Polyolefin compositions obtained from recycled polyolefins

Abstract

A polypropylene composition comprising: (a) from 55 wt% to 80 wt% of a crystalline propylene polymer; (b) from 12 wt% to 30 wt% of an elastomeric terpolymer of propylene, ethylene and 1-butene; and (c) from 8 wt% to 25 wt% of recycled polyethylene (r-PE); the percentages of (a), (b) and (c) being relative to the sum of (a), (b) and (c).

Description

Technical Field

[0001] The present disclosure relates to polyolefin compositions containing recycled polyethylene that are useful for injection molded articles, particularly grates and pails. Background Art

[0002] WO 2006 / 125720 describes a polyolefin composition for this use, made from: a) 65% to 77%, preferably 70% to 77%, of a crystalline propylene polymer having an amount of isotactic pentads (mmmm) greater than 97.5 mol%, measured by 13C-MNR on the fraction insoluble in xylene at 25° C., and a polydispersity index ranging from 5 to 10; b) 8% to less than 13%, preferably 9% to 12%, of an elastomer of ethylene and propylene. A copolymer having an amount of repeating units derived from ethylene ranging from 30% to 70%, preferably from 35% to 60%, and being partially soluble in xylene at ambient temperature; the polymer fraction soluble in xylene at ambient temperature having an intrinsic viscosity value ranging from 2 dl / g to 4 dl / g; and c) 10% to 23%, preferably from 10% to 20%, of polyethylene having an intrinsic viscosity value ranging from 1.5 dl / g to 4 dl / g and optionally containing repeating units derived from propylene in an amount lower than 10%.

[0003] Polyolefin compositions suitable for these applications have good stiffness, impact resistance and stress whitening resistance.

[0004] Generally speaking, polyolefin compositions, although appreciated in terms of performance, raise concerns in terms of sustainability, particularly with reference to the fact that their production is based on the use of non-renewable resources.

[0005] Therefore, a common attempt to alleviate this problem is to use variable amounts of recycled polyolefins, such as polypropylene or polyethylene, in the multicomponent polyolefin composition.

[0006] Recycled polyolefins are derived from post-consumer waste (PCW) material streams that have been separated from other polymers such as PVC, PET or PS through various steps.

[0007] In polyolefin recycling, especially when processing material streams from post-consumer waste (PCW), one of the key issues is the difficulty in quantitatively separating polypropylene (PP) from polyethylene (PE), and vice versa. Therefore, although referred to as recycled PE (rPE) or recycled PP (rPP), commercial products from PCW sources have been found to be mixtures of varying amounts of PP and PE.

[0008] This fact, coupled with the presence in the recycled materials of additives and secondary components that may not be fully adapted to the applications for which they are supposed to be used, leads to the consequence that such recycled PP / PE blends suffer from a deterioration in mechanical and optical properties during remolding, as well as poor compatibility between the main polymer phases. As a result, articles using r-PP or r-PE are considered less reliable due to the lower performance of the compositions used in these articles.

[0009] Therefore, the use of recycled materials in applications requiring high performance levels is strongly discouraged and limited to low-cost and less demanding applications.

[0010] It has now been unexpectedly found that the presence of a recycled PE component in certain polypropylene compositions for use in water management systems does not impair performance and makes their production processes more sustainable. Summary of the Invention

[0011] Therefore, the object of the present disclosure is a polypropylene composition comprising:

[0012] (a) from 55 to 80 wt.-%, preferably from 60 to 77 wt.-%, more preferably from 63 to 75 wt.-% of a crystalline propylene polymer having an amount of isotactic pentads (mmmm) higher than 97.0 mol.-%, as measured by 13C-MNR on the fraction insoluble in xylene at 25° C., and a polydispersity index ranging from 3 to 15;

[0013] b) from 12 to 30 wt.-%, preferably from 15 to 23 wt.-%, more preferably from 17 to 21 wt.-% of an elastomeric terpolymer of propylene, ethylene and 1-butene, the terpolymer having an amount of repeating units derived from ethylene in an amount ranging from 30.0 to 70.0 wt.-%, preferably from 35.0 to 60.0 wt.-%, more preferably from 40.0 to 53.0 wt.-% as measured by 13C-NMR, and an amount of repeating units derived from 1-butene in an amount ranging from 5.0 to 25.0 wt.-%, preferably from 10.0 to 20.0 wt.-%, more preferably from 12.0 to 18.0 wt.-%, as measured by 13C-NMR,

[0014] Wherein in the blend of components a) and b):

