative Example 3 except that the hydrogen removal unit was operated at pressure of 105 kPa (abs). The residual of hydrogen from first reactor was removed to an extend of 98.8% by weight. The polymer obtained by this process operation had a melt flow rate of 0.195 g/10 min (5 kg loading) lower than such value obtained from CE3. As seen in Table 2, it revealed an improvement of stiffness-impact balance when the percentage of removed hydrogen residual increases compared with the properties of Comparative Example 3.
• a homopolymer was produced in the first reactor to obtain a medium molecular weight portion before transferring such polymer to hydrogen removal unit.
• the hydrogen removal unit was operated at pressure of 105 kPa (abs) to separate the unreacted mixture from the polymer.
• the residual of hydrogen from first reactor was removed to an extend of 98.9% by weight.
• the medium molecular weight polymer was then transferred to the second reactor to produce a first ultra high molecular weight polymer.
• produced polymer from second reactor was transferred to the third reactor to create a second ultra high molecular weight polymer.
• the second and third reactors are operated under hydrogen depleted polyethylene polymerization.
• the processable in-situ ultra high molecular weight polyethylene is produced by this process operation leads to an excellent improvement of Charpy impact strength while still maintained the flexural modulus.
• the conventional UHMWPE with very high IV was known that it was unable to measured MI 21 .
• the inventive example E4 with IV of 9 dl/g shows good melt flow ability beyond the known art.
• Example 6 was carried out in the same manner as Example 4 except that the comonomer feeding in the third ultra high molecular weight polyethylene.
• the polymer produced by this process leads to an excellent improvement of Charpy impact strength while still maintained the flexural modulus.
• the inventive example 6 with IV of 23 dl/g show the high impact strength (one notched impact without break) and flexural modulus as compared to comparative samples, however, the melt flow index is unmeasurable due to high viscosity and high Mw.
• a homopolymer was produced in first reactor to obtain a low molecular weight portion before transferring such polymer to hydrogen removal unit.
• Reactant mixture was introduced into the hydrogen removal unit to separate the unreacted mixture from the polymer. Residual hydrogen was removed 97.6% by weight when hydrogen removal unit was operated at pressure of 150 kPa (abs).
• the low molecular weight polymer was then transferred to the second reactor to produce a first high molecular weight polymer.
• Final, produced polymer from second reactor was transferred to the third reactor to create a second high molecular weight polymer.
• a copolymerization was carried out by feeding 1-butene as a comonomer.
• Table 2 and 3 the final melt flow rate of CE4 were quite similar to a final melt flow rate of E5. A decay of charpy impact and flexural modulus were showed in CE4 compared to E5, even it showed lower density of E5.
• Example 5 was carried out in the same manner as Comparative Example 4 except that the hydrogen removal unit was operated at pressure of 115 kPa (abs). The residual of hydrogen from first reactor was removed to an extend of 98.5% by weight. The polymer obtained by this process operation had a melt flow rate of 48 g/10 min (5 kg loading) lower than such value obtained from CE3. As seen in Table 2, it revealed an improvement of stiffness-impact balance when the percentage of removed hydrogen residual increases compared with the properties of Comparative Example 4.
• Comparative example 5 is a bimodal polyethylene produced from Ziegler-Natta catalyst. The weight ratio between the ethylene homopolymer and the ethylene copolymer is in the range of 45:55 to 55:45.
• a polymer composition comprises a comonomer in an amount of at least 0.40 mol %.
• Comparative example 6 is a commercial multimodal high density polyethylene Hostalen® ACP5331 UVB plus.
• Multimodal polyethylene compositions of inventive examples 7 and 8(E7 and E8) were produced according to the inventive process with the polymerization condition as shown in Table 3.
• the different weight fraction in each reactor was defined and 1-butene was applied as comonomer in the 2 nd and 3 rd reactor components.
• the properties of the invention from inventive examples 7 and 8 (E7 and E7) were compared to the properties of comparative examples 5 and 6 (CE5 and CE6).
• the better processability can be investigated in term of both faster cycle time and higher flowability.
• Faster cycle time was determined by the lower crystallization haft time (ICHT) and higher crystal growth rate (K).
• the inventive examples 5, 7, and 8 show lower ICHT and higher crystal growth rate (K) than comparative examples 4, 5 and 6 (CE4, CE5 and CE6). It is supposed that the ultra high molecular weight produced in the second component following the inventive process can act as a stem for easier nucleation resulting in faster crystallization rate.
• the flowability is normally determined by spiral flow length at temperature 220° C.
• the spiral flow length of inventive example E5 has higher than comparative example 4 (CE4), and inventive examples 7 and 8 (E7 and E8) have higher than comparative examples 5 and 6 (CE5 and CE6), even inventive examples have lower MI than comparative examples.
• the improvement of stiffness compared to CE5 and CE6 were also investigated.
• the multimodal polyethylene composition of these invention examples 7 and 8 (E7 and E8) have better flexural modulus than comparative examples 5 and 6 (CE5 and CE6) and also the invention example 5 (E5) has higher flexural modulus than comparative examples (CE4). Because of the multimodal polyethylene according to this invention contain higher Mz shows a significant improvement in stiffness.
• the multimodal polyethylene according to this invention (E8) still has better stress cracking resistance as measured by FNCT compare to CE5 and CE6.
• the inventive example 7 (E7) showed equivalent FNCT to the bimodal polyethylene (CE5) even at higher density. This indicated that the inventive multimodal polyethylene composition provide better processability and higher stiffness with good balance to stress crack resistance beyond prior The invention enhanced significantly improvement of properties for screw cap and closure.

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