Patent Application
20070276095
The present invention relates to a multistep process for preparing heterophasic propylene copolymers, by using a particular class of metallocene compounds.
Multistep processes for the polymerization of olefins, carried out in two or more reactors, are known from the patent literature and are of particular interest in industrial practice. The possibility of independently varying, in any reactors, process parameters such as temperature, pressure, type and concentration of monomers, concentration of hydrogen or other molecular weight regulator, provides much greater flexibility in controlling the composition and properties of the end product compared to single-step processes. Multistep processes are generally carried out using the same catalyst in the various steps/reactors. The product obtained in one reactor is discharged and sent directly to the next step/reactor without altering the nature of the catalyst.
U.S. Pat. No. 5,854,354 discloses a multistep process in which a propylene polymer is prepared in step a) followed by an ethylene (co)polymer prepared in step b). In the Examples the metallocene-based catalyst system is not supported on a carrier but only prepolymerized. Therefore there is no control on the morphology of the obtained polymer.
U.S. Pat. No. 5,753,773 discloses a multiphase block copolymer of propylene obtained by carrying out the polymerization in different stages without changing the catalyst system by changing the stage. The catalyst system comprises a metallocene compound supported on silica.
WO 01/48034 discloses in some examples a multistep process in which in the first step a propylene polymer is obtained and then, in the second step an ethylene/propylene polymer is produced. In all the examples of this document the metallocene-based catalysts are supported on silica.
A drawback of these processes is that the resulting polymers are often very sticky or in any case they have a poor flowability. Flowability can be measured according to a test reported in the examples that quantifies with a numerical scale (1-8) the tendency of the polymer particles to adhere to each other.
Thus it is desirable to have a process that permits to obtain heterophasic propylene polymer characterized by low values of flowability, so that to avoid fouling in the reactor and improve the processability of the obtained reactor blend.
This problem has been solved by the present invention by carrying out the whole process by using a metallocene-base catalyst system supported on a porous organic polymer.
An object of the present invention is a multistage process comprising the following steps:
The compound of formula (1) is preferably in the racemic or racemic-like form. “Racemic-like” means that the benzo or thiophene moieties of the two n-ligands on the metallocene compound of formula (I) are on the opposite sides with respect to the plane containing the zirconium and the centre of the cyclopentadienyl moieties as shown in the following compound.
One preferred class of compounds of formula (I) is that wherein R5, R6 R8 and R9, are hydrogen atoms and R7 is a group of formula —C(R14)3 wherein R14, equal to or different from each other, are a linear or branched, saturated or unsaturated C1-C10-alkyl, C3-C10-cycloalkyl, C6-C10-aryl, C7-C10-alkylaryl, or C7-C10-arylalkyl radicals, optionally containing one or more heteroatoms belonging to groups 13-17 of the Periodic Table of the Elements; preferably R14 are linear C1-C10-alkyl radicals; more preferably they are methyl, or ethyl radicals.
A further preferred class of compounds of formula (I) is that wherein both T groups have formula (IIIb) and R5, R6, R7, R8 and R9 have the meaning described above. Preferably in one T group, R12 is a C1-C20 alkyl radical; preferably a C1-C10 alkyl radical; more preferably a methyl or ethyl group and in the other T group R12 being hydrogen.
A further preferred class of compounds of formula (1) is that wherein one T group has formula (IIIa) and the other one has formula (IIIb) and R5, R6, R7, R8 and R9 have the meaning described above.
A still further preferred class of compounds of formula (I) is that wherein both T groups have formula (IIIb), R5, R6, R7, R8 and R9 have the meaning described above and R11, R12 and R13 are hydrogen atoms
Compounds of formula (I) are known in the art, for example they can be prepared according to the disclosure of WO 01/48034, PCT/EP02/13552 and DE 10324541.3
The porous polymer supports that can be used for the process of the present invention are porous polymers such as styrene/divinylbenzene copolymers, polyamides, or porous alpha-olefin polymers.
Preferably porous alpha-olefin polymers are used, such as polyethylene, polypropylene, polybutene, copolymers of propylene and copolymers of ethylene.