[0015] i) the xylene-soluble polymer fraction of components a) + b) at 25° C. ranges from 15.0 wt. % to 30.5 wt. %; preferably ranges from 18.0 wt. % to 28.2 wt. %; more preferably ranges from 22.0 wt. % to 27.1 wt. %;

[0016] ii) the xylene-soluble polymer fraction of components a) + b) at 25° C. has an intrinsic viscosity value, measured in tetralin at 135° C., in the range of from 2.5 dl / g to 4.8 dl / g; preferably in the range of from 3.1 dl / g to 4.5 dl / g; more preferably in the range of from 3.4 dl / g to 4.3 dl / g;

[0017] iii) By 13 The content of ethylene-derived units in the xylene-soluble fraction of components a) + b at 25° C., as measured by C-MNR, ranges from 20.4 to 37.5% by weight; preferably ranges from 23.0 to 35.0% by weight; more preferably ranges from 25.0 to 32.0% by weight;

[0018] iv) the melting point of components a) + b as measured by DSC ranges from 148.0°C to 168°C; preferably ranges from 154°C to 167°C; more preferably ranges from 162.0°C to 166°C;

[0019] v) the melt flow rate (ISO 1133-1230°C / 2.16 kg) of components a) + b ranges from 0.1 g / 10 min to 10.0 g / 10 min; preferably ranges from 0.5 g / 10 min to 8.0 g / 10 min; more preferably ranges from 1.0 g / 10 min to 5.0 g / 10 min;

[0020] The polypropylene composition further comprises:

[0021] (c) from 8 to 25 wt%, preferably from 8 to 20 wt%, more preferably from 8 to 15 wt% of recycled polyethylene (r-PE) having a melt flow rate (ISO 1133-1190°C / 2.16 Kg) of from 0.1 to 10 g / 10 min and containing a polypropylene content in an amount ranging from 1 to 15 wt% of the total r-PE component;

[0022] The entire composition has a melt flow rate (ISO 1133-1230°C / 2.16kg) value ranging from 0.1 g / 10 min to 10.0 g / 10 min; preferably ranging from 0.5 g / 10 min to 8.0 g / 10 min; more preferably ranging from 1.0 g / 10 min to 5.0 g / 10 min;

[0023] The percentages of (a), (b) and (c) are relative to the sum of (a), (b) and (c). DETAILED DESCRIPTION

[0024] As used herein, the term "copolymer" refers to polymers having two different repeating units in the chain and polymers having more than two different repeating units, such as terpolymers. "Ambient temperature" herein means a temperature of 25°C (room temperature).

[0025] The term "crystalline propylene polymer" is understood in the present application to mean a propylene polymer having an amount of isotactic pentads (mmmm) greater than 70 mol%, as measured by 13C-MNR on the fraction insoluble in xylene at 25°C; an "elastomeric" polymer is understood to mean a polymer having a solubility in xylene at ambient temperature greater than 50 wt%.

[0026] Not all characteristics of copolymers (a) to (c) are inextricably linked to one another. This means that a certain level of preference for one of these characteristics does not necessarily lead to the same level of preference for the remaining characteristics.

[0027] The crystalline propylene polymer (a) is selected from propylene homopolymers and propylene copolymers containing up to 3.0 wt.% of ethylene or C4-C10 α-olefins or a combination thereof. Particularly preferred are propylene homopolymers.

[0028] Preferably, the polydispersity index ranges from 3 to 10.

[0029] The r-PE(c) is a crystalline or semi-crystalline high density PE (r-HDPE) selected from commercial PCW (e.g. post-consumer waste from municipalities). Preferably, the r-PE(c) has a density ranging from 0.940 g / cm 3 to 0.965g / cm 3 The density (ISO 1183-1) and the melt flow rate (ISO 1133-1190°C / 2.16Kg) are from 0.1 g / 10 min to 1.0 g / 10 min.

[0030] Before its use, the plastic mixture containing rHDPE undergoes a standard recycling process, including collection, shredding, sorting and washing. Although sorted rHDPE is composed of a large amount of HDPE, it always contains small amounts of other polymers and / or inorganic components. In particular, the r-PE according to the present disclosure contains a polypropylene content of from 1% to 15% by weight, preferably from 5% to a maximum of 10% by weight, of the total r-PE component.

[0031] In a preferred embodiment, the r-PE comprises a crystalline polyethylene fraction in which the amount of repeating units derived from propylene in the polyethylene chain is less than 11 wt%, and most preferably they are absent, i.e. most preferably the r-PE is an ethylene homopolymer containing the above inclusions. Preferably, the (r-PE) has a melt flow rate (ISO 1133-1190°C / 2.16Kg) of from 0.1 g / 10 min to 1.0 g / 10 min, and more preferably from 0.1 g / 10 min to 0.5 g / 10 min.

