Patent Description:
Polymer films are widely used in packaging. These films must obviously protect the contents of the package from damage and the environment.

Especially polyethylene based films are widely used in packaging due to their excellent cost/performance ratios. However, due to increasing demands on the needs of the films, multilayer packaging is typically employed utilising different types of polymers.

One classical combination are polyester (e.g.PET)-polyolefin laminates. Whilst these can offer attractive properties, the recycling of such materials is difficult. Therefore, making the materials pure is preferred. In that manner, a packaging with 'mono-materials' is really appreciated. However, this imposes higher requirements on the performance of materials themselves. There is thus a need to produce multilayer films, which offer the opportunity for facile recycling, together with an attractive balance of properties, e.g. a multilayered material with balanced sealing, stiffness, toughness is highly desirable.

To resolve that problem a machine direction oriented polyethylene (MDO PE) or biaxially oriented polyethylene (BOPE) film can be used to replace the PET film, which is often employed due to its attractive properties. HOPE offers a good alternative to PET in terms of stiffness and thermal resistance. The resulting material comprises polyethylene only and is hence fully mechanically recycled.

<CIT> describes a multilayer film, comprising a machine direction oriented (MDO) substrate and a sealant, wherein the substrate has at least three layers. The core layer is described to comprise two polyethylenes and at least one of the other layers comprises a third polyethylene.

<CIT> relates to machine direction oriented polymer films wherein at least one layer comprises an ethylene-based polymer having a particular set of properties.

<CIT> discloses a recyclable multilayer structure comprising (i) a first polyethylene layer as a first external layer, said first polyethylene layer being oriented in only in the machine direction and is formed from at least three layers; (ii) a second PE external layer; (iii) a core layer made of a copolymer of ethylene and vinyl alcohol (EVOH); and (iv) a tie layer on each side of the EVOH layer, characterised in that the tie layers comprise one or more copolymers of ethylene.

The present inventors have unexpectedly found that an uniaxially oriented film comprising at least two layers (A), being skin layers (SKL-<NUM> and SKL-<NUM>), and one layer (B), whereby the skin layers (SKL) are based on specific multimodal metallocene catalysed HDPEs and layer (B) is based on a multimodal Ziegler-Natta catalysed linear low density polyethylene, possess an attractive balance of mechanical, e.g. tensile modulus, and optical properties.

The present invention is therefore directed to an uniaxially oriented multilayered polyethylene film comprising at least two layers (A), being skin layers (SKL-<NUM> and SKL-<NUM>), sandwiching a layer (B), being a core layer (CL), wherein.

Advantageous embodiments of the uniaxially oriented multilayered film in accordance with the present invention are specified in the dependent claims <NUM> to <NUM>. The present invention further relates in accordance with claim <NUM> to the use of the article according to the present invention as packaging material.

A metallocene-catalysed (linear low density or high density) polyethylene is defined in this invention as a (linear low density or high density) polyethylene copolymer, which has been produced in the presence of a metallocene catalyst.

A Ziegler-Natta-catalysed linear low density polyethylene is defined in this invention as a linear low density polyethylene copolymer, which has been produced in the presence of a Ziegler-Natta catalyst.

For the purpose of the present invention the metallocene-catalysed and the Ziegler-Natta catalysed linear low density polyethylene may consist of a polymer component (A) and a polymer component (B) which means that the polymer is produced in an at least <NUM>-stage sequential polymerization process, wherein first component (A) is produced and component (B) is then produced in the presence of component (A) in a subsequent polymerization step, yielding the metallocene-catalysed or the Ziegler-Natta catalysed (linear low) density polyethylene or vice versa, i.e. first component (B) is produced and component (A) is then produced in the presence of component (B) in a subsequent polymerization step, yielding the metallocene-catalysed or Ziegler-Natta catalysed (linear low density) polyethylene.

For the purpose of the present invention "high density polyethylene (HDPE) which comprises polyethylene component (A) and polyethylene component (B)" means that the HDPE is produced in an at least <NUM>-stage sequential polymerization process, wherein first component (A) is produced and component (B) is then produced in the presence of component (A) in a subsequent polymerization step, yielding the HDPE or vice versa, i.e. first component (B) is produced and component (A) is then produced in the presence of component (B) in a subsequent polymerization step, yielding the HDPE.

Polyethylenes produced in a multistage process are also designated as "in-situ" or "reactor" blends. The resulting end product consists of an intimate mixture of the polymers from the two or more reactors, the different molecular-weight-distribution curves of these polymers together forming a molecular-weight-distribution curve having a broad maximum or two or more maxima, i.e. the end product is a multimodal polymer mixture.

The term "multimodal" in context of multimodal metallocene-catalysed (linear low density or high density) polyethylene or Ziegler-Natta-catalysed (linear low density) polyethylene means herein multimodality with respect to melt flow rate (MFR) of at least the polyethylene components (A) and (B), i.e. the polyethylene components (A) and (B), have different MFR values. The multimodal polyethylenes can have further multimodality between the polyethylene components (A) and (B) with respect to one or more further properties, like density, comonomer type and/or comonomer content, as will be described later below.

A homopolymer in the context of the present invention may comprise up to <NUM> wt% based on the total weight of the homopolymer of comonomers, preferably up to <NUM> wt%, but may be also free of comonomers.

Where the term "comprising" is used in the present description and claims, it does not exclude other non-specified elements of major or minor functional importance. For the purposes of the present invention, the term "consisting of" is considered to be a preferred embodiment of the term "comprising of". If hereinafter a group is defined to comprise at least a certain number of embodiments, this is also to be understood to disclose a group, which preferably consists only of these embodiments.

The uniaxially oriented multilayered polyethylene film according to the present invention comprises at least two layers (A), being skin layers (SKL-<NUM> and SKL-<NUM>), sandwiching a layer (B), being a core layer (CL).

The skin layers of the film according to the present invention comprise a multimodal metallocene catalysed high density polyethylene (mHDPE).

The multimodal mHDPE has a density (ISO <NUM>) in the range of <NUM> to <NUM>/m<NUM> and a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM> and wherein the multimodal mHDPE comprises at least.

The multimodal metallocene catalysed high density polyethylene (mHDPE) may be a homopolymer or a copolymer, but is preferably an ethylene copolymer. By ethylene homopolymer is meant a polymer comprising at least <NUM> wt%, especially at least <NUM> wt% ethylene monomer units. Thus, the ethylene homopolymer may comprise up to <NUM> wt% comonomer units, but preferably comprises only up to <NUM> wt%, like up to <NUM> wt% or even up to <NUM> wt% only. By ethylene copolymer is meant a polymer the majority by weight of which derives from ethylene monomer units (i.e. at least <NUM> wt% ethylene relative to the total weight of the copolymer). The comonomer contribution preferably is up to <NUM> wt%, more preferably up to <NUM> wt%.

The other copolymerizable monomer or monomers are preferably C3-<NUM>, especially C3-<NUM>, alpha olefin comonomers, particularly singly or multiply ethylenically unsaturated comonomers, in particular C3-<NUM>-alpha olefins such as propene, <NUM>-butene, <NUM>-hexene, <NUM>-octene and <NUM>-methyl-pent-<NUM>-ene. The use of <NUM>-hexene, <NUM>-octene and <NUM>-butene, or mixtures thereof, is particularly preferred, especially <NUM>-hexene and/or <NUM>-butene.

