CN111662402A - Polyolefin composition and preparation method and application thereof - Google Patents
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Abstract
The present invention relates to a polyolefin composition comprising: ethylene/C3‑C5α -olefin/C6‑C9α -olefin copolymer, wherein, derived from C3‑C5α -the content of structural units derived from olefins is from 0.2 mol% to 0.6 mol%, and/or derived from C6‑C9α -the content of structural units of the olefin is from 2.5 mol% to 3.0 mol%, by using an ethylene/C having specific structural units3‑C5α -olefin/C6‑C9α -olefin copolymer, and limiting the content of specific structural units in the copolymer to a specific range, endows the polyolefin composition with a wider processing temperature range and good tensile property.
Description
Technical Field
The invention relates to the field of polyolefin materials, in particular to a polyolefin composition and a preparation method and application thereof.
Background
Biaxially Oriented Polyethylene (BOPE) is a Polyethylene film produced by using a biaxial orientation technique of a polymer, that is, between the glass transition temperature and the melting point of Polyethylene, a non-Oriented sheet is sequentially stretched longitudinally and transversely, molecular chains have biaxial orientation in a plane, and finally, the sheet is cooled and shaped under the condition of tension. BOPE thickness is even, tensile strength is high, anti puncture ability reinforce, heat-seal strength is high, the environmental protection, has excellent separation performance and low temperature resistance, and it mainly is applied to the complex film now, can guarantee under the circumstances that the intensity of film can not reduce, plays the effect of attenuate. For example, the BOPE can be used in combination with a biaxially oriented nylon film (BOPA), a biaxially oriented polyester film (BOPET), and the like, for packaging various foods or daily necessities.
However, since 2009 biaxially oriented technology was first applied to polyethylene films, BOPE is not widely produced and applied domestically today. The main reasons are that the polyethylene has the characteristics of easy crystallization, high crystallization rate, high crystallinity and the like, so that a crystalline region of the polyethylene is easy to rapidly grow and rupture a membrane in the stretching process, the relaxation time of a polyethylene molecular chain is short, the thickness of the prepared film is uneven, and the processing and stretching temperature range is narrower than that of PP, PA and PET.
An innovative polyethylene product suitable for biaxial stretching by a flat film method, which is pioneered by the Japan three-well chemical company, is prepared by combining certain mLDPE (low density polyethylene) and LDPE with bimodal distribution of relative molecular mass as raw material resin of BOPE. The mLDPE is produced by using a specific metallocene catalyst and is expensive. The exxon meifu company prepares BOPE by a 5-layer coextrusion process of polyethylene and polypropylene using a blend of 80% VLDPE (ultra low density polyethylene) and 20% LDPE as a coextruded surface layer, which process has the disadvantage of greater operational difficulty.
Disclosure of Invention
In view of the problems of the prior art as described above, it is an object of the present invention to provide a polyolefin composition, a method for preparing the same and use thereof, by using an ethylene/C having a specific structural unit3-C5α -olefin/C6-C9α -olefin copolymer, and limiting the content of specific structural units in the copolymer to a specific range, endows the polyolefin composition with a wider processing temperature range and good tensile property.
In one aspect, the present invention provides a polyolefin composition comprising: ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer, wherein, derived from C3-C5α -the content of structural units derived from olefins is from 0.2 mol% to 0.6 mol%, and/or derived from C6-C9α -content of structural units of an olefin2.5mol％-3.0mol％。
The inventors of the present application have found in their research that when a polyolefin composition contains structural units derived from ethylene, derived from C, together3-C5α structural units of an olefin and derived from C6-C9α -structural units of olefin, and when the content of each structural unit is within the specific range of the application, the melting range of the polyolefin composition is widened due to the co-crystallization phenomenon, and the biaxial stretching temperature range of the polyolefin composition is enlarged, so that the prepared film has the outstanding advantages of good mechanical properties, such as high tensile yield strength, high tensile breaking strength, high elastic modulus and the like.
According to the invention, derived from C3-C5α -the content of structural units of the olefin is preferably from 0.3 mol% to 0.5 mol%, more preferably from 0.35 mol% to 0.45 mol%, and/or derived from C6-C9The content of α -olefin structural units is preferably from 2.6 mol% to 2.9 mol%, more preferably from 2.7 mol% to 2.8 mol%.