[0032] r-PE is commercially available. An example of a suitable r-PE grade is represented by the ivory or grey version of the grade sold by Lyondellbasell under the trade name Hostalen QCP5603.

[0033] The compositions of the present disclosure preferably show tensile modulus values ​​ranging from 500 MPa to 1000 MPa, preferably from 600 MPa to 900 MPa, even more preferably from 650 MPa to 850 MPa.

[0034] The Charpy impact resistance value at 23°C is preferably higher than 70.0 kJ / m 2 , preferably in the range of 70kJ / m 2 Up to 130.0kJ / m 2 , more preferably in the range of 80.0 kJ / m 2 Up to 120.0kJ / m 2 ; Charpy impact resistance at 0 ° C is preferably greater than 40.0kJ / m 2 , preferably in the range of 45.0 kJ / m 2 Up to 110.0kJ / m 2 , more preferably in the range of 50.0 kJ / m 2 Up to 100.0kJ / m 2 , and the Charpy impact resistance at -20°C is preferably at least 6.5 kJ / m 2 ; The preferred range is from 7.0kJ / m 2 Up to 15.0kJ / m 2 .

[0035] The compositions of the present disclosure can be obtained by mechanically blending components (a) to (c) according to conventional techniques.

[0036] According to a preferred method of preparation, component (c) is mechanically blended with a preformed heterogeneous composition comprising components (a) and (b) associated together by a sequential copolymerization process.

[0037] The process comprises polymerizing propylene alone or in a mixture with a small amount of ethylene in a first stage and then polymerizing propylene with a higher amount of ethylene in a second stage, both stages being carried out in the presence of a catalyst comprising the reaction product between:

[0038] i) a solid catalyst component comprising Ti, Mg, Cl and at least one inner electron body compound;

[0039] ii) an alkylaluminum compound and,

[0040] iii) external electron donor compounds having the following general formula:

[0041] (R 7 ) a (R 8 ) b Si(OR 9 ) c , wherein a and b are integers from 0 to 2, c is an integer from 1 to 4, and the sum of (a+b+c) is 4; R 7 、R 8 and R 9 is an alkyl, cycloalkyl or aryl radical having 1 to 18 carbon atoms, which may optionally contain heteroatoms.

[0042] The internal donor is preferably selected from esters of mono- or dicarboxylic organic acids, such as benzoates, malonates, phthalates and certain succinates. Examples of internal donors are described in US 4522930A, EP 045977A2 and international patent applications WO 00 / 63261 and WO 01 / 57099. Particularly suitable are phthalates and succinates. Alkyl phthalates are preferred, such as diisobutyl phthalate, dioctyl phthalate and diphenyl phthalate, as well as benzylbutyl phthalate.

[0043] The particles of solid component (i) may have a substantially spherical morphology and an average diameter ranging between 5 μm and 150 μm, preferably from 20 μm to 100 μm, and more preferably from 30 μm to 90 μm. As particles having a substantially spherical morphology, those particles are meant in which the ratio between the major axis and the minor axis is equal to or lower than 1.5, and preferably lower than 1.3.

[0044] The amount of Mg may preferably range from 8 to 30%, more preferably from 10 to 25 wt%.

[0045] The amount of Ti may range from 0.5 wt% to 7 wt%, and more preferably from 0.7 wt% to 5 wt%.

[0046] According to one method, the solid catalyst component (i) can be prepared by reacting a titanium compound of the formula Ti(OR)q-yXy (wherein q is the valence of titanium and y is a number between 1 and q, preferably TiCl4) with magnesium chloride derived from an adduct of the formula MgCl2·pROH (wherein p is a number between 0.1 and 6, preferably from 2 to 3.5, and R is a hydrocarbyl radical having 1 to 18 carbon atoms). The adduct can be suitably prepared in spherical form by mixing an alcohol and magnesium chloride, operating under stirring conditions at the melting temperature of the adduct (100°C to 130°C). The adduct is then mixed with an inert hydrocarbon immiscible with the adduct, thereby producing an emulsion that is rapidly quenched, resulting in the solidification of the adduct in the form of spherical particles. Examples of spherical adducts prepared according to this procedure are described in USP 4,399,054 and USP 4,469,648. The adduct thus obtained can be reacted directly with the Ti compound, or it can be previously subjected to a thermally controlled dealcoholation (80° C. to 130° C.) to obtain an adduct in which the number of moles of alcohol is less than 3, preferably between 0.1 and 2.5. The reaction with the Ti compound can be carried out by suspending the adduct (dealcoholated or as such) in cold TiCl4; the mixture is heated to 80° C. to 130° C. and maintained at this temperature for 0.5 to 2 hours. The treatment with TiCl4 can be carried out once or several times. The electron donor compound can be added during the treatment with TiCl4 in the desired ratio.

