Patent Description:
Packaging industry is constantly in need for packaging materials that will be suitable to preserve the packed material in a desired state without compromising their properties. Polyolefin films, mostly in multilayered form, are widely utilized for that purpose. Polyethylene films in multilayered film structures are one of the most commonly used solutions, which is usually laminated with a film layer made of PET. Current trend in the polyolefin industry, however, is shifting towards to more mono-material solutions, allowing the concept of Design for Recycling (DfR) to be adapted. For that purpose, replacing PET layer with oriented polyethylene film layer and obtaining a full-polyethylene film structure is seen as a promising solution.

<CIT> relates to an oriented multilayer film that can be used as a flexible packaging material, comprising a core layer, a first and a second skin layer, wherein the core layer comprises at least <NUM> wt. -% high density polyethylene (HDPE). Although the film described can be biaxially oriented, it contains different layer structures containing materials other than polyethylene, making it not suitable for design for recycling concept.

<CIT> describes a polyethylene film which can be biaxially oriented comprising high density polyethylene (HDPE) and a hydrocarbon resin. However, this document focuses on improving the moisture barrier properties with the inclusion of the hydrocarbon resin.

<CIT> discloses films for packaging with an improved water vapour transmission rate comprising a multimodal polymer composition.

As a consequence, there remains a need for designing a packaging material that can easily be recycled after its intended use and has required mechanical properties in terms of improved stiffness in order to protect contents of the packaging.

The present invention pertains to a biaxially oriented polyethylene (BOPE) film comprising a polyethylene composition (C) having a density of from <NUM> to <NUM>/m<NUM>, wherein the polyethylene composition comprises:.

wherein the density is determined in accordance with ISO1183 and the melt flow rate MFR<NUM> is determined at a temperature of <NUM> under a load of <NUM> in accordance with ISO1133.

The present invention further pertains to use of the biaxially oriented polyethylene (BOPE) film described herein in packaging articles.

All the terms used herein is to be understood within their general meaning known to the skilled person in the art. In order to be more precise, the following terms will have the meaning as described hereinbelow.

A high density polyethylene (HDPE) is a polymer of ethylene having a density usually ranging between <NUM> and <NUM>/m<NUM>.

A multimodal polymer is a polymer having two or more fractions different from each other in at least one property, such as weight average molecular weight or comonomer content. The molecular weight distribution curve of such multimodal polymers (graph of polymer weight fraction vs. molecular weight) exhibits two or more maxima depending on the modality, or such curve is distinctly broadened in comparison with the curves of individual fractions. When the polymer contains two different fractions, it is called "bimodal".

All the properties of the polymers as described herein are measured in accordance with the methods described in section "Measurement methods", unless otherwise provided.

The biaxially oriented polyethylene (BOPE) film according to the present invention comprises a polyethylene composition (C). The polyethylene composition (C) according to the present invention comprises:.

The polyethylene composition (C) has a density of from <NUM> to <NUM>/m<NUM>, preferably of from <NUM> to <NUM>/m<NUM>.

It is preferred when the polyethylene composition (C) has:.

The polyethylene composition (C) preferably has:.

It is also preferred when the ratio of Mw/Mn of the polyethylene composition (C) ranges from <NUM> to <NUM>, more preferably from <NUM>-<NUM>. The ratio of Mz/Mw is preferably ranging from <NUM> to <NUM>, more preferably from <NUM> to <NUM>.

The polyethylene composition preferably has:.

The melting enthalpy Hm of the polyethylene composition preferably ranging from <NUM> to <NUM> J/g, more preferably from <NUM> to <NUM> J/g.

The BOPE film preferably comprises the polyethylene composition (C) in an amount of equal to or higher than <NUM> wt. -%, more preferably equal to or higher than <NUM> wt. -%, more preferably equal to or higher than <NUM> wt. -%, and more preferably equal to or higher than <NUM> wt. -%, based on the total weight of the BOPE film. In a more preferred embodiment, the BOPE film consists of the polyethylene composition (C).

The polyethylene composition (C) comprises a high density polyethylene (HDPE) in an amount from <NUM> to <NUM> wt. -%, preferably from <NUM> to <NUM> wt. -%, based on the total weight of the polyethylene composition (C).