Two particularly suitable classes of porous alpha-olefin polymers are those obtained according to WO 01/46272 and WO 02/051887 particularly good results are obtained when the catalyst described WO 01/46272 is used with the process described in WO 02/051887. Polymers obtained according to WO 01/46272 have a high content of the so-called stereoblocks, i.e. of polymer fractions which, although predominantly isotactic, contain a not negligible amount of non-isotactic sequences of propylene units. In the conventional fractionation techniques such as the TREF (Temperature Rising Elution Temperature) those fractions are eluted at temperatures lower than those necessary for the more isotactic fractions. The polymers obtained according to the process described in WO 02/051887 show improved porosity.
The organic porous polymer has preferably porosity due to pores with diameter up 10 μm (100000 Å) measured to the method reported below, higher than 0.1 cc/g preferably comprised between 0.2 cc/g to 2 cc/g; more preferably from 0.3 cc/g to 1 cc/g.
Preferably in the organic porous polymer fit as support according to the process of the present invention, the total porosity due to all pores whose diameter is comprised between 0.1 μm (1000 Å) and 2 μm (20000 Å) is at least 30% of the total porosity due to all pores whose diameter is comprised between 0.02 μm (200 Å) and 10 μm (100000 Å). Preferably the total porosity due to all pores whose diameter is comprised between 0.1 μm (1000 Å) and 2 μm (20000 Å) is at least 40% of the total porosity due to all pores whose diameter is comprised between 0.02 μm (200 Å) and 10 μm (100000 Å). More preferably the total porosity due all pores whose diameter is comprised between 0.1 μm (1000 Å) and 2 μm (20000 Å) is at least 50% of the total porosity due all pores whose diameter is comprised between 0.02 μm (200 Å) and 10 μm (100000 Å).
The catalyst system supported on a porous organic polymer support used in the process of the present invention, can be obtained depositing the metallocene compound i) or the product of the reaction thereof with the component ii), or the component ii) and then the metallocene compound i) on the porous polymer support. The supportation process is carried out in an inert solvent such as hydrocarbon for example toluene, hexane, pentane or propane and at a temperature ranging from 0° C. to 100° C., preferably the process is carried out at a temperature ranging from 25° C. to 90° C. A preferred supportation process is described in WO 01/44319.
A particularly suitable process for supporting the catalyst system is described in W001/44319, wherein the process comprises the steps of:
Alumoxanes used as component ii) can be obtained by reacting water with an organo-aluminium compound of formula HjAlU3-j or HjAl2U6-j, where U substituents, same or different, are hydrogen atoms, halogen atoms, C1-C20-alkyl, C3-C20-cyclalkyl, C6-C20-aryl, C7-C20-alkylaryl or or C7-C20-arylalkyl radical, optionally containing silicon or germanium atoms with the proviso that at least one U is different from halogen, and j ranges from 0 to 1, being also a non-integer number. In this reaction the molar ratio of Al/water is preferably comprised between 1:1 and 100:1. The molar ratio between aluminium and the metal of the metallocene generally is comprised between about 10:1 and about 20000:1, and more preferably between about 100:1 and about 5000:1.
The alumoxanes used in the catalyst according to the invention are considered to be linear, branched or cyclic compounds containing at least one group of the type:
wherein the substituents U, same or different, are defined above.
In particular, alumoxanes of the formula:
can be used in the case of linear compounds, wherein n1 is 0 or an integer of from 1 to 40 and the substituents U are defined as above; or alumoxanes of the formula:
can be used in the case of cyclic compounds, wherein n2is an integer from 2 to 40 and the U substituents are defined as above.
Examples of alumoxanes suitable for use according to the present invention are methylalumoxane (MAO), tetra-(isobutyl)alumoxane (TIBAO), tetra-(2,4,4-trimethyl-pentyl)alumoxane (TIOAO), tetra-(2,3-dimethylbutyl)alumoxane (TDMBAO) and tetra-(2,3,3-trimethylbutyl)alumoxane (TTMBAO).
Particularly interesting cocatalysts are those described in WO 99/21899 and in WO01/21674 in which the alkyl and aryl groups have specific branched patterns.
