Patent Application
20090286946
The present invention relates to a process for the preparation of isotactic copolymers of propylene and at least ethylene or an alpha olefin of formula CH2═CHT wherein T is a C2-C20 alkyl radical carried out in solution. Said process being carried out by using a particular class of metallocene-based catalyst system.
Process for the copolymerization of propylene by using metallocene catalyst system are already known in the art. For example in EP 629 632 a series of solution polymerization examples are described. However this document describes a bridged bis indenyl metallocene-based catalyst system wherein the indenyl groups are substituted only in positions 2 and 4. Moreover the polymerization results can be still improved.
WO 03/050131 describes a class of bridged bis indenyl metallocene compounds wherein the indenyl moieties are substituted at least in positions 2, 4 and 5. In this document about 100 pages are used to list example of compounds included in the general formula, al these compounds are bridged bis indenyl metallocene compounds substituted in positions 2, 4 and 5. WO 03/050131 states that this class of metallocene compounds can be used for every kind of polymerization process including solution polymerizations, however all the examples are directed to slurry polymerization process.
PCT/EP2004/013827 a class of bis indenyl metallocene compounds wherein the indenyl moieties are substituted in position 5 and 6 by a condensed ring is disclosed. PCT/EP2004/013827 is mainly focused on C1 symmetric structures and there are no explicit disclosures of C2 symmetric compounds. In other words this document is focused on metallocene compounds comprising two cyclopentadienyl moieties having different substitution patterns.
Therefore there is the need to find a catalyst system able to give propylene copolymers having high molecular weight in high yields and that can be used at temperatures of industrial interest in a solution polymerization process.
An object of the present invention is a solution polymerization process comprising contacting under polymerization conditions propylene and at least ethylene or an alpha olefin of formula CH2═CHT wherein T is a C2-C20 alkyl radical, in the presence of a catalyst system obtainable by contacting:
A further preferred class of compounds of formula (I) has formula (IIa), (IIb), or (IIc):
Wherein M, L, X, R1, R4, R6, R7, R8, R9 and R10 have the meaning reported above and R11 and R12 equal to or different from each other, are hydrogen atoms or C1-C40 hydrocarbon radicals optionally containing heteroatoms belonging to groups 13-17 of the Periodic Table of the Elements; preferably R11 and R12 are hydrogen atoms or linear or branched, cyclic or acyclic, C1-C40-alkyl, C2-C40 alkenyl, C2-C40 alkynyl radicals, optionally containing heteroatoms belonging to groups 13-17 of the Periodic Table of the Elements; more preferably R11 and R12 are hydrogen atoms or C1-C10-alkyl radicals such as methyl or ethyl radicals.
Preferably the metallocene compounds of formula (I) have C2 symmetry. Metallocene symmetry classes can be found on Resconi et al. Chemical Reviews, 2000, Vol. 100, No. 4 1263 and references herein cited.
Preferably the metallocene compounds to be used in the process of the present invention are in their racemic(rac) or racemic-like form. Racemic(rac) and racemic-like form are described in PCT/EP2005/052688.
Examples of compounds having formula (I) are as follows
The process of the present invention is preferably carried out at a temperature ranging from 60° C. to 200° C., more preferably at a temperature ranging from 70° C. to 150° C., even more preferably from 80° C. to 120° C.
The alumoxanes used in the process 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 n′ 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 n2 is 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-methylbutyl)aluminium, tris(2-isopropyl-3-methylbutyl)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-dimethyl-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 r A) are preferred.
Non-limiting examples of compounds able to form an alkylmetallocene cation are compounds of formula D+E−, wherein D+ is a Brnøsted 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 E− 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 typo 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:
Additional examples of compounds of formula D−E− that can be used according to the present invention are described in WO 04/005360, WO 02/102811 and WO 01/62764.
Organic aluminum compounds used as compound c) are those of formula HjAlU3-j or HjAl2U6-j as described above.
The catalyst system of the present invention can be prepared by contacting the metallocene of formula (I) and a suitable cocatalyst, in a solvent. The cocatalyst is preferably the reaction product of methylalumoxane and triisobutylaluminum.
The catalyst of the present invention can be prepared according to PCT/EP2005/002479 both by distilling off toluene or by following the described procedure but without such a distillation.