The HDPE according to the present invention has a density of from <NUM> to <NUM>/m<NUM> and a melt flow rate MFR<NUM> of from <NUM> to <NUM>/<NUM>. In a preferred embodiment, the HDPE has:.

The HDPE according to the present invention comprises at least two fractions:.

In a preferred embodiment, the HDPE is bimodal, meaning that it contains only two polyethylene fractions; the first polyethylene fraction (PE1) and the second polyethylene fraction (PE2).

The HDPE preferably has a comonomer content of from <NUM> to <NUM> mol-%, more preferably from <NUM> to <NUM> mol-%.

The HDPE according to the present invention is preferably a copolymer of ethylene and at least one C<NUM>-C<NUM> alpha-olefin. In particular, C<NUM>-C<NUM> alpha-olefins are preferred, such as propene, <NUM>-butene, <NUM>-hexene, <NUM>-octene, and <NUM>-methyl-<NUM>-pentene. In a most preferred embodiment, HDPE is a copolymer of ethylene and only one C<NUM>-C<NUM> alpha-olefin. Hence it is the most preferred that HDPE is ethylene/<NUM>-butene copolymer.

The HDPE of the present invention comprises a first polyethylene fraction (PE1) in an amount of from <NUM> to <NUM> wt. -%, preferably from <NUM> to <NUM> wt. -%, based on the total weight of the HDPE.

The first polyethylene fraction (PE1) has a density of from <NUM> to <NUM>/m<NUM> and a melt flow rate MFR<NUM> of from <NUM> to <NUM>/<NUM>. In a preferred embodiment, the first polyethylene fraction (PE1) has:.

In a preferred embodiment, the first polyethylene fraction (PE1) is a homopolymer of ethylene; in other words, it does not contain any comonomer units.

The HDPE of the present invention comprises a second polyethylene fraction (PE2) in an amount of from <NUM> to <NUM> wt. -%, preferably from <NUM> to <NUM> wt. -%, based on the total weight of the HDPE.

The second polyethylene fraction (PE2) has a density of from <NUM> to <NUM>/m<NUM> and a melt flow rate MFR<NUM> of from <NUM> to <NUM>/<NUM>. In a preferred embodiment, the second polyethylene fraction (PE2) has:.

In a preferred embodiment, the second polyethylene fraction (PE2) is a copolymer of ethylene and at least one C<NUM>-C<NUM> alpha-olefin. In particular, C<NUM>-C<NUM> alpha-olefins are preferred, such as propene, <NUM>-butene, <NUM>-hexene, <NUM>-octene, and <NUM>-methyl-<NUM>-pentene. In a most preferred embodiment, PE2 is a copolymer of ethylene and only one C<NUM>-C<NUM> alpha-olefin. Hence it is the most preferred that PE2 is ethylene/<NUM>-butene copolymer.

Optionally, the HDPE of the present invention may comprise additives in an amount of from <NUM> to <NUM> wt. -% relative to the total weight of the HDPE. The additives are selected from the group of acid scavengers, antioxidants, anti-blocking agents, UV-stabilizers, anti-scratch agents, mold release agents, lubricants, anti-static agents, pigments, and mixtures thereof.

The polyethylene composition (C) according to the present invention comprises a polyethylene wax in an amount of from <NUM> to <NUM> wt. -%, preferably from <NUM> to <NUM> wt. -%, based on the total weight of the polyethylene composition (C).

The polyethylene wax has a density of from <NUM> to <NUM>/m<NUM>, preferably from <NUM> to <NUM>/m<NUM>, and more preferably from <NUM> to <NUM>/m<NUM>.

It is preferred when the polyethylene wax has:.

The polyethylene wax preferably has one or more, preferably all, of the properties below:.

The polyethylene wax may be produced in a polymerization process in the presence of a catalyst, which could preferably be a Ziegler-Natta catalyst or a metallocene catalyst. Metallocene catalysts are the most preferred.

The polyethylene wax can be an ethylene homopolymer wax or an ethylene random copolymer wax. The ethylene random copolymer wax is preferably a random copolymer of ethylene and C<NUM> to C<NUM> alpha-olefin comonomers. In a more preferred embodiment, the polyethylene wax is an ethylene homopolymer wax.

Commercially available polyethylene waxes may be used; such as Excerex 40800T (Mitsui Chemicals) or Licocene PE4201 (Clariant).