The mHDPE of the invention is multimodal and therefore comprises at least two components. The mHDPE is preferably bimodal. The polymer of the invention thus preferably comprises.

Higher molecular weight hereby means that component (B) has a higher molecular weight and thus lower MFR<NUM> than component (A).

Lower molecular weight hereby means that component (A) has a lower molecular weight and thus higher MFR<NUM> than component (B).

The multimodal mHDPE used according to the present invention has a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) of <NUM> to <NUM>/<NUM>.

Preferably, the mHDPE has a MFR<NUM> of <NUM>/<NUM> or less, more preferably <NUM>/<NUM> or less and even more preferably <NUM>/<NUM> or less. The polymer preferably has a minimum MFR<NUM> of <NUM>/<NUM>, such as at least <NUM>/<NUM>, more preferably at least <NUM>/<NUM>. Thus, particularly suitable ranges of MFR<NUM> are from <NUM> to <NUM>/<NUM>, such as <NUM> to <NUM>/<NUM> or <NUM> to <NUM>/<NUM>.

The MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) of the multimodal mHDPE is preferably in the range of <NUM> to <NUM>/<NUM>, more preferably in the range of <NUM> to <NUM>/<NUM> and most preferably <NUM> to <NUM>/<NUM>.

The multimodal mHDPE used according to the present invention furthermore preferably has a Flow Rate Ratio (FRR) of the MFR<NUM>/MFR<NUM> of at least <NUM>, more preferably of at least <NUM> and even more preferably of at least <NUM>.

Preferably, the Flow Rate Ratio (FRR) of the MFR<NUM>/MFR<NUM> is up to <NUM>, more preferably up to <NUM> and even more preferably up to <NUM>.

Thus, suitable ranges for the FRR are at least <NUM> to <NUM>, preferably at least <NUM> to <NUM> and more preferably at least <NUM> to <NUM>.

Additionally, the multimodal mHDPE used according to the present invention has a density in the range of <NUM> to <NUM>/m<NUM>, preferably of <NUM> to <NUM>/m3 and more preferably of <NUM> to <NUM>/m<NUM>.

The multimodal mHDPE used according to the present invention comprises at least a lower molecular weight component (A) and a higher molecular weight component (B).

In one particularly preferable embodiment, the mHDPE consists of polyethylene components (A) and (B).

The weight ratio of component (A) to component (B) in the multimodal mHDPE is in the range <NUM>:<NUM> to <NUM>:<NUM>, preferably <NUM>:<NUM> to <NUM>:<NUM>, more preferably <NUM>:<NUM> to <NUM>:<NUM>. In some embodiments the ratio may be <NUM> to <NUM> wt% of component (A) and <NUM> to <NUM> wt% of component (B), such as <NUM> to <NUM> wt% of component (A) and <NUM> to <NUM> wt% of component (B), wherein the wt% values are relative to the total weight of the multimodal mHDPE.

In a particularly preferred embodiment, the wt% values for the polyethylene components (A) and (B) add up to <NUM> %.

Each component (A) and component (B) may be an ethylene homopolymer or an ethylene copolymer. The terms "ethylene homopolymer" and "ethylene copolymer" are as defined above.

In a preferred embodiment, the polyethylene component (A) is an ethylene copolymer and component (B) is an ethylene homopolymer.

Preferably, polyethylene component (B) consists of a single ethylene homopolymer. Polyethylene component (A) may consist of a single ethylene copolymer. Alternatively, Polyethylene component (A) may be an ethylene copolymer mixture comprising (e.g. consisting of) a first ethylene copolymer fraction (A-<NUM>) and a second ethylene copolymer fraction (A-<NUM>). Polyethylene component (A) may be unimodal or multimodal. In case polyethylene component (A) is an ethylene copolymer mixture, it is preferable if the comonomer(s) in the first and second ethylene copolymer fractions are the same.

The polyethylene component (A) preferably has a MFR<NUM> in the range of <NUM> to <NUM>/<NUM>, more preferably <NUM> to <NUM>/<NUM>, even more preferably <NUM> to <NUM>/<NUM> and most preferably <NUM> to <NUM>/<NUM>.

The density of the polyethylene component (A) preferably is in the range of <NUM> to <NUM>/m<NUM>, more preferably <NUM> to <NUM>/m<NUM> and even more preferably <NUM> to <NUM>/m<NUM>.

As stated above, in one preferred embodiment the polyethylene component (A) is an ethylene copolymer. Preferred ethylene copolymers employ alpha-olefins (e.g. C3-<NUM> alpha-olefins) as comonomers. Examples of suitable alpha-olefins include <NUM>-butene, <NUM>-hexene and <NUM>-octene. <NUM>-butene is an especially preferred comonomer.

In another embodiment it is further preferred that polyethylene component (A) consists of two fractions, i.e. a first ethylene copolymer fraction (A-<NUM>) and a second ethylene copolymer fraction (A-<NUM>).

It is possible that fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor or vice versa, i.e. fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor. Preferably, fraction (A-<NUM>) is produced first.

The MFR<NUM> and/or the density of fractions (A-<NUM>) and (A-<NUM>) may be the same or may be different from each other.

Thus, the ethylene polymer fraction (A-<NUM>) preferably has a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>, preferably of <NUM> to <NUM>/<NUM>, more preferably of <NUM> to <NUM>/<NUM> and even more preferably of <NUM> to <NUM>/<NUM>.

The ethylene polymer fraction (A-<NUM>) preferably has a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>, preferably of <NUM> to <NUM>/<NUM>, more preferably of <NUM> to <NUM>/<NUM> and most preferably of <NUM> to <NUM>/<NUM>.

Preferably, the MFR<NUM> of fraction (A-<NUM>) is higher than the MFR<NUM> of fraction (A-<NUM>).

The density of the ethylene polymer fraction (A-<NUM>) preferably is in the range of <NUM> to <NUM>/m<NUM>, more preferably <NUM> to <NUM>/m<NUM> and even more preferably <NUM> to <NUM>/m<NUM>.

The ethylene polymer fraction (A-<NUM>) preferably has a density in the range of <NUM> to <NUM>/m<NUM>, more preferably <NUM> to <NUM>/m<NUM> and even more preferably <NUM> to <NUM>/m<NUM>.

Preferably, the density of fraction (A-<NUM>) is higher than the density of fraction (A-<NUM>).

The polyethylene component (B) preferably has a MFR<NUM> in the range of <NUM> to <NUM>/<NUM>, more preferably of <NUM> to <NUM>/<NUM>, and even more preferably of <NUM> to <NUM>/<NUM>. The density of the polyethylene component (B) preferably is in the range of <NUM> to <NUM>/m<NUM>, more preferably <NUM> to <NUM>/m<NUM> and even more preferably <NUM> to <NUM>/m<NUM>.

As stated above polyethylene component (B) preferably is an ethylene homopolymer.

The multimodal mHDPE may be produced by polymerization using conditions which create a multimodal (e.g. bimodal) polymer product using a metallocene catalyst system.

Thus, the multimodal mHDPE can be produced in a <NUM>-stage process, preferably comprising a slurry reactor (loop reactor), whereby the slurry (loop) reactor is connected in series to a gas phase reactor (GPR), whereby either polyethylene component (A) or polyethylene component (B) is produced in the loop reactor and the other ethylene polymer component is then produced in GPR in the presence of the first produced ethylene polymer component to produce the multimodal mHDPE, preferably the polyethylene component (A) is produced in the loop reactor and the polyethylene component (B) is produced in GPR in the presence of the polyethylene component (A) to produce the multimodal mHDPE.