The catalysts of the present invention can also be supported on an inert carrier. This is achieved by depositing the metallocene compound a) or the product of the reaction thereof with the component b), or the component b) and then the metallocene compound a) on an inert support. The support can be a porous solid such as talc, a sheet silicate, an inorganic oxide or a finely divided polymer powder (e.g. polyolefin). Suitable inorganic oxides may be found among the oxides of elements of groups 2, 3, 4, 5, 13, 14, 15 and 16 of the Periodic Table of the Elements. Examples of oxides preferred as supports include silicon dioxide, aluminum oxide, and also mixed oxides of the elements calcium, aluminum, silicon, magnesium or titanium and also corresponding oxide mixtures, magnesium halides, styrene/divinylbenzene copolymers, polyethylene or polypropylene. Other inorganic oxides which can be used alone or in combination with the abovementioned preferred oxidic supports are, for example, MgO, ZrO2, TiO2 or B2O3.
A suitable class of supports which can be used is that constituted by porous organic supports functionalized with groups having active hydrogen atoms. Particularly suitable are those in which the organic support is a partially crosslinked styrene polymer. Supports of this type are described in European application EP-633 272.
Another class of inert supports particularly suitable for use according to the invention is that of polyolefin porous prepolymers, particularly polyethylene.
A further suitable class of inert supports for use according to the invention is that of porous magnesium halides such as those described in International application WO 95/32995.
The support materials used preferably have a specific surface area in the range from 10 to 1 000 m2/g, a pore volume in the range from 0.1 to 5 ml/g and a mean particle size of from 1 to 500 μm. Preference is given to supports having a specific surface area in the range from 50 to 500 m2/g, a pore volume in the range from 0.5 to 3.5 ml/g and a mean particle size in the range from 5 to 350 μm. Particular preference is given to supports having a specific surface area in the range from 200 to 400 m2/g, a pore volume in the range from 0.8 to 3.0 ml/g and a mean particle size of from 10 to 300 μm.
The inorganic support can be subjected to a thermal treatment, e.g. to remove adsorbed water. Such a drying treatment is generally carried out at from 80 to 300° C., preferably from 100 to 200° C., with drying at from 100 to 200° C. preferably being carried out under reduced pressure and/or a blanket of inert gas (e.g. nitrogen), or the inorganic support can be calcined at from 200 to 1000° C. to produce the desired structure of the solid and/or set the desired OH concentration on the surface. The support can also be treated chemically using customary desiccants such as metal alkyls, preferably aluminum alkyls, chlorosilanes or SiCl4, or else methylaluminoxane. Appropriate treatment methods are described, for example, in WO 00/31090.
The inorganic support material can also be chemically modified. For example, treatment of silica gel with (NH4)2SiF6 leads to fluorination of the silica gel surface, or treatment of silica gels with silanes containing nitrogen-, fluorine- or sulfur-containing groups leads to correspondingly modified silica gel surfaces.
Organic support materials such as finely divided polyolefin powders (e.g. polyethylene, polypropylene or polystyrene) can also be used and are preferably likewise freed of adhering moisture, solvent residues or other impurities by means of appropriate purification and drying operations before use. It is also possible to use functionalized polymer supports, e.g. supports based on polystyrene, via whose functional groups, for example carboxylic or hydroxy groups, at least one of the catalyst components can be immobilized. The solid compound obtained by supporting the catalyst system object of the present invention on a carrier in combination with the further addition of the alkylaluminium compound either as such or prereacted with water if necessary.
For the purpose of the present invention the term solution polymerization means that the polymer is fully soluble in the polymerization medium at the polymerization temperature used, and in a concentration range of 5 to 50% by weight.
In order to have the polymer completely soluble in the polymerization medium, a mixtures of monomers in the presence of an inert solvent can be used. This solvent can be an aliphatic or cycloaliphatic hydrocarbon such as hexane, heptane, isooctane, isododecane, cyclohexane and methylcyclohexane. It is also possible to use mineral spirit or a hydrogenated diesel oil fraction. Also aromatic hydrocarbons can be used such as toluene. Preferred solvents to be used are cyclohexane and methylcyclohexane. The propylene content in the mixture can be varied according to the final comonomer content wished in the copolymer and the relative reactivity ratio of the comonomers. The propylene content in the liquid phase of the polymerization medium preferably ranges from 5% to 60% by weight; more preferably from 20% to 50% by weight.
