The present invention relates to containers especially containers for food having a particular balance of mechanical and optical properties. Said container comprises a propylene/ethylene/ 1-hexene terpolymer having particular properties.

Propylene/ethylene/ 1-hexene terpolymer are already known in the art mainly for the production of pipes or films.

For example WO2006/002778 relates to a pipe system comprising a terpolymer of propylene/ethylene and alpha olefin wherein the ethylene content is from 0 to 9% by mol, preferably from 1 to 7% by mol and the 1-hexene content ranges from 0.2 to 5% wt.

US 6,365,682 relates to propylene based terpolymers to be used for films. The ethylene content ranges generally from 1 to 10 wt and the alpha olefin ranges from 5 to 25wt%. for the preparation of films terpolymers having an ethylene content ranging from 0.9 to 3 wt and an alpha olefin content ranging from 1 to 15wt is indicated. Only terpolymer of propylene/ethylene and 1-butene are exemplified.

The applicant found that containers preferably a container for food can be obtained by using a propylene-ethylene- 1-hexene terpolymer having a particular composition.

Thus an object of the present invention is a container, preferably a container for food comprising a propylene, ethylene, 1-hexene terpolymer wherein in the terpolymer:

i) the content of ethylene derived units ranges from 0.5 wt to 2.0 wt ; preferably from 0.7wt to 1.5 wt ; more preferably from 0.9 wt to 1.3 wt ;

ii) the content of 1-hexene derived units ranges from 1.5 wt to 5.5 wt ; preferably from 1.8 wt% to 5.0 wt ; more preferably from 2.0 wt% to 4.5 wt ;

iii) the content of ethylene derived units fulfills the following equation (I);

C2<C6*0.65 (I);

Preferably the equation (I) is C2<C6*0.55; more preferably C2<C6*0.50; even more preferably C2<C6*0.40;

wherein C2 are the ethylene derived units and C6 are the 1-hexene derived units;

iv) the melt flow rate ,MFR measured according to ISO 1133 ,230° C, 2.16 kg ranges from 15 to 80 g/10 min; preferably from 20 to 50 g/ 10 min; more preferably from 25 to 45 g/10 min.

The terpolymer contains only propylene, ethylene and 1-hexene, the sum of these three comonomers derived units content being 100 wt . In order to achieve the MFR of the terpolymer it is also possible to visbreak a polymer having a lower MFR. In order to visbreak the polymer known visbreaking agent can be used such as peroxides. With the visbreaking it is possible to fine tune the MFR of the product.

The terpolymers have a stereoregularity of isotactic type of the propylenic sequences this is clear by the low value of xylene extractables that is lower than 15 wt%.

The containers object of the present invention are further endowed with a low level of hexane extractable that renders them particularly suitable for containing food. The hexane extractables measured according to FDA 21 77: 1520 is lower than 2 wt% ; preferably lower than 1.9 wt%; more preferably equal to or lower than 1.87 wt%.

Furthermore the container of the present invention is preferably endowed with a low value of haze. The haze is lower than 20.0% (measured on 2 mm plaque); preferably lower than

17.0%; more preferably lower than 16.0 % even more preferably lower than 15.5 %.

The containers of the present invention show preferably high values of impact properties. In a container having 0.4 mm wall thick the container impact test at 23°C shows values higher than 4.5 J; preferably higher than 5.0 J even more preferably higher than 5.2 J.

Furthermore the containers of the present invention shows preferably good values of top load. The top load of a container having 0.4 mm wall thick is higher than 200 N; preferably higher than 220 N;

The container of the present invention can be obtained with method commonly known in the art such as injection molding.

The terpolymer for the container of the present invention can be prepared by polymerisation in one or more polymerisation steps. Such polymerisation can be carried out in the presence of Ziegler-Natta catalysts. An essential component of said catalysts is a solid catalyst component comprising a titanium compound having at least one titanium- halogen bond, and an electron-donor compound, both supported on a magnesium halide in active form. Another essential component (co-catalyst) is an organo aluminium compound, such as an aluminium alkyl compound.