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 temperature in the first polymerization stage is preferably from <NUM> to <NUM>, preferably from <NUM> to <NUM>. 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.

In the second polymerization stage, ethylene is polymerized in the presence of the catalyst and the ethylene polymer produced in the first polymerization stage. 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, to form the multimodal mHDPE of the present invention.

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 nonreactive gas such as nitrogen or low boiling point hydrocarbons such as propane together with monomer (e.g. ethylene).

In case that the polyethylene component (A) of the multimodal mHDPE consists of ethylene polymer fractions (A-<NUM>) and (A-<NUM>), the multimodal mHDPE can be produced with a <NUM>-stage process, preferably comprising a first slurry reactor (loop reactor <NUM>), whereby the first slurry loop reactor is connected in series with another slurry reactor (loop reactor <NUM>), so that the first ethylene polymer fraction (A-<NUM>) produced in the loop reactor <NUM> is fed to the loop reactor <NUM>, wherein the second ethylene polymer fraction (A-<NUM>) is produced in the presence of the first fraction (A-<NUM>). It is possible that fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor or vice versa, i.e. fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor. Preferably, fraction (A-<NUM>) is produced first.

The loop reactor <NUM> is thereby connected in series to a gas phase reactor (GPR), so that the polyethylene component (A) leaving the second slurry reactor is fed to the GPR to produce a trimodal polyethylene copolymer. In this case, the reaction conditions in the two slurry reactors are chosen in a way that in the two slurry reactors different products in view of MFR and/or density are produced.

Such a process is described inter alia in <CIT>, <CIT>, <CIT>, <CIT> and <CIT>. Full details of how to prepare suitable multimodal polymers can be found in these references.

A suitable process is the Borstar PE process or the Borstar PE <NUM> process.

The multimodal mHDPE comprising fractions (A-<NUM>) and (A-<NUM>) is therefore preferably produced in a loop loop gas cascade.

Such polymerization steps (either loop gas or loop loop gas) 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 preferably conducted in slurry.

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 or polymer produced in the prepolymerization lies within <NUM> to <NUM> wt% in respect to the final metallocene catalysed multimodal mHDPE. This can counted as part of the first polyethylene component (A).

The multimodal mHDPE is one made using a metallocene catalyst. A metallocene catalyst comprises a metallocene complex and a cocatalyst. The metallocene compound or complex is referred herein also as organometallic compound (C).

The organometallic compound (C) comprises a transition metal (M) of Group <NUM> to <NUM> of the Periodic Table (IUPAC <NUM>) or of an actinide or lanthanide.

The term "an organometallic compound (C)" in accordance with the present invention includes any metallocene or non-metallocene compound of a transition metal, which bears at least one organic (coordination) ligand and exhibits the catalytic activity alone or together with a cocatalyst. The transition metal compounds are well known in the art and the present invention covers compounds of metals from Group <NUM> to <NUM>, e.g. Group <NUM> to <NUM>, or <NUM> to <NUM>, such as Group <NUM> to <NUM> of the Periodic Table, (IUPAC <NUM>), as well as lanthanides or actinides.

In an embodiment, the organometallic compound (C) has the following formula (I):
<CHM>.

Preferably, the compound of formula (I) has the structure
<CHM>.

Highly preferred complexes of formula (I) are
<CHM>
<CHM>.

Most preferably the complex dimethylsilanediylbis[<NUM>-(<NUM>-trimethylsilylfuran-<NUM>-yl)-<NUM>,<NUM>-dimethylcyclopentadien-<NUM>-yl] zirconium dichloride is used.

More preferably the polyethylene components (A) and (B) of the multimodal metallocene catalysed high density polyethylene (mHDPE) are produced using, i.e. in the presence of, the same metallocene catalyst.

To form a catalyst, a cocatalyst, also known as an activator, is used, as is well known in the art. Cocatalysts comprising Al or B are well known and can be used here. The use of aluminoxanes (e.g. MAO) or boron based cocatalysts (such as borates) is preferred. Polyethylene copolymers made using single site catalysis, as opposed to Ziegler Natta catalysis, have characteristic features that allow them to be distinguished from Ziegler Natta materials. In particular, the comonomer distribution is more homogeneous. This can be shown using TREF or Crystaf techniques. Catalyst residues may also indicate the catalyst used. Ziegler Natta catalysts would not contain a Zr or Hf group (IV) metal for example.

The multimodal mHDPE may contain additives and/or fillers.

The optional additives and fillers and the used amounts thereof are conventional in the field of film applications. Examples of such additives are, among others, antioxidants, process stabilizers, UV-stabilizers, pigments, fillers, antistatic additives, antiblock agents, nucleating agents, acid scavengers as well as polymer processing agent (PPA).

The two skin layers SKL-<NUM> and SKL-<NUM> may comprise the same mHDPE or different mHDPEs as defined above.

In an embodiment of the invention it is possible that the mHDPE is blended with a low amount, e.g. <NUM> to <NUM> wt%, based on the total weight of the skin layer, of another polyethylene based polymer, like a mLLDPE or a znLLPDE as defined below.

In a preferred embodiment of the present invention both skin layers SKL-<NUM> and SKL-<NUM> comprise the same mHDPE.

In a further preferred embodiment of the present invention, both skin layers SKL-<NUM> and SKL-<NUM> consist of the same mHDPE only. (i.e. <NUM> wt% mHDPE related to the total weight of the skin layers).

The multimodal Ziegler-Natta catalysed linear low density polyethylene (znLLDPE) has a density in the range of <NUM> to <NUM>/m<NUM> (ISO <NUM>), preferably from <NUM> to <NUM>/m<NUM>, more preferably from <NUM> to <NUM>/m<NUM>, and even more preferably from <NUM> to <NUM>/m<NUM>.

The MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) of the znLLDPE is in the range of <NUM> to <NUM>/<NUM>, preferably from <NUM> to <NUM>/<NUM>, more preferably from <NUM> to <NUM>/<NUM>, and even more preferably from <NUM> to <NUM>/<NUM>.

The znLLDPE contains at least one or two comonomer(s). Suitable comonomers are C<NUM>-C<NUM> alpha-olefin comonomers.

Thus, the znLLDPE can be a copolymer of ethylene and one C<NUM>-C<NUM> alpha-olefin comonomer or a terpolymer of ethylene and two different C<NUM>-C<NUM> alpha-olefin comonomers.

Preferably, the comonomers are selected from the group of <NUM>-butene, <NUM>-hexene and <NUM>-octene. It is preferred if the comonomer employed is <NUM>-butene and/or <NUM>-hexene.

More preferred are terpolymers comprising <NUM>-butene and <NUM>-hexene comonomers.

The total comonomer content of the znLLDPE is preferably in the range of from <NUM> to <NUM> wt%, more preferably of from <NUM> to <NUM> wt% and even more preferably of from <NUM> to <NUM> wt%. <NUM>-butene is preferably present in the znLLDPE in an amount of from <NUM> to <NUM> wt%, more preferably of from <NUM> to <NUM> wt%, and even more preferably of from <NUM> to <NUM> wt% and <NUM>-hexene is present in the znLLDPE in an amount of from <NUM> to <NUM> wt%, more preferably of from <NUM> to <NUM> wt% and even more preferably of from <NUM> to <NUM> wt%.