The HDPE of the present invention may be produced by polymerization using conditions which create a multimodal polymer product ideally using a Ziegler Natta catalyst system. Typically, a two or more stage, i.e. multistage, polymerization process is used with different process conditions in the different stages or zones (e.g. different temperatures, pressures, polymerization media, hydrogen partial pressures, etc.). Preferably, the multimodal composition is produced by a multistage polymerization, e.g. using a series of reactors, with optional comonomer addition preferably in only the reactor(s) used for production of the higher/highest molecular weight component(s). A multistage process is defined to be a polymerization process in which a polymer comprising two or more fractions is produced by producing each or at least two polymer fraction(s) in a separate reaction stage, usually with different reaction conditions in each stage, in the presence of the reaction product of the previous stage which comprises a polymerization catalyst. The polymerization reactions used in each stage may involve conventional ethylene homopolymerization or copolymerization reactions, e.g. gas-phase, slurry phase, liquid phase polymerizations, using conventional reactors, e.g. loop reactors, gas phase reactors, batch reactors etc. (see for example <CIT> and <CIT>).

Preferably, the HDPE according to the present invention is a bimodal HDPE prepared in a two-stage polymerization process; a first and a second polymerization stage.

The first polymerization stage produces an ethylene homopolymer or an ethylene copolymer, typically an ethylene homopolymer, which is subsequently fed to the second polymerization stage. The second polymerization stage can produce a further ethylene homopolymer, or an ethylene copolymer, preferably an ethylene copolymer.

The first polymerization stage is preferably a slurry polymerization step.

The slurry polymerization usually takes place in an inert diluent, typically a hydrocarbon diluent such as methane, ethane, propane, n-butane, isobutane, pentanes, hexanes, heptanes, octanes etc., or their mixtures. Preferably the diluent is a low-boiling hydrocarbon having from <NUM> to <NUM> carbon atoms or a mixture of such hydrocarbons. An especially preferred diluent is propane, possibly containing minor amounts of methane, ethane and/or butane.

The ethylene content in the fluid phase of the slurry may be from <NUM> to <NUM> % by mole, preferably from <NUM> to <NUM> % by mole and in particular from <NUM> to <NUM> % by mole. The benefit of having a high ethylene concentration is that the productivity of the catalyst is increased but the drawback is that more ethylene then needs to be recycled than if the concentration was lower.

The temperature in the first polymerization stage is typically from <NUM> to <NUM>. An excessively high temperature should be avoided to prevent partial dissolution of the polymer into the diluent and the fouling of the reactor. The pressure is generally from <NUM> to <NUM> bar, preferably from <NUM> to <NUM> bar.

The slurry polymerization may be conducted in any known reactor used for slurry polymerization. Such reactors include a continuous stirred tank reactor and a loop reactor. It is especially preferred to conduct the slurry polymerization in a loop reactor. In such reactors the slurry is circulated with a high velocity along a closed pipe by using a circulation pump. Loop reactors are generally known in the art and examples are given, for instance, in <CIT>, <CIT>, <CIT>, <CIT> and <CIT>. It is thus preferred to conduct the first polymerization stage as a slurry polymerization in a loop reactor.

The slurry may be withdrawn from the reactor either continuously or intermittently. A preferred way of intermittent withdrawal is the use of settling legs where slurry is allowed to concentrate before withdrawing a batch of the concentrated slurry from the reactor. The use of settling legs is disclosed, among others, in <CIT>, <CIT> and <CIT>. Continuous withdrawal is disclosed, among others, in <CIT>, <CIT>, <CIT> and <CIT>. The continuous withdrawal is advantageously combined with a suitable concentration method, as disclosed in <CIT> and <CIT>. It is preferred to withdraw the slurry from the first polymerization stage continuously.

Hydrogen is typically introduced into the first polymerization stage for controlling the MFR<NUM> of the resultant polymer. The amount of hydrogen needed to reach the desired MFR depends on the catalyst used and the polymerization conditions. The desired polymer properties may be obtained in slurry polymerization in a loop reactor with the molar ratio of hydrogen to ethylene of from <NUM> to <NUM> mol/kmol (or mol/<NUM> mol) and preferably of from <NUM> to <NUM> mol/kmol. The average residence time in the first polymerization stage is typically from <NUM> to <NUM> minutes, preferably from <NUM> to <NUM> minutes. As it is well known in the art the average residence time<IMG> can be calculated from Equation <NUM> below: <MAT>.