The temperature range useful for the polymerization process of the present invention is comprised between 60° C. and 200° C., preferably from 80° C. to 150° C., more preferably from 89° C. to 120° C.
Hydrogen can be efficiently used to regulate the molecular weight of the obtained polymers. Preferably the concentration of hydrogen ranges from 1 ppm to 1000 ppm, preferably from 2 ppm to 300 ppm.
The ratio of the comonomers varies accordingly, depending on the wished final copolymer and the relative comonomers reactivity ratio of the catalyst system.
The skilled man is able to select the ratio of propylene and comonomer in order to obtain the whished copolymer.
The copolymers obtained according to the process of the present invention, especially those having high comonomer content, are very sticky, this makes it difficult to produce in an industrial plant when the polymerization process is carried out in slurry or in gas phase because of the fouling in the reactor. On the contrary when a solution polymerization process is carried this problem is avoided.
According to the process of the present invention propylene is contacted with at least ethylene or an alpha olefin of formula CH2═CHT wherein T is a C2-C20 alkyl radical. Examples of alpha olefin of formula CH2═CHT are 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 comonomer to be used are ethylene, 1-butene and 1-hexene.
The content of propylene derived units in the copolymers obtained according to the present invention contains up to 95% by mol of propylene derived units. Preferably the content of propylene derived units ranges from 30% by mol to 91% by mol. More preferably the content of propylene derived units ranges from 70% by mol to 91% by mol.
The molecular weight distribution can be varied by using mixtures of different metallocene compounds or by carrying out the polymerization in several stages which differ as to the polymerization temperature and/or the concentrations of the molecular weight regulators and/or the monomers concentration. Moreover by carrying out the polymerization process by using a combination of two different metallocene compounds a polymer endowed with a broad melting is produced.
The polymer obtained according to the process of the present invention can further contain 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; more preferably from 0.5% to 3% by weight. If desired, more than one diene may be incorporated simultaneously, for example HD and ENB, with total diene incorporation within the limits specified above.
Therefore a further object of the present invention is a solution polymerization process comprising contacting under polymerization conditions propylene, at least ethylene or an alpha olefin of formula CH2═CHT wherein T is a C2-C20 alkyl radical and a non conjugated diene, in the presence of a catalyst system obtainable by contacting:
The following examples are given to illustrate and not to limit the invention.
All chemicals must be handled using standard Schlenk techniques.
Methylalumoxane (MAO) was received from Albemarle as a 30% wt/wt. toluene solution and used as such.
Pure triisobutylaluminum (TIBA) was used as such.
Isododecane was purified over alumina to reach a water content below 10 ppm.
A 110 g/L TIBA/isododecane solution was obtained by mixing the above components.
I.V. Intrinsic viscosities were measured in tetrahydronaphtalene THN at 135° C.
DSC. The melting points of the polymers (Tm) were measured by Differential Scanning Calorimetry (DSC) on a Perkin Elmer DSC-7 calorimeter equipped with Pyris 1 software, in the Solid State Properties (FE-PPC) laboratory, previously calibrated at indium and zinc melting points with particular attention in determining the baseline with required accuracy. The preparation of the samples, for calorimetric investigations, has been performed by cutting them into small pieces by using a cutter. The weight of the samples in every DSC crucible was kept at 6.0±0.5 mg.
The weighted sample was sealed into aluminum pans and heated to 180° C. at 10° C./minute the temperature peak was token as Tm(I). The sample was kept at 180° C. for 5 minutes to allow a complete melting of all the crystallites, then cooled to 20° C. at 10° C./minute. After standing 2 minutes at 20° C., the sample was heated for the second time to 180° C. at 10° C./min. In this second heating run, the peak temperature was taken as the melting temperature (Tm(II)) and the area of the peak as its melting enthalpy (ΔHf).