Non-limiting examples of aluminium compounds that can be reacted with water to give suitable alumoxanes (b), described in WO 99/21899 and WO01/21674, are: tris(2,3,3-trimethyl-butyl)aluminium, tris(2,3-dimethyl-hexyl)aluminium, tris(2,3-dimethyl-butyl)aluminium, tris(2,3-dimethyl-pentyl)aluminium, tris(2,3-dimethyl-heptyl)aluminium, tris(2-methyl-3-ethyl-pentyl)aluminium, tris(2-methyl-3-ethyl-hexyl)aluminium, tris(2-methyl-3-ethyl-heptyl)aluminium, tris(2-methyl-3-propyl-hexyl)aluminium, tris(2-ethyl-3-methyl-butyl)aluminium, tris(2-ethyl-3-methyl-pentyl)aluminium, tris(2,3-diethyl-pentyl)aluminium, tris(2-propyl-3-methyl-butyl)aluminium, tris(2-isopropyl-3-methyl-butyl)aluminium, tris(2-isobutyl-3-methyl-pentyl)aluminium, tris(2,3,3-trimethyl-pentyl)aluminium, tris(2,3,3-trimethyl-hexyl)aluminium, tris(2-ethyl-3,3-methyl-butyl)aluminium, tris(2-ethyl-3,3-dimethyl-pentyl)aluminium, tris(2-isopropyl-3,3-dimethyl-butyl)aluminium, tris(2-trimethylsilyl-propyl)aluminium, tris(2-methyl-3-phenyl-butyl)aluminium, tris(2-ethyl-3-phenyl-butyl)aluminium, tris(2,3-dimethyl-3-phenyl-butyl)aluminium, tris(2-phenyl-propyl)aluminium, tris[2-(4-fluoro-phenyl)-propyl]aluminium, tris[2-(4-chloro-phenyl)-propyl]aluminium, tris[2-(3-isopropyl-phenyl)-propyl]aluminium, tris(2-phenyl-butyl)aluminium, tris(3-methyl-2-phenyl-butyl)aluminium, tris(2-phenyl-pentyl)aluminium, tris[2-(pentafluorophenyl)-propyl]aluminium, tris[2,2-diphenyl-ethyl]aluminium and tris[2-phenyl-2-methyl-propyl]aluminium, as well as the corresponding compounds wherein one of the hydrocarbyl groups is replaced with a hydrogen atom, and those wherein one or two of the hydrocarbyl groups are replaced with an isobutyl group.
Amongst the above aluminium compounds, trimethylaluminium (TMA), triisobutylaluminium (TIBA), tris(2,4,4-trimethyl-pentyl)aluminium (TIOA), tris(2,3-dimethylbutyl)aluminium (TDMBA) and tris(2,3,3-trimethylbutyl)aluminium (TTMBA) are preferred.
Non-limiting examples of compounds able to form an alkylmetallocene cation are compounds of formula D+E−, wherein D+ is a Brøonsted acid, able to donate a proton and to react irreversibly with a substituent X of the metallocene of formula (I) and E is a compatible anion, which is able to stabilize the active catalytic species originating from the reaction of the two compounds, and which is sufficiently labile to be removed by an olefinic monomer. Preferably, the anion E comprises one or more boron atoms. More preferably, the anion F is an anion of the formula BAr4(−), wherein the substituents Ar which can be identical or different are aryl radicals such as phenyl, pentafluorophenyl or bis(trifluoromethyl)phenyl. Tetrakis-pentafluorophenyl borate is particularly preferred compound, as described in WO 91/02012. Moreover, compounds of formula BAr3 can be conveniently used. Compounds of this type are described, for example, in the International patent application WO 92/00333. Other examples of compounds able to form an alkylmetallocene cation are compounds of formula BAr3P wherein P is a substituted or unsubstituted pyrrol radical. These compounds are described in WO01/62764. Compounds containing boron atoms can be conveniently supported according to the description of DE-A-19962814 and DE-A-19962910. All these compounds containing boron atoms can be used in a molar ratio between boron and the metal of the metallocene comprised between about 1:1 and about 10:1; preferably 1:1 and 2.1; more preferably about 1:1.
Non limiting examples of compounds of formula D+E− are:
Organic aluminum compounds used as compound iii) are those of formula HjAlU3-j or HjAl2U6-j as described above.
Preferably step a) further comprises a prepolymerization step a-1).