Where VR is the volume of the reaction space (in case of a loop reactor, the volume of the reactor, in case of the fluidized bed reactor, the volume of the fluidized bed) and Qo is the volumetric flow rate of the product stream (including the polymer product and the fluid reaction mixture).

The production rate is suitably controlled with the catalyst feed rate. It is also possible to influence the production rate by suitable selection of the monomer concentration. The desired monomer concentration can then be achieved by suitably adjusting the ethylene feed rate.

As a result of the first polymerization stage, the first polyethylene fraction (PE1) is produced.

In the second polymerization stage, ethylene is polymerized, optionally together with at least one alpha-olefin comonomer, in the presence of the catalyst and the ethylene polymer produced in the first polymerization stage, PE1. It will thus be appreciated that the second polymerization stage generates an ethylene polymer, which combines with the ethylene polymer from the first polymerization stage (PE1), to form the HDPE. Preferable comonomers are discussed hereinbefore, however it is noted that it is particularly preferable if the at least one alpha-olefin is butene.

The second polymerization stage is preferably a gas phase polymerization step, i.e. carried out in a gas-phase reactor. Any suitable gas phase reactor known in the art may be used, such as a fluidised bed gas phase reactor.

For gas phase reactors, the reaction temperature used will generally be in the range <NUM> to <NUM> (e.g. <NUM> to <NUM>), the reactor pressure will generally be in the range <NUM> to <NUM> bar, and the residence time will generally be <NUM> to <NUM> hours. The gas used will commonly be a non-reactive gas such as nitrogen or low boiling point hydrocarbons such as propane together with monomer (e.g. ethylene).

A chain transfer agent (e.g. hydrogen) is typically added to the second polymerization stage, preferably in amounts of <NUM> to <NUM> mol of H2/kmol ethylene.

The split between the first polymerization stage and the second polymerization stage (i.e. between the slurry polymerization and the gas phase polymerization) is typically <NUM>:<NUM> to <NUM>:<NUM>, more preferably <NUM>:<NUM> to <NUM>:<NUM>.

As a result of the second polymerization step, a mixture of the first polyethylene fraction PE1 and the second polyethylene fraction PE2 is produced and is called a first polyethylene mixture PEM1.

The polymerization steps discussed above may be preceded by a prepolymerization step. The purpose of the prepolymerization is to polymerize a small amount of polymer onto the catalyst at a low temperature and/or a low monomer concentration. By prepolymerization it is possible to improve the performance of the catalyst in slurry and/or modify the properties of the final polymer. The prepolymerization step is conducted in slurry.

Thus, the prepolymerization step may be conducted in a loop reactor. The prepolymerization is then preferably conducted in an inert diluent, typically a hydrocarbon diluent such as methane, ethane, propane, n-butane, isobutane, pentanes, hexanes, heptanes, octanes etc., or their mixtures. Preferably the diluent is a low-boiling hydrocarbon having from <NUM> to <NUM> carbon atoms or a mixture of such hydrocarbons.

The temperature in the prepolymerization step is typically from <NUM> to <NUM>, preferably from <NUM> to <NUM> and more preferably from <NUM> to <NUM>.

The amount of monomer is typically such that from <NUM> to <NUM> grams of monomer per one gram of solid catalyst component is polymerized in the prepolymerization step. As the person skilled in the art knows, the catalyst particles recovered from a continuous prepolymerization reactor do not all contain the same amount of prepolymer. Instead, each particle has its own characteristic amount which depends on the residence time of that particle in the prepolymerization reactor. As some particles remain in the reactor for a relatively long time and some for a relatively short time, then also the amount of prepolymer on different particles is different and some individual particles may contain an amount of prepolymer which is outside the above limits. However, the average amount of prepolymer on the catalyst typically is within the limits specified above.

The molecular weight of the prepolymer may be controlled by hydrogen as it is known in the art. Further, antistatic additives may be used to prevent the particles from adhering to each other or the walls of the reactor, as disclosed in <CIT> and <CIT>.