The chemical composition and comonomer distribution of the copolymers were investigated by 13C-NMR analysis with a Bruker DPX400 spectrometer operating at 100.61 MHz. The samples were measured as 8% (w/v) solutions of 1,12,2-tetrachloroethane, the 13C-NMR spectra were recorded at 120° C. with a 90 degree pulse, 12 s of delay between pulses and CPD to remove 1H-13C coupling. About 1K of transients were stored in 32K data points using a spectral window of 6000 Hz. The Sδδ peak at 29.9 ppm (nomenclature according to reference 1) was used as internal reference. The product of reactivity ratios r1×r2 was calculated from the triads according to reference 1. The copolymer compositions and triad distributions were determined according to reference 2.
was prepared according to EP05102189.
rac-dimethylsilylbis(2-methyl-4-phenyl)-indenyl)dichlorozirconium (rac-μ-{bis-[η5-2-methyl-4-phenyl-inden-1-yl]dimethylsilanediyl}dichlorozirconium (I)) (C-1) was prepared according to U.S. Pat. No. 5,786,432
rac-dimethylsilylbis(2-methyl-4-(ara-tert-butylphenyl)indenyl)dichlorozirconium (rac-Me2Si(2-Me-4(4tBuPh)Ind)2ZrCl2) (C-2) was prepared according to WO 98/40331 (example 65).
3.6 g of silica (Sylopol 948™) is loaded in a process filter whose filter plate points upward, and suspended in 20 mL of toluene. While stirring 8.8 mL of a 30% MAO (methylalumoxane) strength 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, 118 mg of A-1 in 1.1 mL of 30% strength MAO 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 suspended in 20 ml of toluene. After addition is complete, the suspension is stirred for 15 minutes. A nitrogen pressure of 3 bar is applied in order to drain the solution. At the end the solid is dried under vacuum.
14.6 mL of TUBA/isododecane solution (110 g/L) were mixed with 3.4 mL of MAO/toluene solution (Albemarle 30% wt/wt) to obtain a MAO/TIBA molar ratio of 2:1. The solution was stirred for 30 minutes at room temperature. Then, 50 mg of A-1 were dissolved in the solution.
The orange solution did not show any trace of residual solid.
The final solution was diluted with 8 mL of toluene to reach a concentration of 100 g/L (1.92 g A-1/L).
9.5 mL of TIBA/isododecane solution (110 g/L) were mixed with 2.7 mL of MAO/toluene solution (Albemarle 30% wt/wt, 12.8 mmol MAO) to obtain a MAO/TIBA molar ratio of 2.4:1. The solution was stirred for 30 minutes at room temperature. Then, 25 mg of C-1 were dissolved in the solution. The solution did not show any trace of residual solid. The final solution was diluted with 5.1 mL of toluene to reach a concentration of 105 g/L (1.45 gmetallocene/L).
8.1 mL of TIBA/isododecane solution (110 g/L) were mixed with 1.9 mL of MAO/toluene solution (Albemarle 30% wt/wt, 9 mmol MAO) to obtain a MAO/TIBA molar ratio of 2:1. The solution was stirred for 30 minutes at room temperature. Then, 25 mg of C-2 were dissolved in the solution. The solution did not show any trace of residual solid. The final solution was diluted with 4.4 mL of toluene to reach a concentration of 100 g/L (1.74 gmetallocene/L).
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 958 g of cyclo-hexane, 45 g of ethylene and 489 g of propylene were fed into the reactor in order to obtain a liquid composition at 90° C., 22 bar-g, corresponding to a liquid composition of 7/93% wt ethylene/propylene.
1 mL of the catalyst system A-IC containing the catalyst/cocatalyst mixture (1.92 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene propylene 18/82% wt was continuously fed for 1 hour to maintain the pressure of 22 bar-g:79.6 g of propylene and 18.9 g of ethylene were consumed.
The pressure into the autoclave was decreased until 20 bar, the bottom discharge valve was opened and the copolymer was discharged into a heated steel tank containing water at 70° C. The tank heating was switched off and a flow of nitrogen at 0.5 bar-g was fed. After cooling at room temperature, the steel tank was opened and the wet polymer collected. The wet polymer was dried in an oven under reduced pressure at 70° C. Polymerization data are reported in table 1
The procedure of example 1 was repeated feeding 958 g of c-hexane, 41 g of Ethylene and 651 g of propylene in order to obtain a liquid composition at 90° C., 29 bar-g, corresponding to a liquid composition of 5/95% wt ethylene/propylene.