In some preferred embodiments of the present invention, said C3-C5α -olefin is selected from propylene and/or 1-butene, preferably 1-butene, C6-C9The α -olefin is selected from 1-hexene and/or 1-octene, preferably 1-hexene.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a density of 0.710g/cm3-1.125g/cm3。
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α melt index MI of olefin copolymer2.16Is 0.01g/10min-10g/10 min.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α the weight average molecular weight of the olefin copolymer is 100000 or more.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α the molecular weight distribution of the olefin copolymer is 1-10.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a molecular chain relaxation time of greater than 2.5 s.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a crystallization rate function value of less than 4.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α the spherulite size of the olefin copolymer is less than 10 μm.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymers have a shear viscosity greater than 100Pa.s at a shear rate of 1000/s.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a density of 0.910g/cm3-0.925g/cm3Preferably 0.915g/cm3-0.920g/cm3。
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α melt index MI of olefin copolymer2.16Is 0.5g/10min-3.0g/10min, preferably 0.5g/10min-2.0g/10 min.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a weight average molecular weight of 100000-500000, preferably 100000-120000.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α the molecular weight distribution of the olefin copolymer is 2 to 6, preferably 3 to 5.
In some preferred embodiments of the inventionIn the formula (II), the ethylene/C3-C5α -olefin/C6-C9α the molecular chain relaxation time of the olefin copolymer is more than 3 s.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a crystallization rate function value of less than 3.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α the spherulite size of the olefin copolymer is less than 8 μm.
In some preferred embodiments of the invention, the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymers have a shear viscosity greater than 150Pa.s at a shear rate of 1000/s.
In still another aspect, the present invention provides a method for preparing a polyolefin composition, comprising:
containing ethylene and C3-C5α -olefin, C6-C9α -contacting a reactant stream of olefin and condensing agent with an olefin polymerization catalyst to produce ethylene, C3-C5α -olefins and C6-C9α -olefin polymerization to said ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer.
In some preferred embodiments of the present invention, the molar ratio of the ethylene to the condensing agent in the reactant stream is (0.5-3.0):1, preferably (1.0-2.0):1, more preferably (1.2-1.7): 1.
In some preferred embodiments of the present invention, the ethylene and the C are in the reactant stream3-C5α -olefin molar ratio is (30-80):1, preferably (40-60): 1.
In some preferred embodiments of the present invention, the ethylene and the C are in the reactant stream6-C9α -olefin molar ratio is (5.0-12.0):1, preferably (8.0-10.0): 1.
The inventor of the present application finds in research that the temperature of the polymerization reaction can be effectively controlled by controlling the molar ratio of ethylene to the condensing agent, so that the polyolefin composition prepared has the advantages of good processability, wide temperature window for stretching processing, and excellent mechanical properties.
In some preferred embodiments of the present invention, the polymerization temperature of the polymerization reaction is 20 ℃ to 120 ℃ and the polymerization pressure is 0.1MPa to 10 MPa.
In some preferred embodiments of the invention, the condensing agent is selected from C5-C8At least one of the alkanes is preferably at least one selected from n-pentane, isopentane, cyclohexane, n-hexane, n-heptane and n-octane, more preferably isopentane and/or n-heptane.
According to the invention, the reactant stream also comprises hydrogen and nitrogen.
According to the invention, the molar ratio of hydrogen to ethylene in the reactant stream is (0.10-0.15): 1.
According to the invention, the molar ratio of nitrogen to ethylene in the reaction stream is (0.50-2.50): 1.
In a particular embodiment, the preparation process according to the invention can be carried out in a fluidized-bed reactor, the particular operating steps comprising: replacing air in the fluidized bed reactor by nitrogen, and fluidizing the seed bed under the condition of nitrogen; then adding a small amount of olefin polymerization catalyst into the fluidized bed reactor, and gradually reducing the introduction amount of nitrogen; then adding ethylene and C in gradually increasing input quantity3-C5α -olefin, C6-C9α -olefin and condensing agent to finally obtain ethylene and C3-C5α -olefin, C6-C9α -the amount of olefin as well as condensing agent and nitrogen are within the specified ranges herein, while adding the olefin polymerization catalyst to the predetermined amount.
In this process, the polymerization temperature is further regulated by recovering the condensing agent and recycling it to the fluidized bed reactor after heat exchange. Preferably, the condensing agent enters the reactor from the side wall or bottom of the fluidized bed.
In some preferred embodiments of the present invention, the olefin polymerization catalyst is selected from at least one of a ziegler-natta catalyst, a metallocene catalyst, and a late transition metal catalyst.
According to the present invention, olefin polymerization catalysts (e.g., Ziegler-Natta, metallocene, and late transition metal catalysts) prepared by methods and ratios known in the art can be applied to the present invention and achieve the desired technical effects.