The catalyst components are preferably all introduced to the prepolymerization step when a prepolymerization step is present. However, where the solid catalyst component and the cocatalyst can be fed separately it is possible that only a part of the cocatalyst is introduced into the prepolymerization stage and the remaining part into subsequent polymerization stages. Also in such cases it is necessary to introduce so much cocatalyst into the prepolymerization stage that a sufficient polymerization reaction is obtained therein.

It is understood within the scope of the invention, that the amount of polymer produced in the prepolymerization typically lies within <NUM>-<NUM> wt. -% in respect to the final HDPE. Within the scope of the present invention, the split of the prepolymerization is included in the split of the first polymerization stage.

The polymerization is typically conducted in the presence of a Ziegler-Natta polymerization catalyst. Suitable Ziegler-Natta (ZN) catalysts generally comprise at least a catalyst component formed from a transition metal compound of Group <NUM> to <NUM> of the Periodic Table (IUPAC, Nomenclature of Inorganic Chemistry, <NUM>), a metal compound of Group <NUM> to <NUM> of the Periodic Table (IUPAC), optionally a compound of group <NUM> of the Periodic Table (IUPAC), and optionally an internal organic compound, like an internal electron donor. A ZN catalyst may also comprise further catalyst component(s), such as a cocatalyst and optionally external additives.

Suitable ZN catalysts preferably contain a magnesium compound, an aluminum compound and a titanium compound supported on a particulate support.

The particulate support can be an inorganic oxide support, such as silica, alumina, titania, silica-alumina, silica-titania or a MgCl2 based support. Preferably, the support is silica or a MgCl2 based support.

Particularly preferred Ziegler-Natta catalysts are such as described in <CIT>.

If used, the magnesium compound preferably is a reaction product of a magnesium dialkyl and an alcohol. The alcohol is a linear or branched aliphatic monoalcohol. Preferably, the alcohol has from <NUM> to <NUM> carbon atoms. Branched alcohols are especially preferred, and <NUM>-ethyl-<NUM>-hexanol is one example of the preferred alcohols. The magnesium dialkyl may be any compound of magnesium bonding to two alkyl groups, which may be the same or different. Butyl-octyl magnesium is one example of the preferred magnesium dialkyls.

The aluminium compound is a chlorine containing aluminium alkyl. Especially preferred compounds are aluminium alkyl dichlorides and aluminium alkyl sesquichlorides.

The transition metal compound of Group <NUM> to <NUM> is preferably a titanium or vanadium compound, more preferably a halogen containing titanium compound, most preferably chlorine containing titanium compound. An especially preferred titanium compound is titanium tetrachloride.

The catalyst can be prepared by sequentially contacting the carrier with the above mentioned compounds, as described in <CIT> or <CIT>. Alternatively, it can be prepared by first preparing a solution from the components and then contacting the solution with a carrier, as described in <CIT>.

Another group of suitable ZN catalysts contain a titanium compound together with a magnesium halide compound acting as a support. Thus, the catalyst contains a titanium compound and optionally a Group <NUM> compound for example an aluminium compound on a magnesium dihalide, like magnesium dichloride. Such catalysts are disclosed, for instance, in <CIT>, <CIT>, <CIT> and <CIT>.

Suitable activators are group <NUM> metal compounds, typically group <NUM> alkyl compounds and especially aluminium alkyl compounds, where the alkyl group contains <NUM> to <NUM> C-atoms. These compounds include trialkyl aluminium compounds, such as trimethylaluminium, triethylaluminium, tri-isobutylaluminium, trihexylaluminium and tri-n-octylaluminium, alkyl aluminium halides, such as ethylaluminium dichloride, diethylaluminium chloride, ethylaluminium sesquichloride, dimethylaluminium chloride and the like. Especially preferred activators are trialkylaluminiums, of which triethylaluminium, trimethylaluminium and tri-isobutylaluminium are particularly used.

The amount in which the activator is used depends on the specific catalyst and activator. Typically triethylaluminium is used in such amount that the molar ratio of aluminium to the transition metal, like Al/Ti, is from <NUM> to <NUM>, preferably from <NUM> to <NUM> and in particular from about <NUM> to about <NUM> mol/mol.