1 mL of the catalyst system A-1C containing the catalyst/cocatalyst mixture (1.92 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 14/86% wt was continuously fed for 30 minutes to maintain the pressure of 29 bar-g:98.6 g of propylene and 16.3 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of c-hexane, 64 g of Ethylene and 473 g of propylene in order to obtain a liquid composition at 90° C., 23 bar-g, corresponding to a liquid composition of 10/90% wt ethylene/propylene.
1 mL of the catalyst system A-1C containing the catalyst/cocatalyst mixture (1.92 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 20/80% wt was continuously fed for 30 minutes to maintain the pressure of 23 bar-g:30.9 g of propylene and 7.5 g of ethylene were consumed. The results are reported in Table 1.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of c-hexane, 31 g of Ethylene and 500 g of propylene in order to obtain a liquid composition at 90° C., 22 bar-g, corresponding to a liquid composition of 5/95% wt ethylene/propylene.
2 mL of the catalyst system C-1C containing the catalyst/cocatalyst mixture (1.48 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 19/81% wt was continuously fed for 30 minutes to maintain the pressure of 22 bar-g:22.6 g of propylene and 5.3 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of c-hexane, 50 g of Ethylene and 484 g of propylene in order to obtain a liquid composition at 90° C., 23 bar-g, corresponding to a liquid composition of 8/92% wt ethylene/propylene.
3 mL of the solution the catalyst system C-1C containing the catalyst/cocatalyst mixture (1.48 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 18/82% wt was continuously fed for 30 minutes to maintain the pressure of 23 bar-g:72.6 g of propylene and 14.9 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of cyclohexane, 64 g of ethylene and 473 g of propylene in order to obtain a liquid composition at 90° C., 26 bar-g, corresponding to a liquid composition of 10/90% wt ethylene/propylene.
4 mL of the catalyst system C-1C containing the catalyst/cocatalyst mixture (1.48 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 20/80% wt was continuously fed for 30 minutes to maintain the pressure of 26 bar-g:186.5 g of propylene and 45.9 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of cyclohexane, 31 g of ethylene and 500 g of propylene in order to obtain a liquid composition at 90° C., 21 bar-g, corresponding to a liquid composition of 5/95% wt ethylene/propylene.
4 mL of the catalyst system C-2C containing the catalyst/cocatalyst mixture (1.74 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 11/89% wt was continuously fed for 30 minutes to maintain the pressure of 21 bar-g:33.7 g of propylene and 4.1 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of cyclo-hexane, 50 g of ethylene and 484 g of propylene in order to obtain a liquid composition at 90° C., 24 bar-g, corresponding to a liquid composition of 8/92% wt ethylene/propylene.
4 mL of the catalyst system C-1C containing the catalyst/cocatalyst mixture (1.74 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of cyclohexane through the stainless-steel vial.
A mixture of ethylene/propylene 16/84% wt was continuously fed for 30 minutes to maintain the pressure of 24 bar-g:31.2 g of propylene and 5.9 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
The procedure of example 1 was repeated feeding 958 g of cyclo-hexane, 64 g of ethylene and 473 g of propylene in order to obtain a liquid composition at 90° C., 26 bar-g, corresponding to a liquid composition of 10/90% wt ethylene/propylene.
4 mL of the catalyst system C-2C containing the catalyst/cocatalyst mixture (1.74 mg metallocene/mL solution) was injected in the autoclave by means of 4 mL of c-hexane through the stainless-steel vial.
A mixture of ethylene/propylene 20/80% wt was continuously fed for 30 minutes to maintain the pressure of 26 bar-g:86.5 g of propylene and 21.6 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 950 g of cyclo-hexane, 70.5 g of ethylene and 469 g of propylene were fed into the reactor in order to obtain a liquid composition at 90° C., 26.85 bar-g, corresponding to a liquid composition of 13/87% wt ethylene/propylene.
115 mg of the catalyst A-0C was injected in the autoclave by means of 5 mL of isododecane through the stainless-steel vial.
A mixture of ethylene propylene 20/80% wt was continuously fed for 30 minutes to maintain the pressure of 26.85 bar-g:118.5 g of propylene and 30.6 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
From table 1 it clearly results that the polymerization activity of the metallocene compounds of formula (I) used in the process of the present invention is considerably higher than that of the metallocene compounds used in the comparative examples at the same polymerization conditions. Also the molecular weight of the polymer obtained with the process of the present invention is higher than those of the comparative example. This higher activity is maintained also when the metallocene compounds of formula (I) are supported.