In one embodiment of the present invention, the znLLDPE comprises.

The LMW homopolymer fraction (A) has a lower molecular weight than the HMW terpolymer fraction (B).

In a further embodiment of the present invention, the lower molecular weight (LMW) homopolymer of ethylene (A) consists of one or two fractions, i.e. of one or two homopolymers of ethylene.

In case that the lower molecular weight (LMW) homopolymer of ethylene (A) consists of two homopolymers of ethylene, these two fractions are named (A-<NUM>) and (A-<NUM>).

The lower molecular weight homopolymer (A) of the znLLDPE has a melt index MFR<NUM> according to ISO <NUM> (<NUM>) in the range of from <NUM> to <NUM>/<NUM>, preferably of from <NUM> to <NUM>/<NUM> and a density according to ISO <NUM> in the range of from <NUM> to <NUM>/m<NUM>, preferably <NUM> to <NUM>/m<NUM>.

The amount of the lower molecular weight fraction (A) of the znLLDPE is in the range of <NUM> to <NUM> wt%, preferably <NUM> to <NUM> wt% and more preferably <NUM> to <NUM> wt%.

The expression "homopolymer of ethylene" used herein refers to a polyethylene that consists substantially, i.e. to at least <NUM> wt% and more preferably at least <NUM> wt% by weight, like at least <NUM> wt% of ethylene.

In case that the lower molecular weight (LMW) homopolymer of ethylene (A) consists of two homopolymers of ethylene, i.e. fractions (A-<NUM>) and (A-<NUM>), these two fractions preferably have a different MFR<NUM> according to ISO <NUM> (<NUM>).

The homopolymer fraction (A-<NUM>) preferably has a MFR<NUM> according to ISO <NUM> (<NUM>) in the range of <NUM> to <NUM>/<NUM>, more preferably in the range of <NUM> to <NUM>/<NUM>, whereas the homopolymer fraction (A-<NUM>) preferably has a MFR<NUM> according to ISO <NUM> (<NUM>) in the range of <NUM> to <NUM>/<NUM>, more preferably in the range of <NUM> to <NUM>/<NUM>.

The MFR<NUM> of fraction (A-<NUM>) is preferably lower than the MFR<NUM> of the total lower molecular weight (LMW) homopolymer of ethylene (A).

According to a preferred embodiment the ratio of MFR<NUM>(A)/MFR<NUM>(A-<NUM>) may be for example between greater than <NUM> and up to <NUM>, preferably between <NUM> and <NUM>, such as <NUM> to <NUM>. Ideally, the MFR difference between the first and second homopolymer fraction (A-<NUM>) and (A-<NUM>) is as high as possible.

Ideally, the MFR difference between the first homopolymer fraction (A-<NUM>) and the MFR<NUM> of the total lower molecular weight (LMW) homopolymer of ethylene (A) is as high as possible e.g. MFR<NUM> of first homopolymer fraction (A-<NUM>) may be at least <NUM>/<NUM>, such as at least <NUM>/<NUM>, like <NUM> to <NUM>/<NUM> lower than the MFR<NUM> of the total lower molecular weight (LMW) homopolymer of ethylene (A).

The density of the two homopolymer fractions (A-<NUM>) and (A-<NUM>) may be the same or may be different and is in the range of <NUM> to <NUM>/m<NUM>, preferably <NUM> to <NUM>/m<NUM> or <NUM> to <NUM>/m<NUM>.

In an embodiment of the present invention the density of homopolymer fractions (A-<NUM>) and (A-<NUM>) are the same or differ +/- <NUM>/m<NUM>, preferably +/- <NUM>/m<NUM>.

The total lower molecular weight (LMW) homopolymer of ethylene (A) may comprise <NUM> to <NUM> wt% of the first ethylene homopolymer fraction (A-<NUM>) and <NUM> to <NUM> wt% of the second ethylene homopolymer fraction (A-<NUM>). In some embodiments, there is an excess of the second ethylene homopolymer fraction (A-<NUM>), e.g. <NUM> to <NUM> wt% of the second ethylene homopolymer fraction (A-<NUM>).

In another embodiment the total lower molecular weight (LMW) homopolymer of ethylene (A) contains the same amount of first and second ethylene homopolymer fractions (A-<NUM>) and (A-<NUM>).

The higher molecular weight fraction (B) has a lower MFR<NUM> and a lower density than the lower molecular weight fraction (A).

Preferably, the znLLDPE is produced in a multi-stage, e.g. two-stage or three-stage polymerization using the same Ziegler-Natta catalyst in all stages. Preferably, the znLLDPE is made using a slurry polymerization in at least one loop reactor followed by a gas phase polymerization in a gas phase reactor.

A loop reactor - gas phase reactor system or loop - loop - gas phase reactor system is well known as Borealis technology, i.e. a BORSTAR® reactor system.

In one embodiment, the znLLDPE is thus preferably formed in a two-stage process comprising a first slurry loop polymerization followed by gas phase polymerization in the presence of a Ziegler-Natta catalyst.

Preferably, the lower molecular weight fraction (A) is produced in a continuously operating loop reactor where ethylene is polymerized in the presence of a Ziegler-Natta catalyst and the higher molecular weight fraction (B) is then formed in a gas phase reactor using the same Ziegler-Natta catalyst.

Such znLLDPEs are known in the state of the art and are described e.g. in <CIT> or <CIT> or are commercially available, such as BorShape™ FX1001 and BorShape™ FX1002 (both from Borealis AG).

In another embodiment the znLLDPE is preferably formed in a three-stage process preferably comprising a first slurry reactor (loop reactor <NUM>), whereby the first slurry loop reactor is connected in series with another slurry reactor (loop reactor <NUM>), so that the first homopolymer fraction (A-<NUM>) produced in the loop reactor <NUM> is fed to the loop reactor <NUM>, wherein the second homopolymer fraction (A-<NUM>) is produced in the presence of the first fraction (A-<NUM>). The loop reactor <NUM> is thereby connected in series to a gas phase reactor (GPR), so that the total lower molecular weight fraction (A) leaving the second slurry reactor is fed to the GPR to produce the znLLDPE. In this case, the reaction conditions in the two slurry reactors are chosen in a way that in the two slurry reactors different products in view of MFR and/or density are produced.

Such a process is described inter alia in <CIT>.

A suitable process is the Borstar PE <NUM> process.

The polymerization is conducted in the presence of a Ziegler Natta catalyst. Ziegler Natta catalysts are useful as they can produce polymers within a wide range of molecular weight and other desired properties with a high productivity. Ziegler Natta catalysts used in the present invention are preferably supported on an external support.

Suitable Ziegler Natta catalysts preferably contain a magnesium compound, an aluminium compound and a titanium compound supported on a particulate support.

The particulate support typically used in Ziegler-Natta catalysts comprises an inorganic oxide support, such as silica, alumina, titania, silica-alumina and silica-titania or a MgCl2 based support. The catalyst used in the present invention is supported on an inorganic oxide support. Most preferably the Ziegler-Natta catalyst used in the present invention is supported on silica.