An optional internal organic compound may be chosen from the following classes: ethers, esters, amines, ketones, alcohols, anhydrides or nitriles or mixtures thereof. Preferably, the optional internal organic compound is selected from ethers and esters, most preferably from ethers. Preferred ethers are of <NUM> to <NUM> carbon-atoms and especially mono, di or multi cyclic saturated or unsaturated ethers comprising <NUM> to <NUM> ring atoms. Typical cyclic ethers suitable in the present invention, if used, are tetrahydrofuran (THF), substituted THF, like <NUM>-methyl THF, di-cyclic ethers, like <NUM>,<NUM>-di(<NUM>-tetrahydrofuryl)propane, <NUM>,<NUM>-di-(<NUM>-furan)-propane, or isomers or mixtures thereof. Internal organic compounds are also often called as internal electron donors.

The manufacture of biaxially oriented films is well-known (e.g. <NPL>). The person skilled in the art can apply his/her knowledge of BOPP film production to the manufacture of the BOPE films of the invention. The films of the invention may be manufactured by any known technology, such as the double bubble, tenter frame or spontaneous process.

In a typical process, the components of the film are initially mixed and melted within an extruder. The temperature within the extruder is conventional and will be sufficient to ensure melting of the components. The extrudate is cast to form a cast film (or flat film) which is then cooled. The film should ideally be cooled to a temperature of less than <NUM> before any reheating process is begun. The film is then reheated and stretching is begun. The temperature during the stretching phase may vary and may decrease as the stretching process continues. The reheat temperature in this first step is defined as the temperature at the start of the stretching process. Once stretching in the machine direction is complete, the film is annealed. This maintains the MDO film structure for the TD stretch. Reheating for the second stretching phase is carried out and again, the temperature can vary during the stretching phase. The reheat temperature in this second step is defined therefore as the temperature at the start of the second stretch procedure. Finally, the film is allowed to cool.

As mentioned hereinabove, the BOPE film preferably comprises the polyethylene composition (C) in an amount of equal to or higher than <NUM> wt. -%, more preferably equal to or higher than <NUM> wt. -%, more preferably equal to or higher than <NUM> wt. -%, and more preferably equal to or higher than <NUM> wt. -%, based on the total weight of the BOPE film. In a more preferred embodiment, the BOPE film consists of the polyethylene composition (C). In addition, BOPE film according to the present invention may comprise non-polyethylene based polymers, i.e. polymers other than polyethylenes, from <NUM> to a maximum of <NUM> wt. -%, preferably a maximum of <NUM> wt. -%, hence the BOPE film of the present invention is made substantially of polyethylene-based materials, in order to ensure design for recycling.

In a preferred embodiment, the BOPE film according to the present invention exhibits improved mechanical properties, in terms of tensile modulus in both machine and transverse directions. According to this embodiment, the BOPE film preferably has:.

The BOPE film of the invention ideally has a stretch ratio in the machine direction (MD) and/or transverse direction (TD) of from <NUM> times to <NUM> times, more preferably from <NUM> to <NUM> times.

The BOPE film according to the present invention preferably has a thickness of from <NUM> to <NUM>, more preferably from <NUM> to <NUM>, and most preferably from <NUM> to <NUM>.

The BOPE film according to the present invention may be a monolayer or a multilayer film. Multilayer film may comprise <NUM> or more layers, such as <NUM>, <NUM>, <NUM> or more layers. Preferably, the BOPE film is a monolayer film.

The BOPE film according to the present invention may be used for the production of packaging articles like bags, pouches, labels or lids, or other technical applications like banknotes. The BOPE film of the present invention is preferably used for applications related to food packaging.

The density was measured according to ISO1183, where the samples were prepared according to ISO1872-<NUM>.

The melt flow rates were measured at a temperature of <NUM> with a load of <NUM> for MFR<NUM> and of <NUM> for MFR<NUM> according to ISO1133.

MFR values for the first polyethylene fraction (PE1) was directly measured after the reaction in the loop reactor, while the values for the second polyethylene fraction (PE2) was calculated using the formula (I) below: <MAT> wherein.

Flow Rate Ratio, FRR, is a ratio between MFR values at different loads. For instance, FRR21/<NUM> is a ratio between MFR<NUM> and MFR<NUM>.

The weight average molecular weight Mw, the number average molecular weight Mn and the z-average molecular weight Mz were determined by Gel Permeation Chromatography (GPC) according to ISO <NUM>-<NUM>:<NUM>, ISO <NUM>-<NUM>:<NUM>, ISO <NUM>-<NUM>:<NUM> and ASTM D <NUM>-<NUM> using the following formulas: <MAT> <MAT> <MAT>.