The prepolymerization step a-1) can be carried out by contacting the catalyst system supported on the porous organic support with one ore more alpha olefins of formula CH2═CHT3 wherein T3 is hydrogen or a C1-C20 alkyl radical; preferably said alpha olefin is propylene or ethylene, at a temperature ranging from −20° C. to 70° C., in order to obtain a prepolymerized catalyst system containing preferably from 5 to 500 g of polymer per gram of catalyst system.
Thus preferably step a) comprises
a-1) contacting the catalyst system described above with ethylene and/or propylene and/or one ore more alpha olefins of formula CH2═CHT1, wherein T1 is a C2-C20 alkyl radical; preferably propylene or ethylene in order to obtain a prepolymerized catalyst system preferably containing from 5 to 500 g of polymer per gram of catalyst system;
Step a) of the present invention can be carried out in liquid phase, in which the polymerization medium can be an inert hydrocarbon solvent or the polymerization medium can be liquid propylene optionally in the presence of an inert hydrocarbon solvent, and of one or more comonomer of formula CH2═CHT1, or step a) can be carried out in a gas phase. Said hydrocarbon solvent can be either aromatic (such as toluene) or aliphatic (such as propane, hexane, heptane, isobutane, cyclohexane and 2,2,4-trimethylpentane).
Preferably the polymerization medium is liquid propylene. It can optionally contains minor amounts (up to 20% by weight, preferably up to 10% by weight, more preferably up to 5% by weight) of an inert hydrocarbon solvent or of one or more comonomer of formula CH2═CHT1.
Step a) can be carried out in the presence of hydrogen. The amount of hydrogen present during the polymerization reaction is preferably more than 1 ppm; more preferably from 5 to 2000 ppm; even more preferably from 6 to 500 ppm with respect to the propylene present in the reactor. Hydrogen can be added either at the beginning of the polymerization reaction or it can also be added at a later stage after a prepolymerization step has been carried out.
The propylene polymer obtained in step a) is a propylene homopolymer or a propylene copolymer containing up to 20% by mol preferably from 0.1 to 10% by mol, more preferably from 1% to 5% by mol of derived units of one or more alpha olefins of formula CH2═CHT1. Non-limiting examples of alpha olefins of formula CH2═CHT1 which can be used in the process of the invention are ethylene, 1-butene, 1-pentene, 4-methyl-1 -pentene, 1-hexene, 1-octene, 4,6-dimethyl-1-heptene, 1-decene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1-octadecene and 1-eicosene. Preferred comonomers are ethylene or 1-butene. Preferably in step a) a propylene homopolymer is produced.
The content of the polymer obtained in step a) ranges from 5% to 90% by weight of the polymer produced in the whole process, preferably it ranges from 10% to 70% by weight more preferably from 15% to 50% by weight of the total polymer produced in the whole process.
Step b) is carried out in a gas phase, preferably in a fluidized bed reactor. The polymerization temperature is generally comprised between −100° C. and +200° C., and, preferably, between 10° C. and +90° C. The polymerization pressure is generally comprised between 0.5 and 100 bar.
In step b) an ethylene copolymer containing from 5% to 90% by mol, preferably from 10% to 50% by mol, more preferably from 15% to 30% by mol of derived units of one or more alpha olefins of formula CH2═CHT2 is produced. Examples of comonomer of formula CH2═CHT2 that can be used in step b) of the present invention are: propylene, 1-butene, 1-pentene, 4-methyl-1-pentene, 1-hexene, 1-octene, 4,6-dimethyl-1-heptene, 1-decene, 1-dodecene, 1-tetradecene, 1-hexadecene, 1-octadecene and 1-eicosene. Preferred comonomers are propylene or 1-butene.
The content of polymer obtained in step b) preferably ranges from 10 to 95% by weight of the polymer produced in the whole process, preferably it ranges from 30% to 90% by weight and more preferably from 50% to 85% by weight.
The polymer obtained in step b) can optionally contains up to 20% by mol of a non conjugated diene. Non conjugated dienes can be a straight chain, branched chain or cyclic hydrocarbon diene having from 6 to 20 carbon atoms. Examples of suitable non-conjugated dienes are:
Preferred dienes are 1,4-hexadiene (HD), 5-ethylidene-2-norbornene (ENB), 5-vinylidene-2-norbornene (VNB), 5-methylene-2-norbornene (MNB) and dicyclopentadiene (DCPD). Particularly preferred dienes are 5-ethylidene-2-norbornene (ENB) and 1,4-hexadiene (HD).