The average particle size of the silica support can be typically from <NUM> to <NUM>. However, it has turned out that special advantages can be obtained if the support has an average particle size from <NUM> to <NUM>, preferably from <NUM> to <NUM>. Alternatively, the support may have an average particle size of from <NUM> a <NUM>, preferably from <NUM> to <NUM>. Examples of suitable support materials are, for instance, ES747JR produced and marketed by Ineos Silicas (former Crossfield), and SP9-<NUM>, produced and marketed by Grace.

The magnesium compound 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 chlorine containing aluminium alkyl. Especially preferred compounds are aluminium alkyl dichlorides, aluminium dialkyl chlorides and aluminium alkyl sesquichlorides.

The transition metal is preferably titanium. The titanium compound is a halogen containing titanium compound, preferably chlorine containing titanium compound. 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>.

The Ziegler Natta catalyst is used together with an activator, which is also called as cocatalyst. Suitable activators are metal alkyl compounds, typically Group <NUM> metal alkyl compounds, and especially aluminium alkyl compounds. They include trialkylaluminium compounds, such as trimethylaluminium, triethylaluminium, tri-isobutylaluminium, trihexylaluminium and tri-n-octylaluminium. Aluminium alkyl compounds may also include alkyl aluminium halides, such as ethylaluminium dichloride, diethylaluminium chloride, ethylaluminium sesquichloride, dimethylaluminium chloride and the like and alkylaluminium oxy-compounds, such as methylaluminiumoxane, hexaisobutylaluminiumoxane and tetraisobutylaluminiumoxane and also other aluminium alkyl compounds, such as isoprenylaluminium. Especially preferred cocatalysts are trialkylaluminiums, of which triethylaluminium, trimethylaluminium and tri-isobutylaluminium are particularly preferred.

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 for example from <NUM> to <NUM>, preferably from <NUM> to <NUM> and in particular from about <NUM> to about <NUM> mol/mol.

Additionally the znLLDPE, preferably the znLLDPE terpolymer may also contain one or more additives selected from antioxidants, process stabilizers, slip agents, pigments, UV-stabilizers and other additives known in the art.

The multimodal metallocene catalysed linear low density polyethylene (mLLDPE) has a density in the range of <NUM> to <NUM>/m<NUM> (ISO <NUM>), preferably of <NUM> to <NUM>/m<NUM> and more preferably of <NUM> to <NUM>/m<NUM>.

The MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) of the mLLDPE is in the range of <NUM> to <NUM>/<NUM>, preferably of <NUM> to <NUM>/<NUM> and more preferably of <NUM> to <NUM>/<NUM>.

The mLLDPE has a ratio of the MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) to MFR<NUM> (<NUM>, <NUM>, ISO <NUM>), MFR<NUM>/MFR<NUM>, in the range of from <NUM> to <NUM>, preferably <NUM> to <NUM> and more preferably <NUM> to <NUM>.

The multimodal metallocene catalysed linear low density polyethylene (mLLDPE) comprises, preferably consists of.

The amount of (A) and (B) preferably add up to <NUM> wt%.

In a preferred embodiment of the present invention, the ethylene-<NUM>-butene polymer component (A) consists of an ethylene polymer fraction (A-<NUM>) and (A-<NUM>).

It is possible that fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor or vice versa, i.e. fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor. Preferably fraction (A-<NUM>) is produced first.

In case that the ethylene-<NUM>-butene polymer component (A) consists of ethylene polymer fractions (A-<NUM>) and (A-<NUM>), the MFR<NUM> of the ethylene polymer fractions (A-<NUM>) and (A-<NUM>) may be the same or may be different from each other.

Thus, the ethylene polymer fractions (A-<NUM>) and (A-<NUM>) have a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>, preferably of <NUM> to <NUM>/<NUM>, more preferably of <NUM> to <NUM>/<NUM> and even more preferably of <NUM> to <NUM>/<NUM>, like <NUM> to <NUM>/<NUM>.

The MFR<NUM> of the ethylene polymer components (A) and (B) are different from each other.

The ethylene polymer component (A) has a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>, preferably of <NUM> to <NUM>/<NUM>, more preferably of <NUM> to <NUM>/<NUM>, even more preferably of <NUM> to <NUM>/<NUM> and still more preferably of <NUM> to <NUM>/<NUM>.

The ethylene polymer component (B) has a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>, preferably of <NUM> to <NUM>/<NUM>, more preferably of <NUM> to <NUM>/<NUM> and even more preferably of <NUM> to <NUM>/<NUM>.

In an embodiment of the invention it is preferred the ratio of the MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) of the ethylene-<NUM>-butene polymer component (A) to the MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) of the final multimodal metallocene catalysed linear low density polyethylene (mLLDPE) is at least <NUM> to <NUM>, preferably <NUM> to <NUM>, more preferably of <NUM> to <NUM> and even more preferably of <NUM> to <NUM>.

Naturally, in addition to multimodality with respect to, i.e. difference between, the MFR<NUM> of ethylene polymer components (A) and (B), the multimodal PE of the invention can also be multimodal e.g. with respect to one or both of the two further properties:
multimodality with respect to, i.e. difference between,.

Preferably, the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) is further multimodal with respect to the comonomer content of the ethylene polymer components (A) and (B).

The comonomer type for the polymer fractions (A-<NUM>) and (A-<NUM>) is the same, thus both fractions therefore have <NUM>-butene as comonomer.

Even more preferably the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) of the invention is further multimodal with respect to difference in density between the ethylene polymer component (A) and ethylene polymer component (B). Preferably, the density of ethylene polymer component (A) is different, preferably higher, than the density of the ethylene polymer component (B).

The density of the ethylene polymer component (A) is in the range of <NUM> to <NUM>/m<NUM>, preferably of <NUM> to <NUM>/m<NUM>, more preferably <NUM> to <NUM>/m<NUM> and/or the density of the ethylene polymer component (B) is of in the range of <NUM> to <NUM>/m<NUM>, preferably of <NUM> to <NUM>/m<NUM> and more preferably of <NUM> to <NUM>/m<NUM>.

The polymer fraction (A-<NUM>) has a density in the range of from <NUM> to <NUM>/m<NUM>, preferably of <NUM> to <NUM>/m<NUM>, more preferably of <NUM> to <NUM>/m<NUM>, like <NUM> to <NUM>/m<NUM>.

The density of the polymer fraction (A-<NUM>) is in the range of from <NUM> to <NUM>/m<NUM>, preferably of <NUM> to <NUM>/m<NUM>, like <NUM> to <NUM>/m<NUM>.

More preferably the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) is multimodal at least with respect to, i.e. has a difference between, the MFR<NUM>, the comonomer content as well as with respect to, i.e. has a difference between the density of the ethylene polymer components, (A) and (B), as defined above, below or in the claims including any of the preferable ranges or embodiments of the polymer composition.

It is within the scope of the invention, that the first and the second ethylene polymer fraction (A-<NUM> and A-<NUM>) of the ethylene polymer component (A) are present in a weight ratio of <NUM>:<NUM> up to <NUM>:<NUM>, such as <NUM>:<NUM> to <NUM>:<NUM>, or <NUM>:<NUM> to <NUM>:<NUM>, or <NUM>:<NUM>.