[0047] The alkyl-Al compound (ii) is preferably selected from trialkylaluminum compounds such as, for example, triethylaluminum, triisobutylaluminum, tri-n-butylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum. Alkylaluminum halides, alkylaluminum hydrides or alkylaluminum sesquichlorides such as AlEt2Cl and Al2Et3Cl3 can also be used, possibly mixed with the above-mentioned trialkylaluminums. The Al / Ti ratio is higher than 1 and can preferably be in the range between 50 and 2000.

[0048] Particularly preferred are silicon compounds (iii) in which a is 1, b is 1, c is 2, at least one of R7 and R8 is selected from a branched alkyl, cycloalkyl or aryl group having 3 to 10 carbon atoms, optionally containing heteroatoms, and R9 is a C1-C10 alkyl group, in particular a methyl group. Examples of such preferred silicon compounds are methylcyclohexyldimethoxysilane (C donor), diphenyldimethoxysilane, methyl tert-butyldimethoxysilane, dicyclopentyldimethoxysilane (D donor), diisopropyldimethoxysilane, (2-ethylpiperidinyl)tert-butyldimethoxysilane, (2-ethylpiperidinyl)tert-hexyldimethoxysilane, (3,3,3-trifluoro-n-propyl) (2-ethylpiperidinyl)dimethoxysilane, methyl (3,3,3-trifluoro-n-propyl) dimethoxysilane. Furthermore, preferred are silicon compounds wherein a is 0, c is 3, R8 is a branched alkyl or cycloalkyl group optionally containing heteroatoms, and R9 is methyl. Examples of such preferred silicon compounds are cyclohexyltrimethoxysilane, tert-butyltrimethoxysilane, and tert-hexyltrimethoxysilane.

[0049] The external electron donor compound (iii) is used in such an amount that the molar ratio between the organoaluminium compound and said external electron donor compound (iii) is from 0.1 to 200, preferably from 1 to 100, and more preferably from 3 to 50.

[0050] The polymerization process can be carried out in the gas phase, operating in one or more fluidized bed or mechanically stirred bed reactors, using an inert hydrocarbon solvent as a diluent for slurry polymerization, or using a liquid monomer (such as propylene) as the reaction medium for bulk polymerization.

[0051] Preferably, the heterophasic composition used in the present disclosure is obtained by a sequential polymerization process in two or more stages, wherein component (a) is obtained in a first stage and then component (b) is obtained in the presence of component (a) in a second stage. Each stage can be carried out in the gas phase, operating in one or more fluidized bed or mechanically stirred bed reactors, or in bulk using liquid monomer (e.g. propylene) as the reaction medium. Also preferred are hybrid processes in which one stage (preferably the stage for preparing component (a)) is carried out in liquid monomer and another stage (preferably the stage for preparing component (b)) is carried out in the gas phase.

[0052] According to a preferred embodiment, component (a) is produced in a gas phase reactor, as described in EP 782587, comprising a first and a second interconnected polymerization zone, into which propylene and optionally ethylene are fed in the presence of a catalyst system and from which the produced polymer is discharged. The growing polymer particles flow under fast fluidization conditions through the first polymerization zone (riser), leave the first polymerization zone and enter the second polymerization zone (downcomer), where they flow under gravity in a densified form through the second polymerization zone, leave the second polymerization zone and are reintroduced into the first polymerization zone, thereby establishing a polymer circulation between the two polymerization zones. Typically, fast fluidization conditions in the first polymerization zone are established by feeding a monomer gas mixture below the point at which the growing polymer is reintroduced into the first polymerization zone. The velocity of the transport gas entering the first polymerization zone is higher than the transport velocity under operating conditions and is typically between 2 m / s and 15 m / s. In the second polymerization zone, in which the polymer flows in a densified form under the action of gravity, a high solid density value close to the bulk density of the polymer is reached; a positive pressure gain can therefore be obtained along the flow direction, making it possible to reintroduce the polymer into the first reaction zone without the aid of mechanical means. In this way, a "loop" circulation is established, which is defined by the pressure balance between the two polymerization zones and the head loss introduced into the system. Optionally, one or more inert gases, such as nitrogen or aliphatic hydrocarbons, are maintained in the polymerization zone in an amount such that the sum of the partial pressures of the inert gases is preferably between 5% and 80% of the total gas pressure. Preferably, the various catalyst components are fed to the first polymerization zone at any point in the first polymerization zone. However, they can also be fed at any point in the second polymerization zone. Molecular weight regulators known in the art (particularly hydrogen) can be used to regulate the molecular weight of the growing polymer. If a bimodal arrangement is required, a barrier flow can be used to separate the polymerization environments of the riser and downcomer as described in EP-A-1012195.