21.8 mL of TIBA/isododecane solution (110 g/L) were mixed with 5 mL of MAO/toluene solution (Albemarle 30% wt/wt, 24 mmol MAO) to obtain a MAO/TIBA molar ratio of 2:1. The solution was stirred for 30 min at room temperature. Then, 49.6 mg of A-1 were dissolved in the solution and the resulting green/brown suspension was diluted with 11.7 mL of isododecane to reach a concentration of 100 gTOT/L and 1.29 gmetallocene/L. The mixture turned to a dark orange solution after overnight stirring at room temperature.
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 720 g of cyclo-hexane, 35 g of ethylene and 654 g of propylene were fed into the reactor in order to obtain a liquid composition at 100° C., 33 bar-g, corresponding to a liquid composition of 0.04 (wt/wt) ethylene/propylene.
1 ml of the catalyst A-1Cl was injected in the autoclave by means of 5 mL of isododecane through the stainless-steel vial.
ethylene propylene 10/90% wt was continuously fed for 30 minutes to maintain the pressure of 33 bar-g:171.3 g of propylene and 19.7 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 715 g of cyclo-hexane, 61 g of ethylene and 631 g of propylene and 50 ml of hydrogen were fed into the reactor in order to obtain a liquid composition at 100° C., 35 bar-g, corresponding to a liquid composition of 0.08 (wt/wt) ethylene/propylene.
1 ml of the catalyst A-1Cl was injected in the autoclave by means of 5 mL of isododecane through the stainless-steel vial.
ethylene propylene 17/83% wt was continuously fed for 30 minutes to maintain the pressure of 35 bar-g:109.3 g of propylene and 22.8 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 715 g of cyclo-hexane, 61 g of ethylene and 631 g of propylene and 500 ml of hydrogen were fed into the reactor in order to obtain a liquid composition at 100° C., 35 bar-g, corresponding to a liquid composition of 0.08 (wt/wt) ethylene/propylene.
1 ml of the catalyst A-1Cl was injected in the autoclave by means of 5 mL of isododecane through the stainless-steel vial.
ethylene propylene 17/83% wt was continuously fed for 30 minutes to maintain the pressure of 35 bar-g:238 g of propylene and 48.6 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 676 g of cyclo-hexane, 72 g of ethylene and 647 g of propylene were fed into the reactor in order to obtain a liquid composition at 100° C., 38 bar-g, corresponding to a liquid composition of 0.09 (wt/wt) ethylene/propylene.
1.5 ml of the catalyst A-1Cl was injected in the autoclave by means of 5 mL of isododecane through the stainless-steel vial.
ethylene propylene 21/79% wt was continuously fed for 30 minutes to maintain the pressure of 38 bar-g:96.1 g of propylene and 25.7 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
A 4.4 L jacketed stainless-steel autoclave, equipped with a magnetically driven stirrer and a 35-mL stainless-steel vial and connected to a thermostat for temperature control, was previously purified by washing with an Al(i-Bu)3 solution in hexane and dried at 50° C. in a stream of nitrogen.
6 mmol of Al(i-Bu)3 (as a 100 g/L solution in hexane), 859 g of cyclo-hexane, 53 g of ethylene and 508 g of propylene were fed into the reactor in order to obtain a liquid composition at 120° C., 37 bar-g, corresponding to a liquid composition of 0.09 (wt/wt) ethylene/propylene.
1.5 ml of the catalyst A-1Cl was injected in the autoclave by means of 5 mL of isododecane through the stainless-steel vial.
ethylene propylene 17/83% wt was continuously fed for 30 minutes to maintain the pressure of 37 bar-g:144.6 g of propylene and 29.7 g of ethylene were consumed.
The copolymer was discharged according to the procedure described in the first example.
| Number | Date | Country | Kind |
|---|---|---|---|
| 0515137.3 | Jun 2005 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2006/062964 | 6/7/2006 | WO | 00 | 12/12/2007 |
| Number | Date | Country | |
|---|---|---|---|
| 60690629 | Jun 2005 | US |