The ethylene polymer component (A) is present in an amount of <NUM> to <NUM> wt% based on the multimodal metallocene catalysed linear low density polyethylene (mLLDPE), preferably in an amount of <NUM> to <NUM> wt% and even more preferably in an amount of <NUM> to <NUM> wt%. Thus, the ethylene polymer component (B) is present in an amount of <NUM> to <NUM> wt% based on the multimodal metallocene catalysed linear low density polyethylene (mLLDPE), preferably in an amount of <NUM> to <NUM> wt% and more preferably in an amount of <NUM> to <NUM> wt%.

The multimodal metallocene catalysed linear low density polyethylene (mLLDPE), can be produced in a <NUM>-stage process, preferably comprising a slurry reactor (loop reactor), whereby the slurry (loop) reactor is connected in series to a gas phase reactor (GPR), whereby either ethylene component (A) or ethylene component (B) is produced in the loop reactor and the other ethylene polymer component is then produced in GPR in the presence of the first produced ethylene polymer component to produce the multimodal metallocene catalysed linear low density polyethylene (mLLDPE), preferably the ethylene polymer component (A) is produced in the loop reactor and the ethylene polymer component (B) is produced in GPR in the presence of the ethylene polymer component (A) to produce the multimodal metallocene catalysed linear low density polyethylene (mLLDPE).

In case that the ethylene component (A) of the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) consists of ethylene polymer fractions (A-<NUM>) and (A-<NUM>), the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) can be produced with a <NUM>-stage process, preferably comprising a first slurry reactor (loop reactor <NUM>), whereby the first slurry loop reactor is connected in series with another slurry reactor (loop reactor <NUM>), so that the first ethylene polymer fraction (A-<NUM>) produced in the loop reactor <NUM> is fed to the loop reactor <NUM>, wherein the second ethylene polymer fraction (A-<NUM>) is produced in the presence of the first fraction (A-<NUM>). It is possible that fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor or vice versa, i.e. fraction (A-<NUM>) is produced first and then fraction (A-<NUM>) is produced in the presence of fraction (A-<NUM>) in a subsequent reactor. Preferably fraction (A-<NUM>) is produced first.

The loop reactor <NUM> is thereby connected in series to a gas phase reactor (GPR), so that the ethylene polymer component (A) leaving the second slurry reactor is fed to the GPR to produce a trimodal polyethylene copolymer. In this case, the reaction conditions in the two slurry reactors are chosen in a way that in the two slurry reactors different products in view of MFR and/or density are produced.

Such a process is described inter alia in <CIT>, <CIT>, <CIT>, <CIT> and <CIT>. Full details of how to prepare suitable multimodal metallocene catalysed linear low density polyethylene (mLLDPE) can be found in these references.

The multimodal metallocene catalysed linear low density polyethylene (mLLDPE) according to the present invention is therefore preferably produced in a loop loop gas cascade. Such polymerization steps 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 preferably conducted in slurry.

It is understood within the scope of the invention, that the amount or polymer produced in the prepolymerization lies within <NUM> to <NUM> wt% in respect to the final metallocene catalysed multimodal metallocene catalysed linear low density polyethylene (mLLDPE). This can counted as part of the ethylene polymer component (A).

The multimodal metallocene catalysed linear low density polyethylene (mLLDPE) used in the core layer (CL) of the present of the invention is one made using a metallocene catalyst. A metallocene catalyst comprises a metallocene complex and a cocatalyst. The metallocene compound or complex is referred herein also as organometallic compound (C).

As metallocene catalyst, the one described for the mHDPE can be used.

The multimodal metallocene catalysed linear low density polyethylene (mLLDPE) may contain further polymer components and optionally additives and/or fillers. In case the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) contains further polymer components, then the amount of the further polymer component(s) typically varies between <NUM> to <NUM> wt% based on the combined amount of the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) and the other polymer component(s).

It is understood herein that any of the additives and/or fillers can optionally be added in so-called master batch, which comprises the respective additive(s) together with a carrier polymer. In such case the carrier polymer is not calculated to the polymer components of the multimodal metallocene catalysed linear low density polyethylene (mLLDPE), but to the amount of the respective additive(s), based on the total amount of the multimodal metallocene catalysed linear low density polyethylene (mLLDPE) (<NUM> wt%).

The multilayered film according to the present invention has an attractive balance of mechanical, e.g. tensile modulus (TM) or tensile strength (TS), and optical properties, e.g. haze.

Films according to the present invention may have a haze measured according to ASTM D1003 on a <NUM> test blown film of below <NUM>%, preferably in the range of <NUM> to <NUM>% and more preferably in the range of <NUM> to <NUM>%.

Films according to the present invention have good stiffness (tensile modulus measured on a <NUM> monolayer test blown film according to ISO <NUM>-<NUM>), i.e. ><NUM> MPa (in machine direction).

Thus, the multilayered films according to the present invention have a tensile modulus (measured on a <NUM> monolayer test blown film according to ISO <NUM>-<NUM>) in machine (MD) direction in the range of ><NUM> MPa to <NUM> MPa, preferably of <NUM> MPa to <NUM> MPa and more preferably of <NUM> MPa to <NUM> MPa.

As mentioned above a multilayered film according to the present invention has an attractive balance of mechanical, e.g. tensile modulus or strength, and optical properties, e.g. haze and thus provides an attractive alternative to substitute polyester films.

This can be seen in an improved optomechanical ability (I) (OMA I) according to formula: <MAT> determined on <NUM> test blown film of at least <NUM> [MPa*g/%] up to <NUM> [MPa*g/%], preferably in the range of from <NUM> [MPa*g/%] up to <NUM> [MPa*g/%], more preferably in the range of from <NUM> [MPa*g/%] up to <NUM> [MPa*g/%], wherein the Tensile Modulus and the Elongation in machine direction are measured according to ISO <NUM>-<NUM> at <NUM> on <NUM> test blown films and haze is measured according to ASTM D1003 on a <NUM> test blown film.

In addition or alternatively this improved balance can be seen by an improved optomechanical ability (II) (OMA II) according to formula: <MAT> determined on <NUM> test blown film of at least <NUM> [MPa*g/%] up to <NUM> [MPa*g/%], preferably in the range of from <NUM> [MPa*g/%] up to <NUM> [MPa*g/%], more preferably in the range of from <NUM> [MPa*g/%] up to <NUM> [MPa*g/%], wherein the Tensile Strength and Elongation in machine direction are measured according to ISO <NUM>-<NUM> at <NUM> and haze is measured according to ASTM D1003.

The multilayered film of the invention is an uniaxially oriented film. Preferably, the film is oriented in the machine direction.

The uniaxially oriented multilayered film of the present invention can have a thickness in the range of <NUM> - <NUM>, such as <NUM> - <NUM>, like <NUM> - <NUM> or <NUM> - <NUM> after orientation.

The multilayer film of the invention comprises least two layers (A), being skin layers (SKL-<NUM> and SKL-<NUM>), sandwiching a layer (B), being a core layer (CL). Thus, the films of the invention comprise at least three layers, however it is possible for the films to comprise more than three layers, such as <NUM> or <NUM> layers. Where more than three layers are present, the additional layers are typically tie layers.

The skin layers and the core layer may all be of equal thickness or alternatively the core layer may be thicker than each of the skin layers.

A convenient film comprises skin layers which each form <NUM> to <NUM>%, preferably <NUM> to <NUM>% of the total thickness of the <NUM>-layered film, the core layer forming the remaining thickness, e.g. <NUM> to <NUM>%, preferably <NUM> to <NUM>% of the total thickness of the <NUM>-layered film. The multilayer films of the present invention can be symmetric (with the skin layers SKL-<NUM> and SKL-<NUM> having the same thickness, or asymmetric (with the skin layers SKL-<NUM> and SKL-<NUM> differing in view of their thickness).