For a constant elution volume interval ΔVi, where Ai, and Mi are the chromatographic peak slice area and polyolefin molecular weight (Mw), respectively associated with the elution volume, Vi, where N is equal to the number of data points obtained from the chromatogram between the integration limits.

A high temperature GPC instrument, equipped with either infrared (IR) detector (IR4 or IR5 from PolymerChar (Valencia, Spain), equipped with <NUM> x Agilent-PLgel Olexis and 1x Agilent-PLgel Olexis Guard columns was used. As the solvent and mobile phase <NUM>,<NUM>,<NUM>-trichlorobenzene (TCB) stabilized with <NUM>/L <NUM>,<NUM>-Di tert butyl-<NUM>-methyl-phenol) was used. The chromatographic system was operated at <NUM> and at a constant flow rate of <NUM>/min. <NUM>µL of sample solution was injected per analysis. Data collection was performed using either Agilent Cirrus software version <NUM> or PolymerChar GPC-IR control software.

The column set was calibrated using universal calibration (according to ISO <NUM>-<NUM>:<NUM>) with <NUM> narrow MWD polystyrene (PS) standards in the range of <NUM>,<NUM>/mol to <NUM><NUM>/mol. The PS standards were dissolved at room temperature over several hours. The conversion of the polystyrene peak molecular weight to polyolefin molecular weights is accomplished by using the Mark Houwink equation and the following Mark Houwink constants: <MAT> <MAT> <MAT>.

All samples were prepared in the concentration range of <NUM>,<NUM> -<NUM>/ml and dissolved at <NUM> for <NUM> hours for PP or <NUM> hours for PE under continuous gentle shaking.

Melting temperaure Tm, crystallization temperature Tc and melting enthalpy Hm were measured with a TA Instrument Q2000 differential scanning calorimetry (DSC) on <NUM> to <NUM> samples. DSC is run according to ISO <NUM> / part <NUM> / method C2 in a heat / cool / heat cycle with a scan rate of <NUM>/min in the temperature range of -<NUM> to +<NUM>. Crystallization temperature Tc was determined from the cooling step, while melting temperature Tm and melting enthalpy Hm are determined from the second heating step.

Tensile modulus in machine direction (MD) and in transverse direction (TD) were measured on a BOPE film, with a thickness of <NUM>, as <NUM>% secant modulus with <NUM>/min test speed and <NUM> gauge length according to ASTM D882.

Quantitative <NUM>C{<NUM>H} NMR spectra recorded in the molten-state using a Bruker Advance III <NUM> NMR spectrometer operating at <NUM> and <NUM> for <NUM>H and <NUM>C respectively. All spectra were recorded using a <NUM>C optimised <NUM> magic-angle spinning (MAS) probehead at <NUM> using nitrogen gas for all pneumatics. Approximately <NUM> of material was packed into a <NUM> outer diameter zirconia MAS rotor and spun at <NUM>. This setup was chosen primarily for the high sensitivity needed for rapid identification and accurate quantification. {klimke06, parkinson07, castignolles09} Standard single-pulse excitation was employed utilising the NOE at short recycle delays {pollard04, klimke06} and the RS-HEPT decoupling scheme {fillip05,griffin07}. A total of <NUM> (<NUM>) transients were acquired per spectra.

Quantitative <NUM>C{<NUM>H} NMR spectra were processed, integrated and relevant quantitative properties determined from the integrals. All chemical shifts are internally referenced to the bulk methylene signal (δ+) at <NUM> ppm.

The amount of ethylene was quantified using the integral of the methylene (δ+) sites at <NUM> ppm accounting for the number of reporting sites per monomer: <MAT> the presence of isolated comonomer units is corrected for based on the number of isolated comonomer units present: <MAT> where B and H are defined for their respective comonomers. Correction for consecutive and non-consecutive commoner incorporation, when present, is undertaken in a similar way.

Characteristic signals corresponding to the incorporation of <NUM>-butene were observed and the comonomer fraction calculated as the fraction of <NUM>-butene in the polymer with respect to all monomer in the polymer: <MAT>.