An external donor is optionally added.

The catalysts generally used in the process of the invention are capable of producing polypropylene with a value of xylene insolubility at ambient temperature greater than 90%, preferably greater than 95%. Catalysts having the above mentioned characteristics are well known in the patent literature; particularly advantageous are the catalysts described in US patent 4,399,054 and European patent 45977. Other examples can be found in US patent 4,472,524.

The solid catalyst components used in said catalysts comprise, as electron-donors (internal donors), compounds selected from the group consisting of ethers, ketones, lactones, compounds containing N, P and/or S atoms, and esters of mono- and dicarboxylic acids. Particularly suitable electron-donor compounds are esters of phtalic acid and 1,3-diethers of formula:

R!-O— CH ₂ CH ₂ O-R ^IV

wherein R ¹ and R ¹¹ are the same or different and are C C^ alkyl, C ₃ -C ₁₈ cycloalkyl or C ₇ - Ci ₈ aryl radicals; R ^m and R ^IV are the same or different and are CrC ₄ alkyl radicals; or are the 1,3-diethers in which the carbon atom in position 2 belongs to a cyclic or polycyclic structure made up of 5, 6, or 7 carbon atoms, or of 5-n or 6-n' carbon atoms, and respectively n nitrogen atoms and n' heteroatoms selected from the group consisting of N, O, S and Si, where n is 1 or 2 and n' is 1, 2, or 3, said structure containing two or three unsaturations (cyclopolyenic structure), and optionally being condensed with other cyclic structures, or substituted with one or more substituents selected from the group consisting of linear or branched alkyl radicals; cycloalkyl, aryl, aralkyl, alkaryl radicals and halogens, or being condensed with other cyclic structures and substituted with one or more of the above mentioned substituents that can also be bonded to the condensed cyclic structures; one or more of the above mentioned alkyl, cycloalkyl, aryl, aralkyl, or alkaryl radicals and the condensed cyclic structures optionally containing one or more heteroatom(s) as substitutes for carbon or hydrogen atoms, or both.

Ethers of this type are described in published European patent applications 361493 and 728769. Representative examples of said diethers are 2-methyl-2-isopropyl-l,3-dimethoxypropane, 2,2-diisobutyl- 1 ,3-dimethoxypropane, 2-isopropyl-2-cyclopentyl- 1 ,3-dimethoxypropane, 2- isopropyl-2-isoamyl-l,3-dimethoxypropane, 9,9-bis (methoxymethyl) fluorene.

Other suitable electron-donor compounds are phthalic acid esters, such as diisobutyl, dioctyl, diphenyl and benzylbutyl phthalate.

It is also possible to use mixture of at least two electron donor compounds one of which being present in an amount from 30 to 90% by mol with respect to the total amount of donors and selected from succinates and the other being selected from 1,3 diethers.

The preparation of the above mentioned catalyst component is carried out according to various methods.

For example, a MgCl ₂ -nROH adduct (in particular in the form of spheroidal particles) wherein n is generally from 1 to 3 and ROH is ethanol, butanol or isobutanol, is reacted with an excess of TiCl ₄ containing the electron-donor compound. The reaction temperature is generally from 80 to 120° C. The solid is then isolated and reacted once more with TiCl ₄ , in the presence or absence of the electron-donor compound, after which it is separated and washed with aliquots of a hydrocarbon until all chlorine ions have disappeared.

In the solid catalyst component the titanium compound, expressed as Ti, is generally present in an amount from 0.5 to 10% by weight. The quantity of electron-donor compound which remains fixed on the solid catalyst component generally is 5 to 20% by moles with respect to the magnesium dihalide.

The titanium compounds, which can be used for the preparation of the solid catalyst component, are the halides and the halogen alcoholates of titanium. Titanium tetrachloride is the preferred compound.

The reactions described above result in the formation of a magnesium halide in active form. Other reactions are known in the literature, which cause the formation of magnesium halide in active form starting from magnesium compounds other than halides, such as magnesium carboxylates.