The three-layer structure in accordance with the present invention may be prepared by any conventional film extrusion procedure known in the art including cast film and blown film extrusion. Preferably, the three-layer film is formed by blown film extrusion, more preferably by coextrusion processes, which in principle are known and available to the skilled person. Typical processes for preparing a three-layer structure in accordance with the present invention are extrusion processes through an angular die, followed by blowing into a tubular film by forming a bubble which is collapsed between the rollers after solidification. This film can then be slid, cut or converted, such as by using a gazette head, as desired. Conventional film production techniques may be used in this regard. Typically the core layer mixture and the polymer or mixture for the sandwiching layers are coextruded at a temperature in the range of from <NUM> to <NUM> and cooled by blowing gas (generally air) at a temperature of <NUM> to <NUM>, to provide a frost line height of <NUM> or <NUM> to <NUM> times the diameter of the dye. The blow up ratio should generally be in the range of from <NUM> to <NUM>, such as from <NUM> to <NUM>, preferably <NUM> to <NUM>.

If desired any of the three layers of the three-layered structure of the invention may comprise usual additives, such as stabilizers, processing aids, colorants, anti-block agents, slip agents etc. in amounts not detrimental to the desired function of the three-layered structure. Typically the overall amount of additives in a layer is <NUM> wt% or less, based on the weight of the layer, preferably <NUM> wt% or less, more preferably <NUM> wt% or less. In embodiments the layers can be completely free of any additives.

The multilayer films of the invention are preferably symmetric, i.e. wherein the two skin layers SKL-<NUM> and SKL-<NUM> are the same (i.e. in view of thickness and of the composition).

The preparation process of the uniaxially oriented multilayer film of the invention comprises at least the steps of forming a layered film structure and stretching the obtained multilayer film in the machine direction, typically in a draw ratio of at least <NUM>:<NUM>. As to the first step of the preparation process, the layered structure of the film of the invention may be prepared by any conventional film formation process including extrusion procedures, such as cast film or blown film extrusion. The multilayer films are ideally blown films and are thus preferably prepared by blown film extrusion.

Particularly preferably the multilayer film of the invention is formed by blown film extrusion, more preferably by blown film coextrusion processes. Typically, the compositions providing the core and skin layers will be blown (co)extruded at a temperature in the range <NUM> to <NUM>, and cooled by blowing gas (generally air) at a temperature of <NUM> to <NUM> to provide a frost line height of <NUM> or <NUM> to <NUM> times the diameter of the die. The blow up ratio should generally be in the range <NUM> to <NUM>, preferably <NUM> to <NUM>.

The obtained, preferably coextruded, multilayer film is subjected to a subsequent stretching step, wherein the multilayer film is stretched in the machine direction. Stretching may be carried out by any conventional technique using any conventional stretching devices, which are well known to those skilled in the art. the film may be coextruded to first form a bubble which is then collapsed and cooled, if necessary, and the obtained tubular film is stretched in line. Stretching is preferably carried out at a temperature in the range <NUM>-<NUM>, e.g. about <NUM>. Any conventional stretching rate may be used, e.g. <NUM> to <NUM> %/second.

Preferably, the film is stretched only in the MD. The effect of stretching in only one direction is to uniaxially orient the film. The film is stretched at least <NUM> times, preferably <NUM> to <NUM> times, its original length in the machine direction. This is stated herein as a draw ratio of at least <NUM>:<NUM>, i.e. "<NUM>" represents the original length of the film and "<NUM>" denotes that it has been stretched to <NUM> times that original length. Preferred films of the invention are stretched in a draw ratio of at least <NUM>:<NUM>, more preferably between <NUM>:<NUM> and <NUM>:<NUM>, e.g. between <NUM>:<NUM> and <NUM>:<NUM>. An effect of stretching (or drawing) is that the thickness of the film is similarly reduced. Thus a draw ratio of at least <NUM>:<NUM> preferably also means that the thickness of the film is at least three times less than the original thickness. Blow extrusion and stretching techniques are well known in the art, e.g. in <CIT>.

The film preparation process steps of the invention are known and may be carried out in one film line in a manner known in the art. Such film lines are commercially available. The final uniaxially oriented in MD films can be further processed, e.g. laminated on a substrate. Preferably, however, the films are used in non- laminated film applications.

The films of the invention have a wide variety of applications but are of particular interest in packaging.

Thus, viewed from another aspect, the invention provides an article, preferably a packaging article, comprising a uniaxially oriented multilayer film as hereinbefore defined.

The additional optional layers are naturally selected so that they have no adverse effect on the inventive effect achieved with the three-layer structure according to the invention. Thus it is also possible to use the three-layer structure of the present invention for producing a <NUM>- or even <NUM>-layered film, depending upon the desired end application.

However, the three-layer structure in accordance with the present invention preferably is employed as such, without lamination to any further film material.

The uniaxially oriented films of 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 uniaxially oriented films of the present invention are preferably used for applications related to food packaging.

The present invention will now be described in further detail by the examples provided below.

Unless otherwise stated in the description or in the experimental part, the following methods were used for the property determinations of the polymers (including its fractions and components) and/or any sample preparations thereof as specified in the text or experimental part.

The melt flow rate (MFR) was determined according to ISO <NUM> and is indicated in g/<NUM>. The MFR is determined at <NUM> for polyethylene. MFR may be determined at different loadings such as <NUM> (MFR<NUM>), <NUM> (MFR<NUM>) or <NUM> (MFR<NUM>).

The density was measured according to ISO <NUM> and ISO1872-<NUM> for sample preparation.

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>.

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

The amount isolated <NUM>-hexene incorporated in EEHEE sequences was quantified using the integral of the B4 sites at <NUM> ppm accounting for the number of reporting sites per comonomer: <MAT>.

The amount consecutively incorporated <NUM>-hexene in EEHHEE sequences was quantified using the integral of the ααB4B4 site at <NUM> ppm accounting for the number of reporting sites per comonomer: <MAT>.

The amount non consecutively incorporated <NUM>-hexene in EEHEHEE sequences was quantified using the integral of the ββB4B4 site at <NUM> ppm accounting for the number of reporting sites per comonomer: <MAT>.

The total mole fraction of <NUM>-hexene in the polymer was then calculated as: <MAT>.

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

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

Data was measured with a TA Instrument Q2000 differential scanning calorimetry (DSC) on <NUM> to <NUM> samples. DSC was 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) and crystallization enthalpy (Hc) were determined from the cooling step, while melting temperature (Tm) and melting enthalpy (Hm) are determined from the second heating step.

Tensile modulus and elongation were measured in machine and/or transverse direction according to ISO <NUM>-<NUM> on film samples prepared as described under the Film Sample preparation with film thickness of <NUM> and at a cross head speed of <NUM>/min for the modulus. For tensile strength and elongation a cross head speed of <NUM>/min was used.

Haze as a measure for the optical appearance of the films was determined according to ASTM D1003 on film samples with a thickness of <NUM>.

Optomechanical ability (I) (OMA I) was determined on <NUM> test blown film and was calculated according to formula: <MAT> wherein the Tensile Modulus and Elongation in machine direction were measured according to ISO <NUM>-<NUM> at <NUM> and haze was measured according to ASTM D1003.