The amount isolated <NUM>-butene incorporated in EEBEE sequences was quantified using the integral of the *B2 sites at <NUM> ppm accounting for the number of reporting sites per comonomer: <MAT>.

The amount consecutively incorporated <NUM>-butene in EEBBEE sequences was quantified using the integral of the ααB2B2 site at <NUM> ppm accounting for the number of reporting sites per comonomer: <MAT>.

The amount non consecutively incorporated <NUM>-butene in EEBEBEE sequences was quantified using the integral of the ββB2B2 site at <NUM> ppm accounting for the number of reporting sites per comonomer: <MAT>.

Due to the overlap of the *B2 and *βB2B2 sites of isolated (EEBEE) and non-consecutivly incorporated (EEBEBEE) <NUM>-butene respectively the total amount of isolated <NUM>-butene incorporation is corrected based on the amount of non-consecutive <NUM>-butene present: <MAT>.

The total <NUM>-butene content was calculated based on the sum of isolated, consecutive and non-consecutively incorporated <NUM>-butene: <MAT>.

The mole percent comonomer incorporation is calculated from the mole fraction: <MAT>.

The high density polyethylene (HDPE) used in both the inventive and comparative examples is produced in a pilot plant configured to operate as prepolymerization - loop - gas phase reactor using a Ziegler-Natta catalyst whose details are disclosed in <CIT>. The conditions for the reaction are presented in Table <NUM>.

The HDPE obtained was pelletized with <NUM> ppm Irganox <NUM> (supplied by BASF), <NUM> ppm Irgafos <NUM> (supplied by BASF), <NUM> ppm calcium stearate (CEASIT FI, supplied by Baerlocher) in a twin screw extruder. The properties presented in Table <NUM> below were measured on these compositions.

Polyethylene wax used in the inventive example is a commercially available product supplied by Mitsui Chemicals having the name of Excerex™ 40800T. The mentioned PE wax has a density of <NUM>/m<NUM>, a weight average molecular weight Mw of <NUM>/mol, an Mw/Mn ratio of <NUM>, a melting temperature Tm of <NUM>, a crystallization temperature Tc of <NUM> and a melting enthalpy Hm of <NUM> J/g.

Polyethylene compositions (C) for the inventive example (IE) and the comparative example (CE) are prepared with the recipes provided in Table <NUM>, which also shows the properties of the composition (C) that were measured.

Biaxially oriented polyethylene (BOPE) films of IE and CE were prepared on a Karo <NUM> lab scale stretch facility. Sheet before stretching was made from as lab scale cast line, with a chill roll temperature of <NUM>. The initial sheet thickness was controlled according to the maximum stretch ratio to reach the final film thickness of <NUM>. The stretch conditions, such as reheating time and stretch temperature are tuned by a person skilled in the art. The target stretch ratio was <NUM> x <NUM> in MD/TD.

The properties of the BOPE films produced are presented in Table <NUM> below.

Claim 1:
A biaxially oriented polyethylene (BOPE) film comprising a polyethylene composition (C) having a density of from <NUM> to <NUM>/m<NUM>, wherein the polyethylene composition comprises:
a) <NUM>-<NUM> wt.-%, based on the total weight of the polyethylene composition (C), of a high density polyethylene (HDPE) with a density of from <NUM> to <NUM>/m<NUM>, and a melt flow rate MFR<NUM> of from <NUM> to <NUM>/<NUM>, comprising at least two fractions:
a1) <NUM>-<NUM> wt.-%, based on the total weight of the HDPE, of a first polyethylene fraction (PE1) with a density of from <NUM> to <NUM>/m<NUM>, and a melt flow rate MFR<NUM> of from <NUM> to <NUM>/<NUM>, and
a2) <NUM>-<NUM> wt.-%, based on the total weight of the HDPE, of a second polyethylene fraction (PE2) with a density of from <NUM> to <NUM>/m<NUM>, and a melt flow rate MFR<NUM> of from <NUM> to <NUM>/<NUM>,
b) <NUM>-<NUM> wt.-%, based on the total weight of the polyethylene composition (C), of a polyethylene wax having a density of from <NUM> to <NUM>/m<NUM>;
wherein the density is determined in accordance with ISO1183 and the melt flow rate MFR<NUM> is determined at a temperature of <NUM> under a load of <NUM> in accordance with ISO1133.