The Al-alkyl compounds used as co-catalysts comprise the Al-trialkyls, such as Al-triethyl, Al-triisobutyl, Al-tri-n-butyl, and linear or cyclic Al-alkyl compounds containing two or more Al atoms bonded to each other by way of O or N atoms, or S0 ₄ or S0 ₃ groups.

The Al-alkyl compound is generally used in such a quantity that the Al/Ti ratio be from 1 to 1000. The electron-donor compounds that can be used as external donors include aromatic acid esters such as alkyl benzoates, and in particular silicon compounds containing at least one Si-OR bond, where R is a hydrocarbon radical.

Examples of silicon compounds are (tert-butyl) ₂ Si(OCH ₃ ) ₂ , (cyclohexyl)(methyl)Si (OCH ₃ ) ₂ , (cyclopentyl) ₂ Si(OCH ₃ ) ₂ and (phenyl) ₂ Si(OCH ₃ ) ₂ and (1,1,2- trimethylpropyl)Si(OCH ₃ ) ₃ .

1,3-diethers having the formulae described above can also be used advantageously. If the internal donor is one of these diethers, the external donors can be omitted.

In particular, even if many other combinations of the previously said catalyst components may allow to obtain propylene polymer compositions according to the present invention, the terpolymers are preferably prepared by using catalysts containing a phthalate as internal donor and (cyclopentyl) ₂ Si(OCH ₃ ) ₂ as outside donor, or the said 1,3-diethers as internal donors.

The said propylene-ethylene-hexene-1 polymers are produced with a polymerization process illustrated in EP application 1 012 195.

In detail, the said process comprises feeding the monomers to said polymerisation zones in the presence of catalyst under reaction conditions and collecting the polymer product from the said polymerisation zones. In the said process the growing polymer particles flow upward through one (first) of the said polymerisation zones (riser) under fast fluidisation conditions, leave the said riser and enter another (second) polymerisation zone (downcomer) through which they flow downward in a densified form under the action of gravity, leave the said downcomer and are reintroduced into the riser, thus establishing a circulation of polymer between the riser and the downcomer.

In the downcomer high values of density of the solid are reached, which approach the bulk density of the polymer. A positive gain in pressure can thus be obtained along the direction of flow, so that it become to possible to reintroduce the polymer into the riser without the help of special mechanical means. In this way, a "loop" circulation is set up, which is defined by the balance of pressures between the two polymerisation zones and by the head loss introduced into the system.

Generally, the condition of fast fluidization in the riser is established by feeding a gas mixture comprising the relevant monomers to the said riser. It is preferable that the feeding of the gas mixture is effected below the point of reintroduction of the polymer into the said riser by the use, where appropriate, of gas distributor means. The velocity of transport gas into the riser is higher than the transport velocity under the operating conditions, preferably from 2 to 15 m/s.

Generally, the polymer and the gaseous mixture leaving the riser are conveyed to a solid/gas separation zone. The solid/gas separation can be effected by using conventional separation means. From the separation zone, the polymer enters the downcomer. The gaseous mixture leaving the separation zone is compressed, cooled and transferred, if appropriate with the addition of make-up monomers and/or molecular weight regulators, to the riser. The transfer can be effected by means of a recycle line for the gaseous mixture. The control of the polymer circulating between the two polymerisation zones can be effected by metering the amount of polymer leaving the downcomer using means suitable for controlling the flow of solids, such as mechanical valves.

The operating parameters, such as the temperature, are those that are usual in olefin polymerisation process, for example between 50 to 120° C.

This first stage process can be carried out under operating pressures of between 0.5 and 10 MPa, preferably between 1.5 to 6 MPa.

Advantageously, one or more inert gases are maintained in the polymerisation zones, in such quantities that the sum of the partial pressure of the inert gases is preferably between 5 and 80% of the total pressure of the gases. The inert gas can be nitrogen or propane, for example.