The present invention is preferably a Ziegler-Natta catalyst or a composite catalyst of a Ziegler-Natta catalyst and a metallocene catalyst and/or a late transition metal catalyst.
The Ziegler-Natta catalyst system comprises: 1) a solid component containing a titanium compound and an electron-donor compound (internal donor) supported on a magnesium dihalide, preferably magnesium chloride; 2) an alkylaluminum compound (cocatalyst); optionally 3) an electron-donor compound (external donor); wherein the electron-donor compound (internal donor) is selected from ethers, ketones, lactones, compounds containing N, P and or S atoms, and compounds of monocarboxylic and dicarboxylic esters; the alkylaluminum compounds are trialkylaluminum compounds, such as Al-triethyl, Al-triisobutyl and Al-tri-n-butyl; the electron-donor compound (external donor) is selected from aromatic acid esters (e.g. alkyl benzoates, heterocyclic compounds), particularly preferably a silicon compound containing at least one Si-OR bond (wherein R is a hydrocarbon group), further preferably tert-hexyltrimethoxysilane (2, 3-dimethyl-2-trimethoxysilyl-butane).
In a further aspect the present invention provides the use of a polyolefin composition as described above or a polyolefin composition prepared according to the above preparation process as a biaxially oriented polyolefin feedstock.
According to the invention, the term "ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer means ethylene, C3-C5α -olefins and C6-C9α -copolymerization product of olefins.
The polyolefin composition or the polyolefin composition prepared by the preparation method provided by the invention has the advantages of large molecular weight, wide molecular weight distribution, low crystallization rate and long molecular chain relaxation time, and finally leads to the widening of the processing temperature interval of the resin and the enhancement of the stretchability of the film, thereby meeting the application requirements of BOPE.
Drawings
FIG. 1 is a schematic view of a reaction apparatus in the examples.
Description of reference numerals: 1-a distribution plate; 2-a fluidized bed reactor; 3-a compression device; 4-a heat exchange device; 5-separation equipment; 6-a feed pump; 7-gas circulation line; 8-discharging tank; 9-purging the tank; 10-degassing bin; 11-a fluid conduit for introducing a hydrocarbon polymerization catalyst into the fluidized bed reactor; 12-a fluid conduit for introducing a condensate, olefin monomer, etc. into the fluidized bed reactor; 13-a fluid conduit for withdrawing a polymerization product from the fluidized bed reactor; 14-for mixing H2、N2And a fluid conduit for introducing ethylene into the recycle line; 15-a fluid conduit for introducing olefin monomer into the recycle line; 16-a fluid conduit for introducing a condensing agent into the circulation line; 17-a fluid conduit for introducing the stream separated by the separation device into the reactor.
Detailed Description
The present invention will be described in detail below with reference to examples, but the scope of the present invention is not limited to the following description.
The properties of the products obtained were tested according to the following criteria:
the Melt Index (MI) of the product was tested according to GB/T3682-2.16190 ℃ under a load of 2.16 kg);
testing the density of the product according to GB/T1033.2-2010;
testing the thickness of the film product according to GB/T6672-2001;
tensile properties of the product were measured according to ASTM D882.
The properties of the product obtained were tested using the following instruments:
measuring the weight average molecular weight and the molecular weight distribution of the product by a Polymer Laboratories PL-220 type gel permeation chromatograph;
measuring and calculating a function of the crystallization rate of the product by using a TA Q200 differential scanning calorimeter;
measuring the molecular chain relaxation time of the product by using a HAAKE RS6000 type rotational rheometer;
measuring the shear viscosity of the product by using a Malvern RH10Capillary Rheometers type high pressure Capillary rheometer;
measuring the spherulite size of the product by adopting an ECLIPSE E600W POL type polarizing microscope;
measuring the tensile property of the product by adopting an SRI800 type laboratory synchronous biaxial stretching machine;
the comonomer content was measured by means of a nuclear magnetic resonance spectrometer NMK/300 MHZ.
Example 1
In the fluidized-bed reactor 2 with internal nitrogen fluidization as shown in FIG. 1, a small amount of Ziegler-Natta catalyst (solid component TiCl-loaded) was first continuously fed through a line 11 at a rate of 0.1kg/h3The cocatalyst is triethyl aluminum, and Al: ti 60) and ethylene via line 14, 1-butene and 1-hexene via line 15 and a small amount of isopentane condensate via line 16. Then, the flow rate of the Ziegler-Natta catalyst was gradually increased to 5kg/h, and the flow rate of isopentane was gradually increased while keeping the fluidizing gas velocity constant. As the reaction proceeds, ethylene continues to be fed through line 14 and 1-butene feed gas continues to be fed through line 15 to form a circulating medium in the fluidized bed reactor. Wherein, the components and contents in the circulating medium are as follows: 35.2 mol% ethylene, 0.8 mol% 1-butene, 3.9 mol% 1-hexene, 4.7 mol% hydrogen, 30.6 mol% nitrogen and 24.8 mol% isopentane.