[0053] The polymerization can be carried out at a temperature of from 20°C to 120°C, preferably from 40°C to 80°C. When the polymerization is carried out in the gas phase, the operating pressure can range from 0.5 MPa to 5 MPa, preferably from 1 MPa to 4 MPa. In bulk polymerization, the operating pressure can range from 1 MPa to 8 MPa, preferably from 1.5 MPa to 5 MPa. Hydrogen can be used as a molecular weight regulator.

[0054] If desired, the final heterogeneous composition comprising (a) + (b) can be chemically treated with an organic peroxide to reduce the average molecular weight and increase the melt flow index to the value required for a particular application.

[0055] The final composition comprising components (a) to (c) can be added with conventional additives, fillers and pigments commonly used in olefin polymers (such as nucleating agents, extender oils, mineral fillers and other organic and inorganic pigments). In particular, the addition of inorganic fillers such as talc, calcium carbonate and mineral fillers will also improve some mechanical properties such as flexural modulus and HDT. Talc can also have a nucleating effect.

[0056] For example, the nucleating agent is added to the composition of the present disclosure in an amount ranging from 0.05 wt% to 2 wt%, more preferably from 0.1 wt% to 1 wt%, relative to the total weight.

[0057] The polypropylene composition of the present disclosure can be used to obtain injection molded articles of various objects. Particularly preferred is the use of the polypropylene composition for preparing automotive battery boxes.

[0058] As shown in the examples below, compositions employing r-PE do not show any degradation of properties relative to compositions employing virgin PE having similar characteristics.

[0059] The following examples are given to illustrate but not to limit the present disclosure.

[0060] Examples

[0061] Characterization

[0062] Xylene soluble (XS) fraction at 25°C

[0063] 2.5 g of polymer and 250 ml of xylene were introduced into a glass flask equipped with a refrigerator and a magnetic stirrer. The temperature was raised to the boiling point of the solvent over 30 minutes. The resulting clear solution was then held at reflux and stirred for 30 minutes. The sealed flask was then placed in an ice-water bath for 30 minutes, followed by a 25°C constant-temperature water bath for 30 minutes. The resulting solid was filtered through rapid filter paper. 100 ml of the filtrate was poured into a pre-weighed aluminum container and heated on a hot plate under a nitrogen stream to remove the solvent by evaporation. The container was then kept in an oven at 80°C under vacuum until constant weight was reached. The weight percentage of polymer soluble in xylene at room temperature was then calculated.

[0064] The content of the xylene soluble fraction is expressed as a percentage of the original 2.5 g and then expressed as a xylene insoluble percentage (%) by difference (made up to 100%);

[0065] Melt flow rate (MFR)

[0066] Unless otherwise specified, measured according to ISO 1133-1 at 230°C and a load of 2.16 kg.

[0067] density

[0068] Measured according to ISO 1183-1.

[0069] Intrinsic viscosity (IV)

[0070] The sample is dissolved in tetralin at 135°C and then poured into a capillary viscometer. The viscometer tube (Ubbelohde type) is surrounded by a cylindrical glass jacket; this setup allows temperature control with a circulating thermostatic liquid. The downward passage of the meniscus is timed by a photoelectric device.

[0071] The meniscus's passage in front of the upper lamp starts a counter with a quartz crystal oscillator. When it passes the lower lamp, the meniscus stops the counter, and the outflow time is recorded: this is converted to an intrinsic viscosity value using Huggins' equation (Huggins, ML, J. Am. Chem. Soc., 1942, 64, 2716), provided that the flow time of the pure solvent under the same experimental conditions (same viscometer and same temperature) is known. A single polymer solution is used to determine [η].

[0072] Polydispersity index: measured at a temperature of 200° C. using a parallel plate rheometer model RMS-800 sold by RHEOMETRICS (USA), operated at an oscillation frequency increasing from 0.1 rad / s to 100 rad / s. From the crossover modulus, the PI can be derived by the following equation:

[0073] PI=105 / Gc

[0074] Wherein Gc is the crossover modulus, which is defined as the value (expressed in Pa) where G'=G", where G' is the storage modulus and G" is the loss modulus.