The various catalysts are fed up to the riser at any point of the said riser. However, they can also be fed at any point of the downcomer. The catalyst can be in any physical state, therefore catalysts in either solid or liquid state can be used.

Conventional additives, fillers and pigments, commonly used in olefin polymers, may be added, such as nucleating agents, extension oils, mineral fillers, and other organic and inorganic pigments. In particular, the addition of inorganic fillers, such as talc, calcium carbonate and mineral fillers, also brings about an improvement to some mechanical properties, such as flexural modulus and HDT. Talc can also have a nucleating effect.

The nucleating agents are added to the compositions of the present invention in quantities ranging from 0.05 to 2% by weight, more preferably from 0.1 to 1% by weight, with respect to the total weight. The container, object of the present invention can have various shapes, such as cubic, conic, or irregular shapes.

The particulars are given in the following examples, which are given to illustrate, without limiting, the present invention.

Examples

Characterization methods

Melting temperature and crystallization temperature:

Determined by differential scanning calorimetry (DSC), weighting 6 ±1 mg, is heated to 220 ±1° C at a rate of 20 °C/min and kept at 220 ±1° C for 2 minutes in nitrogen stream and it is thereafter cooled at a rate of 20° C/min to 40 ±2° C, thereby kept at this temperature for 2 min to crystallise the sample. Then, the sample is again fused at a temperature rise rate of 20° C/min up to 220° C ±1. The melting scan is recorded, a thermogram is obtained, and, from this, melting temperatures and crystallization temperatures are read.

Melt Flow Rate

Determined according to the method ISO 1133 (230° C, 5 kg).

Solubility in xylene:

2.5 g of polymer and 250 ml of xylene are introduced in a glass flask equipped with a refrigerator and a magnetical stirrer. The temperature is raised in 30 minutes up to the boiling point of the solvent. The so obtained clear solution is then kept under reflux and stirring for further 30 minutes. The closed flask is then kept for 30 minutes in a bath of ice and water and in thermostatic water bath at 25° C for 30 minutes as well. The so formed solid is filtered on quick filtering paper. 100 ml of the filtered liquid is poured in a previously weighed aluminium container, which is heated on a heating plate under nitrogen flow, to remove the solvent by evaporation. The container is then kept on an oven at 80° C under vacuum until constant weight is obtained. The weight percentage of polymer soluble in xylene at room temperature is then calculated.

1-hexene and ethylene content:

Determined by 13 C-NMR spectroscopy in terpolymers: NMR analysis. 13 C NMR spectra are acquired on an AV-600 spectrometer operating at 150.91 MHz in the Fourier transform mode at 120 °C. The peak of the propylene CH was used as internal reference at 28.83. The 13 C NMR spectrum is acquired using the following parameters:

Spectral width (SW) 60 ppm

Spectrum centre (01) 30 ppm

Decoupling sequence WALTZ 65_64pl

Pulse program ⁽¹⁾ ZGPG

Pulse Length (PI) ⁽²⁾ ^ for 90°

Total number of points (TD) 32K

Relaxation Delay ⁽²⁾ 15 s

Number of transients ⁽³⁾ 1500

The total amount of 1-hexene and ethylene as molar percent is calculated from diad using the following relations:

[P] = PP + 0.5PH + 0.5PE

[H] = HH + 0.5PH

[E] = EE+ 0.5PE

Assignments of the C NMR spectrum of propylene/ 1-hexene/ethylene copolymers have been calculated according to the following table:

Haze (on 2 mm plaque):

According to the method used, 5x5 cm specimens are cut molded plaques of 2 mm thick and the haze value is measured using a a Gardner photometer with Haze-meter UX-10 equipped with a G.E. 1209 lamp and filter C. The instrument calibration is made by carrying out a measurement in the absence of the sample (0% Haze) and a measurement with intercepted light beam (100% Haze).