The circulating medium from the fluidized bed reactor 2 was received through a pipe 7 connected to the top expanded section of the fluidized bed reactor 2 (the circulating medium was received at a pressure of 2.4MPa and a temperature of 89 ℃). The circulating medium is treated by the heat exchanger 4 and then subjected to gas-liquid separation by the gas-liquid separator 5. Thus, 80 wt% of the total content of the condensing agent in the circulating medium is separately sprayed into the fluidized bed reactor 2 through the fluid pipe 12 at a position 2m above the distribution plate 1, and the rest of the condensing agent and the olefin monomer enter the fluidized bed reactor 2 along with the fluid pipe 17 below the distribution plate 1, thereby forming an upper high-temperature reaction zone (the highest temperature is 91 ℃) and a lower low-temperature reaction zone (the lowest temperature is 74 ℃) in the fluidized bed reactor, and the superficial fluidizing gas velocity is 0.42 m/s.
Under the temperature, pressure and apparent fluidization gas velocity, the first polymerization reaction of ethylene, 1-butene and 1-hexene is carried out for 2 hours, and the 1-butene/1-hexene/ethylene copolymer is generated. Intermittently discharging the generated solid-phase 1-butene/1-hexene/ethylene copolymer from a fluid pipeline 13, carrying out devolatilization treatment on the copolymer by a discharge tank 8, a purge tank 9 and a degassing bin 10 in sequence, and conveying the copolymer to a downstream working section for further processing to prepare the 1-butene/1-hexene/ethylene copolymer.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 0.51 mol%, and the content of the structural unit derived from 1-hexene was 2.91 mol%, and the rest of the results are shown in Table 1, Table 2 and Table 3.
Example 2
A1-butene/1-hexene/ethylene copolymer was prepared in the same manner as in example 1 except that:
the components and contents in the circulating medium are as follows: 30.6 mol% ethylene, 0.7 mol% 1-butene, 3.6 mol% 1-hexene, 4.1 mol% hydrogen, 40.9 mol% nitrogen and 20.1 mol% isopentane.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 0.43 mol%, and the content of the structural unit derived from 1-hexene was 2.64 mol%, and the rest of the results are shown in Table 1, Table 2 and Table 3.
Example 3
A1-butene/1-hexene/ethylene copolymer was prepared in the same manner as in example 1 except that:
the components and contents in the circulating medium are as follows: 28.7 mol% ethylene, 0.5 mol% 1-butene, 3.4 mol% 1-hexene, 3.8 mol% hydrogen, 46.2 mol% nitrogen and 17.4 mol% isopentane.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 0.30 mol%, and the content of the structural unit derived from 1-hexene was 2.55 mol%, and the rest of the results are shown in tables 1, 2 and 3.
Comparative example 1
A1-butene/1-hexene/ethylene copolymer was prepared in the same manner as in example 1 except that:
the components and contents in the circulating medium are as follows: 31.3 mol% ethylene, 0.4 mol% 1-butene, 2.7 mol% 1-hexene, 3.4 mol% hydrogen, 41.7 mol% nitrogen and 20.5 mol% isopentane.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 0.21 mol%, and the content of the structural unit derived from 1-hexene was 1.90 mol%, and the rest of the results are shown in tables 1, 2 and 3.
Comparative example 2
A1-butene/1-hexene/ethylene copolymer was prepared in the same manner as in example 1 except that:
the components and contents in the circulating medium are as follows: 29.9 mol% ethylene, 0.9 mol% 1-butene, 5.1 mol% 1-hexene, 4.0 mol% hydrogen, 40.5 mol% nitrogen and 19.6 mol% isopentane.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 0.78 mol%, and the content of the structural unit derived from 1-hexene was 3.62 mol%, and the rest of the results are shown in tables 1, 2 and 3.
Comparative example 3
A1-butene/1-hexene/ethylene copolymer was prepared in the same manner as in example 1 except that:
the components and contents in the circulating medium are as follows: 30.9 mol% ethylene, 0.7 mol% 1-butene, 3.6 mol% 1-hexene, 4.1 mol% hydrogen, 29.7 mol% nitrogen and 31.0 mol% isopentane.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 1.41 mol%, and the content of the structural unit derived from 1-hexene was 4.47 mol%, and the rest of the results are shown in tables 1, 2 and 3.