[0075] Determination of ethylene and 1-butene content

[0076] 13 C NMR spectra were acquired on a Bruker AV600 spectrometer equipped with a cryoprobe and operated at 150.91 MHz in Fourier transform mode at 120 °C.

[0077] At 29.9ppm S δδThe carbon peak (according to the nomenclature of CJ Carman, RA Harrington and CE Wilkes, Macromolecules, 10, 3, 536 (1977)) was used as an internal reference. Approximately 30 mg of sample was dissolved in 0.5 ml of 1,1,2,2-tetrachloroethane-d2 at 120°C. Each spectrum was acquired with 90° pulses with a 15 second delay between pulses and CPD was used to remove 1 H- 13 C coupling. 512 transient data were stored in 65K data points using a spectral window of 9000 Hz.

[0078] The triple distribution is obtained using the following relation:

[0079] XPX=100I8 / Σ

[0080] XPE=100I5 / Σ

[0081] EPE=100I4 / Σ

[0082] XBX=100I3 / Σ

[0083] XBE=100I2 / Σ

[0084] XEX=100I9 / Σ

[0085] XEE=100I1 / Σ

[0086] EEE=100(0.5I7+0.25I6) / Σ

[0087] Where Σ=I8+I5+I4+I3+I2+I9+I1+0.5I7+0.25I6

[0088] I is the area corresponding to the carbon reported in Table a,

[0089] And X may be propylene or 1-butene.

[0090] The molar contents of ethylene, propylene, and 1-butene were obtained from the triads using the following relationships:

[0091] P(m%)=XPX+XPE+EPE

[0092] B(m%)=XBX+XBE+EBE

[0093] E(m%)=EEE+XEE+XEX

[0094] The molar contents were converted to weights using the monomer molecular weights.

[0095] Table A: Ethylene / propylene / 1-butene terpolymers13 C NMR spectral assignment

[0096] serial number Chemical shift (ppm) carbon sequence 1 37.64-37.35 <![CDATA[S αδ ]]> PEE 2 37.35-37.15 <![CDATA[T βδ ]]> XBE 3 35.27-34.92 <![CDATA[T ββ ]]> XBX 4 33.29-33.15 <![CDATA[T δδ ]]> EPE 5 30.93-30.77 <![CDATA[T βδ ]]> XPE 6 30.35-30.26 <![CDATA[S γδ ]]> PEEE 7 29.97-29.85 <![CDATA[S δδ ]]> EEE 8 29.14-28.31 <![CDATA[T ββ ]]> XPX 9 24.88-24.14 <![CDATA[S ββ ]]> XEX

[0097] The ethylene C2 content of component b has been measured by measuring the C2 content on component a+b) and then calculated by using the formula C2tot=+XbC2b2, where Xb is the amount of component b in the composition. A similar calculation was performed for 1-butene.

[0098] Samples for mechanical testing

[0099] The samples were obtained according to ISO 1873-2:2007.

[0100] Charpy impact test determined according to ISO 179-1eA and ISO 1873-2.

[0101] Elongation at yield: measured according to ISO 527.

[0102] Elongation at break: measured according to ISO 527

[0103] Breaking stress: measured according to ISO 527.

[0104] Tensile modulus: measured according to ISO 527-2.

[0105] Melting point and crystallization point

[0106] Melting points were measured using a DSC instrument according to ISO 11357-3, both under cooling and heating at a scan rate of 20° C. / min under an inert N 2 flow on samples weighing between 5 and 7 mg. Instrument calibration was performed with indium.

[0107] Determination of PP content in r-PE

[0108] 13 C NMR spectra were acquired on a Bruker AV-600 spectrometer equipped with a cryoprobe and operated at 120 °C in Fourier transform mode at 160.91 MHz.

[0109] The peak of CH2 ethylene was used as an internal standard at 29.9 ppm. The sample was dissolved in 1,1,2,2-tetrachloroethane-d2 at a concentration of 8 wt / vol% at 120°C. Each spectrum was acquired with 90° pulses with a 15 s delay between pulses and CPD was used to remove 1 H- 13 C coupling. 512 transient data were stored in 32K data points using a 9000 Hz spectral window.

[0110] The molar composition was obtained using the peak areas as follows (Table 1):

[0111] P=100A3 / S

[0112] E=1000.5A2 / S

[0113] Where S = 0.5A2 + A3

[0114] The molar contents were converted to weights using the monomer molecular weights.