When present the non-conjugated dienes are preferably incorporated into the polymer in an amount from 0.1% to about 20% by mol, preferably from 0.5% to 15% by mol, and more preferably from 0.5% to 7% by mol. If desired, more than one diene may be incorporated simultaneously, for example HD and ENB, with total diene incorporation within the limits specified above.
The process of the present invention can be carried out in one reactor or in two or more reactor in series.
In particular with the process of the present application heterophasic propylene polymers having excellent flowability and in high yields can be obtained. Flowability can be measured according to the procedure reported below. This test gives a numeric value that measures the flowability index of the polymer.
Thus a further object of the present invention is a propylene polymer compositions obtainable according to the process of the present invention comprising:
said propylene polymer or copolymer having isotactic pentads (mmmm) higher than 90%, preferably higher than 95% more preferably higher than 97%;
Preferably compound a) has a distribution of molecular weight Mw/Mn lower than 4; preferably lower than 3; more preferably lower than 2.5.
Preferably compound b) has a distribution of molecular weight Mw/Mn lower than 4; preferably lower than 3; more preferably lower than 2.5.
The ethylene copolymer b) can further optionally contains up to 20% by mol of derived units of a non conjugated diene, preferably in an amount from 0.1% to about 20% by mol; more preferably from 0.5% to 15% by mol, and still more preferably from 0.5% to 7% by mol.
Preferred monomers to be copolymerized with ethylene in step b) are propylene and 1-butene.
The following examples are given to illustrate and not to limit the invention.
General Characterization
Determination of X.S.
2.5 g of polymer were dissolved in 250 ml of o-xylene under stirring at 135° C. for 30 minutes, then the solution was cooled to 25° C. and after 30 minutes the insoluble polymer was filtered. The resulting solution was evaporated in nitrogen flow and the residue was dried and weighed to determine the percentage of soluble polymer (XS) and then, by difference, the insolubles (X.I.).
NMR
The proton and carbon spectra of polymers were obtained using a Bruker DPX 400 spectrometer operating in the Fourier transform mode at 120° C. at 400.13 MHz and 100.61 MHz respectively. The samples were dissolved in C2D2Cl4. As reference the residual peak of C2DHCl4 in the 1H spectra (5.95 ppm) and the peak of the mmmm pentad in the 13C spectra (21.8 ppm) were used. Proton spectra were acquired with a 45° pulse and 5 seconds of delay between pulses; 256 transients were stored for each spectrum. The carbon spectra were acquired with a 90° pulse and 12 seconds (15 seconds for ethylene based polymers) of delay between pulses and CPD (waltz 16) to remove 1H-13C couplings. About 3000 transients were stored for each spectrum.
The intrinsic viscosity (I.V.) was measured in tetrahydronaphtalene (THN) at 135° C.
Metallocene Compounds
rac-dimethylsilanediyl(2-methyl-4-(4′-tert-butylphenyl)indenyl)(2-isopropyl-4-(4′-tetr-butylphenyl)indenyl)zirconium dichloride (A-1) was prepared according to the procedure described in WO 01/48034
rac-dimethylsilanediyl(2,6-dimethyl-4-(4′-tert-butylphenyl)indenyl)(2-isopropyl-4-(4′-tetr-butylphenyl)indenyl)zirconium dichloride (A-2) ) was prepared according to the procedure described in DE 10324541.3
{Me2Si (4-(4-tert-Butyl-phenyl)-2-isopropyl-inden-1-yl)(2,5-dimethyl-3-phenyl-cyclopento[2,3-b]thiophen-6-yl)}ZrCl2 (A-3) was prepared according to the procedure described in PCT/EP02/13552
{Me2Si (4-(4-tert-Butyl-phenyl)-2-isopropyl-inden-1-yl)(2,5-dimethyl-3-(4-tert-butyl-phenyl)-cyclopento[2,3-b]thiophen-6-yl)}ZrCl2. (A-4) was prepared according to the procedure described in PCT/EP02/13552.