Comparative example 4
A1-butene/1-hexene/ethylene copolymer was prepared in the same manner as in example 1 except that:
the components and contents in the circulating medium are as follows: 28.7 mol% of ethylene, 0.7 mol% of 1-butene, 3.3 mol% of 1-hexene, 3.8 mol% of hydrogen and 63.5 mol% of nitrogen.
The properties of the obtained 1-butene/1-hexene/ethylene copolymer were tested, wherein the content of the structural unit derived from 1-butene was 0.15 mol%, and the content of the structural unit derived from 1-hexene was 0.90 mol%, and the rest of the results are shown in tables 1, 2 and 3.
Comparative example 5
The DOWLEX 2045G, a BOPE specific resin commercially available from Dow corporation, USA, was tested. The results are shown in tables 1, 2 and 3.
TABLE 1
TABLE 2
TABLE 3
According to the data in table 1, table 2 and table 3, it can be known that the polyolefin composition polyethylene prepared by the examples of the present application has a large molecular weight, a wide molecular weight distribution, a small crystallization rate and a long molecular chain relaxation time, which finally results in a widened processing temperature range of the resin and an enhanced stretchability of the film, meets the application requirements of the BOPE, and is significantly better than other comparative examples.
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.
Claims (10)
1. A polyolefin composition comprising: ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer, wherein, derived from C3-C5α -the content of structural units derived from olefins is from 0.2 mol% to 0.6 mol%, and/or derived from C6-C9α -the content of structural units of the olefin is from 2.5 mol% to 3.0 mol%.
2. Polyolefin composition according to claim 1, wherein C is3-C5α -olefin is selected from propylene and/or 1-butene, preferably 1-butene, C6-C9The α -olefin is selected from 1-hexene and/or 1-octene, preferably 1-hexene.
3. Polyolefin composition according to claim 1 or 2, characterized in that the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a density of 0.710g/cm3-1.125g/cm3Melt index MI2.160.01g/10min-10g/10min, weight average molecular weight above 100000, molecular weight distribution of 1-10, molecular chain relaxation time greater than 2.5s, crystallization rate function value less than 4, spherulite size less than 10 μm, and shear viscosity greater than 100Pa.s at shear rate of 1000/s.
4. Polyolefin composition according to any of claims 1 to 3, wherein the ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer has a density of 0.910g/cm3-0.925g/cm3Preferably 0.915g/cm3-0.920g/cm3Melt index MI2.160.5g/10min-3.0g/10min, preferably 0.5g/10min-2.0g/10min, a weight average molecular weight of 100000-500000, preferably 100000-120000, a molecular weight distribution of 2-6, preferably 3-5, a molecular chain relaxation time of more than 3s, a crystallization rate function value of less than 3, a spherulite size of less than 8 μm, and a shear viscosity at a shear rate of 1000/s of more than 150 Pa.s.
5. A process for the preparation of a polyolefin composition according to any of claims 1-4 comprising:
containing ethylene and C3-C5α -olefin, C6-C9α -contacting a reactant stream of olefin and condensing agent with an olefin polymerization catalyst to produce ethylene, C3-C5α -olefins and C6-C9α -olefin polymerization to said ethylene/C3-C5α -olefin/C6-C9α -olefin copolymer.
6. The method of claim 5, wherein the molar ratio of the ethylene to the condensing agent in the reactant stream is (0.5-3.0):1, preferably (1.0-2.0):1, more preferably (1.2-1.7): 1; said ethylene and said C3-C5α -olefin in a molar ratio of (30-80):1, preferably (40-60):1, the ethylene and the C6-C9α -olefin molar ratio is (5.0-12.0):1, preferably (8.0-10.0): 1.
7. The process according to claim 5 or 6, wherein the polymerization temperature is 20 ℃ to 120 ℃ and the polymerization pressure is 0.1MPa to 10 MPa.
8. The method of any one of claims 5-7, wherein the condensing agent is selected from C5-C8At least one alkane, preferably at least one selected from the group consisting of n-pentane, isopentane, cyclohexane, n-hexane, n-heptane and n-octane, more preferably isopentane and-Or n-heptane.
9. The production method according to any one of claims 5 to 8, wherein the olefin polymerization catalyst is at least one selected from the group consisting of a Ziegler-Natta catalyst, a metallocene catalyst and a late transition metal catalyst.
10. Use of a polyolefin composition according to any of claims 1 to 4 or a polyolefin composition prepared by the preparation process according to any of claims 5 to 9 as a biaxially oriented polyolefin feedstock.
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