[0115] Table B: Distribution of PP / PE blends

[0116] serial number Chemical shift (ppm) carbon sequence 1 48.8-45.4 <![CDATA[CH2]]> P 2 29.9 <![CDATA[CH2]]> E 3 29.0-28.0 CH P 4 21.8-19.8 CH3 P

[0117] Examples

[0118] Example 1

[0119] In a plant operating continuously according to the mixed liquid-gas polymerization technology, operations were carried out under the conditions specified in Table B.

[0120] The polymerization is carried out in the presence of the catalyst system in a series of two reactors equipped with means for transferring the product from one reactor to the reactor immediately adjacent thereto.

[0121] Preparation of solid catalyst components

[0122] At 0°C, 250 ml of TiCl4 was introduced into a 500 ml four-necked round-bottom flask purged with nitrogen. While stirring, 10.0 g of microspherical MgCl2·1.9C2H5OH (prepared according to the method described in Example 2 of USP 4,399,054, but operated at 3000 rpm instead of 10000 rpm) and 9.1 mmol of diethyl 2,3-(diisopropyl)succinate were added. The temperature was raised to 100°C and maintained for 120 minutes. Then, stirring was stopped, the solid product was allowed to settle, and the supernatant was siphoned off. 250 ml of fresh TiCl4 was then added. The mixture was reacted at 120°C for 60 minutes, and then the supernatant was siphoned off. The solid was washed six times with anhydrous hexane (6×100 ml) at 60°C.

[0123] Catalyst system and prepolymerization treatment

[0124] The solid catalyst component described above was contacted with triethylaluminum (TEAL) and dicyclopentyldimethoxysilane (DCPMS) as an external electron donor component for 24 minutes at 12° C. The weight ratios between TEAL and the solid catalyst component and between TEAL and DCPMS are specified in Table 1.

[0125] The catalyst system was then subjected to prepolymerization by maintaining it in suspension in liquid propylene at 20°C for about 5 minutes before being introduced into the first polymerization reactor.

[0126] Polymeric components a) and b)

[0127] Polymerization operation is carried out continuously in a series of two reactors, and these reactors are equipped with the equipment that product is transferred from one reactor to the reactor next to it.As described in European patent EP 782587, the first reactor is a gas phase polymerization reactor with two interconnected polymerization zones (riser and downcomer).The second reactor is a fluidized bed gas phase reactor.Respectively, polymer (a) is prepared in the first reactor, and polymer (b) is prepared in the second reactor.Temperature and pressure are maintained constant in the whole reaction process.Hydrogen is used as molecular weight regulator.

[0128] The gas phase (propylene, ethylene, 1-butene and hydrogen) was analyzed continuously by gas chromatography.

[0129] At the end of the run, the powder was discharged and dried under a stream of nitrogen. The polymerization parameters are reported in Table 1

[0130] Table 1 - Polymerization process

[0131] Example 1 Comparative Example 2 Component A TEAL / external donor Weight / Weight 10 5 TEAL / Catalyst Weight / Weight 5 5 temperature ℃ 68 70 pressure -bar 26 27 <![CDATA[H2 / C3 - Riser]]> mole / mole 0.011 0.011 Component B temperature ℃ 80 75 pressure -bar 14 1.8 Split ％ 22 13.5 <![CDATA[C2 - / C2 - +C3 - ]]> mole / mole 0.420 0.35 H2 / C2- mole / mole 0.010 0.014 <![CDATA[C4 - / C4 - +C3 - ]]> mole / mole 0.292 -

[0132] The polymer pellets of the heterophasic compositions of Example 1 and Comparative Example 2 were then introduced into a twin-screw extruder (Werner type extruder) where they were mixed with 10% and 20% by weight (based on the total amount of polyolefin) of QCP5603 Ivory (r-PE commercialized by LyondellBasell, containing 10% by weight of PP content) and a standard stabilizer package. The polymer pellets were extruded in a twin-screw extruder at a rotation speed of 250 rpm and a melt temperature of 200° C. to 250° C. under a nitrogen atmosphere.

[0133] Table 2 - Characterization

[0134]

[0135]

[0136] The properties of the final compositions are reported in Table 3.

[0137] Table 3 - Properties of the final composition

[0138]

[0139] The above data show that the polymer composition according to the present disclosure has better impact properties than the comparative example.