The measurement and computation principle are given in the norm ASTM-D1003. The plaques to be tested are produced according to the following method. 75x75x2 mm plaques are molded with a GBF Plastiniector G235/90 Injection Molding Machine, 90 tons under the following processing conditions:

Screw rotation speed: 120 rpm

Back pressure: 10 bar

Melt temperature: 260°C

Injection time: 5 sec

Switch to hold pressure: 50 bar

First stage hold pressure: 30 bar

Second stage pressure: 20 bar

Hold pressure profile: First stage 5 sec

Second stage 10 sec

Cooling time: 20 sec

Mold water temperature: 40°C

The plaques are conditioned for 12 to 48 hours at relative humidity of 50% and temperature of 23° C.

Haze on container:

The haze on container have been measured by cutting a 5x5 cm specimens from the container wall and using the same above procedure for the haze (on 2 mm plaque).

Top Load:

After at least 70 -hours conditioning at 23°C and 50% relative humidity, the bottle is settled between the two plates of the dynamometer and compressed with a stress velocity of the plate of lOmm/min.

The stress at collapse of the container is recorded and the value reported in N. The Top Load value is the mean value obtained from measurements repeated on 6 containers.

Container impact test (CIT)

The test is a biaxial impact test, the container, bottom up, was put on a sample older, having the same dimension of the container

The plate for the impact has a diameter of 62 mm and 5 kg of weight, it falls from 600 mm. The results are expressed in Joule. The results are an average of 10 tests. Containers to be tested are produced with an injection moulding machine with the following specs:

Injection moulding unit parameters:

Injection screw stroke: 1200 kN

Screw diameter: 32 mm

Injected volume: 102.9 cm3

Screw ratio L/D: 20

Max injection press: 2151 bar

The items to be tested must have the listed characteristics

Volume: 250 cc

Surface treatment: Polished

The shape of the container is a truncated pyramid with a square base, wherein the top base has a side of 70 mm and the bottom base has a side of 50 mm, the height being 80 mm IZOD Impact Strength:

Determined according to ISO 180/1 A. Samples have been obtained according to ISO 294-2. Example 1 and comparative examples 2,3 and 4

Terpolymers are prepared by polymerising propylene, ethylene and hexene- 1 in the presence of a catalyst under continuous conditions in a plant comprising a polymerisation apparatus as described in EP 1 012 195.

The catalyst is sent to the polymerisation apparatus that comprises two interconnected cylindrical reactors, riser and downcomer. Fast fluidisation conditions are established in the riser by recycling gas from the gas-solid separator. In examples 1-4 no barrier feed has been used.

The catalyst employed comprises a catalyst component prepared by analogy with example 5 of EP-A-728 769 but using micro spheroidal MgC12 ^« 1.7C2H50H instead of

MgC12 ^» 2.1C2H50H. Such catalyst component is used with dicyclopentyl dimethoxy silane (DCPMS) as external donor and with triethylaluminium (TEA).

The polymer particles exiting the reactor are subjected to a steam treatment to remove the reactive monomers and volatile substances and then dried. The main operative conditions and characteristics of the produced polymers are indicated in Table 1. Table 1 - Polymerization Process

C ₂ ^" = ethylene C ₃ ^~ = propylene C ₆ = 1-hexene

The polymer particles of examples 1-4 are introduced in an extruder, wherein they are mixed with 500 ppm of Irganox 1010 and 1000 ppm of Irgafos 168 and 500 ppm of Ca stearate, 1000 ppm of GMS 90 and 1800 ppm of MiUad 3988. The polymer particles are extruded under nitrogen atmosphere in a twin screw extruder, at a rotation speed of 250 rpm and a melt temperature of 200-250° C.

Properties of the obtained material have been reported in table 2:

Table 2

The polymer obtained have been moulded in containers as above described. The containers have been analysed, the results are reported on table 3.

Table 3

From table 3 clearly results that the container according to the present invention shows improved container Impact Test, keeping a good value of Top Load. This effect is not predictable from the raw material, in fact in table 2 the Izod impact values for the example of the present invention are the lower.