Optomechanical ability (II) (OMA II) was determined on <NUM> test blown film and was calculated according to formula: <MAT> wherein the Tensile Strength and Elongation in machine direction were measured according to ISO <NUM>-<NUM> at <NUM> and haze was measured according to ASTM D1003.

<NUM> of silica (PQ Corporation ES757, calcined <NUM>) was added from a feeding drum and inertized in the reactor until O<NUM> level below <NUM> ppm was reached.

<NUM> wt% MAO in toluene (<NUM>) was added into another reactor from a balance followed by toluene (<NUM>) at <NUM> (oil circulation temp) and stirring <NUM> rpm. Stirring speed was increased <NUM> rpm -> <NUM> rpm after toluene addition, stirring time <NUM>. Metallocene Rac-dimethylsilanediylbis{<NUM>-(<NUM>-(trimethylsilyl)furan-<NUM>-yl)-<NUM>,<NUM>-dimethylcyclopentadien-<NUM>-yl}zirconium dichloride <NUM> was added from a metal cylinder followed by flushing with <NUM> toluene (total toluene amount <NUM>). Reactor stirring speed was changed to <NUM> rpm for MC feeding and returned back to <NUM> rpm for <NUM> reaction time. After reaction time MAO/tol/MC solution was transferred into a feeding vessel.

Reactor temperature was set to <NUM> (oil circulation temp) and stirring was turned to <NUM> rpm during MAO/tol/MC addition. MAO/tol/MC solution (<NUM>) was added within <NUM> followed by <NUM> stirring time (oil circulation temp was set to <NUM>). After stirring "dry mixture" was stabilised for <NUM> at <NUM> (oil circulation temp), stirring <NUM> rpm. Reactor was turned <NUM>° (back and forth) and stirring was turned on <NUM> rpm for few rounds once an hour.

After stabilisation the catalyst was dried at <NUM> (oil circulation temp) for <NUM> under nitrogen flow <NUM>/h, followed by <NUM> under vacuum (same nitrogen flow with stirring <NUM> rpm). Dried catalyst was sampled and HC content was measured in the glove box with Sartorius Moisture Analyser, (Model MA45) using thermogravimetric method. Target HC level was < <NUM>% (actual <NUM> %).

IE1: Borstar pilot plant with a <NUM>-reactor set-up (loop1 - loop2 - GPR <NUM>) and prepolymerization. Multimodal mHDPE and mLLDPE were produced using the polymerization conditions as given in Table <NUM>.

The polymers were mixed with <NUM> wt% Irganox <NUM> (BASF), <NUM> wt% Irgafos <NUM> (BASF) & <NUM> wt% CEASIT FI (Baerlocher) calcium stearate, where wt% are relative to total weight of composition (the sum of polymer powder + additive = <NUM>%) compounded and extruded on a ZSK <NUM> twin screw extruder. The melt temperature was <NUM>; production rate was <NUM>/h.

A solid polymerization catalyst component produced as described in Example <NUM> of <CIT> was used together with triethylaluminium cocatalyst so that the molar ratio of Al/Ti was about <NUM>.

Borstar pilot plant with a <NUM>-reactor set-up (loop1 - loop2 - GPR <NUM>) and a prepolymerization loop reactor.

znLLDPE was produced by using the polymerization conditions as given in Table <NUM>.

The polymer powder was mixed under nitrogen atmosphere with <NUM> ppm of Irganox B561 and <NUM> ppm Ca-stearate. Then it was compounded and extruded under nitrogen atmosphere to pellets by using a JSW CIMP90 twin screw extruder.

For Comparative Example CE1 for all layers:
Lumicene Supertough 40ST05 (40ST05), commercially available from Total, a metallocene MDPE with density <NUM>/m<NUM>, MFR<NUM> <NUM>/<NUM>, Tm <NUM>.

For Comparative Example CE2 for SKL-<NUM> and SKL-<NUM>:
HDPE Borstar® FB5600 from Borouge, bimodal ethylene copolymer, density <NUM>/m<NUM>, Tm <NUM>, MFR<NUM> <NUM>/<NUM>, MFR<NUM> <NUM>/<NUM>, MFR<NUM> <NUM>/<NUM>. MFR<NUM>/MFR<NUM> <NUM>.

The <NUM> layer films before MDO were produced on an Alpine <NUM> layers BF line, all of them had a start film thickness of <NUM>, the melt temperature was fixed at <NUM>, BUR <NUM>:<NUM>, the details are as follows:.

The MDO was done on a lab scale Alpine MDO <NUM> pilot machine, with ratio of <NUM>:<NUM>, stretching roll temperature <NUM>. The final film therefore has total thickness of <NUM>. The properties of CEs and IE on MDO are shown in Table <NUM>.

Due to the nature of the mHDPE, the melting point of the mHDPE (Tm <NUM>) is much higher than for 40ST05 and similar to FB5600, thus, the thermal shielding is much better than for CE1 using only 40ST05.

As can be seen from above Table, the IE has higher stiffness (i.e. higher tensile modulus), TS, elongation in MD, but worse haze, compared to the pure medium density PE solution of CE1.

Compared to the CE2, IE1 has lower stiffness, but slightly increased elongation in MD and clearly improved optics.

Claim 1:
An uniaxially oriented multilayered polyethylene film comprising at least two layers (A), being skin layers (SKL-<NUM> and SKL-<NUM>), sandwiching a layer (B), being a core layer (CL), wherein
(A) the skin layers (SKL-<NUM> and SKL-<NUM>) can be the same or can be different and comprise at least <NUM> wt%, based on the skin layer, of a multimodal metallocene catalysed high density polyethylene (mHDPE),
wherein the multimodal mHDPE has a density (ISO <NUM>) in the range of <NUM> to <NUM>/m<NUM> and a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM> and wherein the multimodal mHDPE comprises at least
(i) <NUM> to <NUM> wt%, relative to the total weight of the multimodal mHDPE, of a polyethylene component (A) having a density (ISO <NUM>) in the range of <NUM> to <NUM>/m<NUM> and a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>; and
(ii) <NUM> to <NUM> wt%, relative to the total weight of the multimodal mHDPE, of a polyethylene component (B) being a polyethylene having a density (ISO <NUM>) in the range of <NUM> to <NUM>/m<NUM> and a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM>;
and wherein
(B) the core layer (CL) comprises:
a) <NUM> wt% to <NUM> wt%, based on the total weight of the core layer (CL), of a multimodal Ziegler-Natta catalysed linear low density polyethylene (znLLDPE) having a density in the range of <NUM> to <NUM>/m<NUM> (ISO <NUM>) and a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of from <NUM> to <NUM>/<NUM>; and
b) <NUM> wt% to <NUM> wt%, based on the total weight of the core layer (CL), of a multimodal metallocene catalysed linear low density polyethylene (mLLDPE) having a density in the range of <NUM> to <NUM>/m<NUM> (ISO <NUM>), a MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) in the range of <NUM> to <NUM>/<NUM> and a ratio of the MFR<NUM> (<NUM>, <NUM>, ISO <NUM>) to MFR<NUM> (<NUM>, <NUM>, ISO <NUM>), MFR<NUM>/MFR<NUM>, in the range of <NUM> to <NUM>.