Claims

1. A polypropylene composition comprising: (a) from 55 to 80 weight percent of a crystalline propylene polymer having a 13 C-NMR measured on the xylene-insoluble fraction at 25° C., an amount of isotactic pentads (mmmm) higher than 97.0 mol % and a polydispersity index ranging from 3 to 15; (b) from 12 to 30 weight percent of an elastomeric terpolymer of propylene, ethylene, and 1-butene, said terpolymer having a 13 The amount of repeating units derived from ethylene ranges from 30.0 wt% to 70.0 wt% as measured by C-NMR, and 13 the repeating units derived from 1-butene in an amount ranging from 5.0 wt% to 25.0 wt% as measured by C-NMR; Wherein in the blend of components a) and b): i) the xylene-soluble polymer fraction of components a) + b) at 25° C. ranges from 15.0 wt. % to 30.5 wt. %; ii) said polymer fraction of components a) + b) soluble in xylene at 25° C. has an intrinsic viscosity measured in tetralin at 135° C. in the range of from 2.5 dl / g to 4.8 dl / g; iii) By 13 The content of ethylene-derived units in the fraction soluble in xylene at 25° C., measured by C-NMR, ranges from 20.4% to 37.5% by weight; iv) a melting point ranging from 148.0°C to 168°C as measured by DSC; v) melt flow rate, ISO 1133-1 230°C / 2.16 kg, ranges from 0.1 g / 10 min to 10.0 g / 10 min; The polypropylene composition further comprises: (c) from 8 to 25 wt% recycled polyethylene (r-PE) having a melt flow rate from 0.1 to 10.0 g / 10 min, ISO 1133-1 190°C / 2.16 Kg, and containing a polypropylene content in an amount ranging from 1 to 15 wt% of the total r-PE component; The entire composition has a melt flow rate value ranging from 0.1 g / 10 min to 10.0 g / 10 min, ISO 1133 - 1230°C / 2.16 kg; The percentages of (a), (b) and (c) are relative to the sum of (a), (b) and (c).

2. The polypropylene composition according to claim 1, wherein: Component (a) ranges from 60 wt% to 77 wt%; Component (b) ranges from 15 wt% to 23 wt%; Component (c) ranges from 8 wt% to 20 wt%.

3. The polypropylene composition according to claim 2, wherein the polymer fraction of components a) + b) soluble in xylene at 25°C ranges from 18.0 wt% to 28.2 wt%.

4. The polypropylene composition according to claim 1, having a melt flow rate ranging from 0.5 g / 10 min to 8.0 g / 10 min, ISO 1133-1 230°C / 2.16 kg.

5. The polypropylene composition according to claim 1, wherein component (c) has a polypropylene content in an amount ranging from 5 wt% to 10 wt%, based on the total amount of component (c).

6. The polypropylene composition according to claim 1, wherein component (c) has a molecular weight ranging from 0.940 g / cm 3 to 0.965g / cm 3 Density, ISO 1183-1, and melt flow rate, ISO 1133-1 190°C / 2.16Kg from 0.1 g / 10 min to 1 g / 10 min.

7. The polypropylene composition according to claim 1, wherein the xylene-soluble polymer fraction of components a) + b) at 25°C has an intrinsic viscosity value measured in tetralin at 135°C in the range of from 3.1 to 4.5 dl / g.

8. The polypropylene composition according to claim 1, wherein 13 The content of the ethylene-derived units in the fraction of components a)+b) soluble in xylene at 25° C., as measured by C-NMR, ranges from 23.0% to 35.0% by weight.

9. The polypropylene composition according to claim 1, wherein component (b) has 13 The amount of ethylene measured by C-NMR ranges from 35 wt% to 60 wt% and by 13 The amount of 1-butene measured by C-NMR ranged from 10.0 wt% to 20.0 wt%.

10. The polypropylene composition according to claim 1, wherein the intrinsic viscosity of the xylene soluble fraction of components a) + b) at 25°C ranges from 3.4 dl / g to 4.3 dl / g.

11. The polypropylene composition according to claim 1 , wherein the melting point of components a) + b as measured by DSC ranges from 154 to 167°C.

12. The polypropylene composition according to claim 1, wherein the melt flow rate of components a) + b, ISO 1133-1 230°C / 2.16 kg, ranges from 0.5 g / 10 min to 8.0 g / 10 min.

13. The polypropylene composition according to claim 1, wherein the melt flow rate of components a) + b, ISO 1133-1 230°C / 2.16 kg, ranges from 1.0 g / 10 min to 5.0 g / 10 min.

14. An injection molded article made from the composition according to claim 1.

15. The injection molded article according to claim 14, which has the form of an automobile battery box.

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