Porous Organic Polymer Supports
Polypropylene prepolymer (support A) was produced according to the procedure described in the example I of WO 00/08065, under the following conditions: polymerisation temperature 20° C., AliBu3 (AliBu3/ZN catalyst=1 (w/w)), propylene flow=1 kg/h for 2 h, then 5 kg/h for 6 h (conversion 40 gPP/gcat). Characterization data of the polymer are reported in table 1
Polyethylene prepolymer (support B) was produced according to the procedure described in example 1 of WO 95/26369, under the following conditions: polymerisation temperature 0° C., AliBu3 (AliBu3/ZN catalyst=1 (w/w)), 1.5 bar-g of ethylene (conversion of 40 gPE/gcat). Characterization data of the polymer are reported in table 1
Preparation of the Catalyst Systems
Catalyst C-1
4.6 g of support B described above, were treated with H2O dispersed in hexane in order to deactivate the MgCl2/Ti-based catalyst, then dried in a flow of nitrogen. The support is contacted with 0.5mL of MAO solution (30% w in toluene) diluited with 1.5 ml of toluene to scavenge impurities and residual water.
The catalytic complex was prepared by adding 42 mg of metallocene (A-4) in 4.1 ml of MAO solution (30% w/w in toluene).
The so obtained catalytic mixture is impregnated on support A (treated as described above) according to procedure described in WO 01/44319.
The obtained supported catalytic system contains 9.5% w of Aluminium and 910 ppm of Zirconium measured via Ion Coupled Plasma.
Catalyst C-2
3.7 g of support B described above, were treated with H2O dispersed in hexane in order to deactivate the MgCl2/Ti-based catalyst, then dried in a flow of nitrogen. The support is contacted with 0.4 mL of MAO solution (30% w in toluene) diluited with 1.6 ml of toluene to scavenge impurities and residual water.
The catalytic complex was prepared by adding 41 mg of metallocene (A-3) in 4.3 ml of MAO solution (30% w/w in toluene).
The so obtained catalytic mixture is impregnated on support B (treated as described above) according to procedure described in WO 01/44319.
The obtained supported catalytic system contains 13.4% w of Aluminium and 1030 ppm of Zirconium measured via Ion Coupled Plasma.
Catalyst C-3
5.6 g of support A described above, were treated with H2O dispersed in hexane in order to deactivate the MgCl2/Ti-based catalyst, then dried in a flow of nitrogen. The support is contacted with 0.7 mL of MAO solution (30% w in toluene) diluited with 1.3 ml of toluene to scavenge impurities and residual water.
The catalytic complex was prepared by adding 66 mg of metallocenes (A-2) in 6.6 ml of MAO solution (30% w/w in toluene).
The so obtained catalytic mixture is impregnated on support A (treated as described above) according to procedure described in WO 01/44319.
The obtained supported catalytic system contains 9.9% w of Aluminium and 0.10% w of Zirconium measured via Ion Coupled Plasma.
Catalyst C-4
5.0 g of support A described above, were treated with H2O dispersed in hexane in order to deactivate the MgCl2/Ti-based catalyst, then dried in a flow of nitrogen. The support is contacted with 0.5 mL of MAO solution (30% w in toluene) diluited with 1.5 ml of toluene to scavenge impurities and residual water.
The catalytic complex was prepared by adding 89 mg of metallocene (A-1) in 4.5 ml of MAO solution (30% w/w in toluene).
The so obtained catalytic mixture is impregnated on support A (treated as described above) according to procedure described in WO 01/44319.
The obtained supported catalytic system contains 8.9% w of Aluminium and 0.14% w of Zirconium measured via Ion Coupled Plasma.
Catalyst C-5 (Comparative)
3 kg of silica (Sylopol 948™) is loaded in a process filter whose filter plate points upward, and suspended in 15 L of toluene. While stirring 7 L of a 30% strength by weight MAO solution are metered in at such a rate that the internal temperature does not exceed 35° C. After stirring for another 1 hour at a low stirrer speed, the process filter is turned that its filtration plate points downwards, the suspension is filtered, firstly under atmospheric pressure and then using 3 bar of nitrogen pressure. In parallel to the treatment of the support material, 2.0 L of 30% strength by weight MAO solution and 92.3 g of rac-dimethylsilylbis(2-methyl-4-(para-tert-butylphenyl)-indenyl)-zirconium dichloride are placed in a reaction vessel, the solution is stirred for 1 hour and allowed to settle for a further 30 minutes. The solution is subsequently added to the pretreated support material with the outlet closed. After addition is complete, the outlet is opened and the filtrate is allowed to drain. When no more runs off, the outlet is closed, the filter cake is stirred for 15 minutes and allowed to rest for 1 hour. A nitrogen pressure of 3 bar is subsequently applied with the outlet open. 15 L of isododecane are added to the remaining solid, the mixture is stirred for 15 minutes and filtered. The washing step is repeated, and the solid is subsequently pressed dry by means of a nitrogen pressure of 3 bar. For use in the polymerization, the total amount of the catalyst is resuspended in 15 L of isododecane.
The catalyst system contains 0.16% w of Zirconium.
Catalyst C-6 (Comparative)
7.39 g of silica (XPO2107 from Grace) was dried at 180° C. for 17 hours at a pressure of 15 mbar. Metallocene compound A-1 (24 μmol) was dissolved in toluene (5 ml) and stirred for 10 minutes, then 7.8 ml of a 30% solution of metylalumoxane in toluene (MAO from Albemarle) solution was added dropwise and color changed immediately from orange to ruby-red. the obtained suspension was stirred for 1 hour and then added dropwise to 1 g of dry silica gel purified as described above. The resulting suspension was stirred until a dark pink colour was obtained. The suspension was finally dried in vacuo for 1.5 hours at 50° C. The resulting catalyst system contains 0.16 wt % of Zr, Al/Zr=209
General Procedure
All polymerization tests were carried out in a 4.250 L stainless steel Reactor, operated by a Yokogawa system, and equipped with a “ribbon” helical stirrer, with stirring rate of 300-400 RPM, a stainless steel vial for catalyst injection, and a look-through glass window.
Step a)
The reactor is purified by washing with 2L hexanes containing 5-6 mL TEA (triethylaluminum) 10% (1M), stirring 1 h at 70° C., and then discharging the solution through the bottom valve under N2 pressure. The reactor temperature is lowered to 30° C., and the reactor pressure to 0.5 bar-g. Then the scavenger (4 mL 1M TEA in hexane) is added under a stream of propylene, and 430 g of liquid propylene is added. The catalyst is added to the reactor through a stainless steel vial. For Polyethylene supported catalysts, the dry powder is loaded into the steel vial under N2 stream, injected into the reactor by N2 overpressure, then the vial rinsed with 3-4 mL of hexanes into the reactor, again with N2 overpressure. For SiO2 supported catalysts, the powder is added as a slurry in hexanes. The homopolymer is produced in liquid monomer, by first a prepolymerization at 30° C. for 5 min, then adding 100 NmL of H2, and the temperature is raised in 10 minutes at the polymerization temperature of 70° C. and this temperature is kept constant until the pressure starts decreasing and no liquid phase is observed.
Step b)
Then the reactor is vented to 0.5 bar-g, the temperature is set at 60° C. and the comonomers are fed in the ratio indicated in table 1, until a pressure of 25 bar-g is reached. The comonomers are fed at constant temperature and pressure until 500 grams are taken in, or for a total polymerization time of two hours.
The polymerization is stopped by venting the monomers. The reactor is cooled, purged with N2, opened to inspect fouling, and the polymer is collected and dried in a vacuum oven at 60° C. for 1 hour. Polymerization data and characterisation of the obtained polymers are reported in table 2.
*comparative
n.a. not available
n.a. not available
# rubber content in the composition
Flowability Test
A flowability test was designed to compare the behaviour of particles of soft and sticky materials. The degree of flowability is rated on a scale of 1 to 8. 1-2 means no clumping hence good flowability, 3 to 7 means increasing clumping hence poor flowability, 8 means a solid clump hence no flowability at all. The test procedure is the following:
Procedure:
behaviour is rated according to the rules reported in table 3. The results of the text carried out on samples of the polymers obtained in examples 1-7 are reported in table 4.
| Number | Date | Country | Kind |
|---|---|---|---|
| 03102736.0 | Sep 2003 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP04/08759 | 8/4/2004 | WO | 3/10/2006 |
| Number | Date | Country | |
|---|---|---|---|
| 60503234 | Sep 2003 | US |
