Patent Application
20130102744
The present invention relates to a catalyst system capable to show, in propylene polymerization, high activity, stereospecificity and increased hydrogen response. Catalyst systems for the stereospecific polymerization of olefins are widely known in the art. The most common type of catalyst system belongs to the Ziegler-Natta family and comprises a solid catalyst component, constituted by a magnesium dihalide on which are supported a titanium compound and an internal electron donor compound, used in combination with an Al-alkyl compound. Conventionally however, when a higher crystallinity of the polymer is required, also an external donor, usually an alkylalkoxysilane, is needed in order to obtain higher isotacticity. In fact, when an external donor is absent, the isotactic index of the resulting polymer is not sufficiently high even if a 1,3-diether is used as internal donor.
In certain applications, particularly in thin wall injection molding (TWIM) it is necessary to use polymers with relatively high fluidity i.e., with a relatively lower molecular weight in order to have high quality moldings.
The low molecular weight polymers are commonly obtained by increasing the content of the chain transfer agent (molecular weight regulator) in particular hydrogen which is commonly used industrially.
In the case of TWIM applications both high cristallinity and low molecular weight is required, and therefore the catalyst system has to incorporate also an external donor.
However, the use of the most common external donors like alkylalkoxysilane leads to a worsening of the hydrogen response, i.e., to the capability of producing increasingly short polymer chain in respect of incremental hydrogen concentration.
This means that it is necessary to increase the hydrogen content in the polymerization mixture thereby increasing the pressure of the reaction system which in turn would make necessary the use of equipments especially designed to withstand to higher pressure and thus being more expensive. A possible solution, particularly for liquid-phase polymerization, would be to run the plant at a lower temperature which can allow a reduced pressure, but this negatively impacts the efficiency of heat exchange and the relative plant productivity.
Therefore, it would be necessary to have a catalyst system showing an improved hydrogen response, i.e., capability of producing polymers with a lower molecular weight in the presence of small amounts of hydrogen.
Examples of catalysts having high hydrogen response are the Ziegler-Natta catalysts containing 1,3-diethers described for example in EP622380. Such catalysts components are generally able to produce propylene polymers with high melt flow rates. When an external donor of the alkylalkoxysilane type is added in order to increase its stereospecificity, the hydrogen response of the catalyst is lowered.
The applicant has found that the selection of a specific type of catalyst system is able to solve the afore-mentioned problem. It is therefore an object of the present invention a catalyst system comprising the product obtained by contacting (a) a solid catalyst component containing Mg, Ti, halogen and at least an electron donor compound selected from 1,3-diethers;
(b) an alkylaluminum cocatalyst; and
(c) an ester of formula ROOC—(CH2)n—COOR in which n is an integer from 2 to 8 and the R groups, equal to or different from each other, are C1-C10 alkyl groups.
Preferably, the solid catalyst component comprises Mg, Ti, halogen and an electron donor selected from 1,3-diethers of formula (I):
where RI and RII are the same or different and are hydrogen or linear or branched C1-C18 hydrocarbon groups which can also form one or more cyclic structures; RIII groups, equal or different from each other, are hydrogen or C1-C18 hydrocarbon groups; RIV groups equal or different from each other, have the same meaning of RIII except that they cannot be hydrogen; each of RI to RIV groups can contain heteroatoms selected from halogens, N, O, S and Si.
In the electron donor of formula (I) preferably, RN is a 1-6 carbon atom alkyl radical and more particularly a methyl while the RIII radicals are preferably hydrogen. Moreover, when RI is methyl, ethyl, propyl, or isopropyl, RII can be ethyl, propyl, isopropyl, butyl, isobutyl, tert-butyl, isopentyl, 2-ethylhexyl, cyclopentyl, cyclohexyl, methylcyclohexyl, phenyl or benzyl; when RI is hydrogen, RII can be ethyl, butyl, sec-butyl, tert-butyl, 2-ethylhexyl, cyclohexylethyl, diphenylmethyl, p-chlorophenyl, 1-naphthyl, 1-decahydronaphthyl; RI and RII can also be the same and can be ethyl, propyl, isopropyl, butyl, isobutyl, tert-butyl, neopentyl, phenyl, benzyl, cyclohexyl, cyclopentyl. Specific examples of ethers that can be advantageously used include: 2-(2-ethylhexyl)1,3-dimethoxypropane, 2-isopropyl-1,3-dimethoxypropane, 2-butyl-1,3-dimethoxypropane, 2-sec-butyl-1,3-dimethoxypropane, 2-cyclohexyl-1,3-dimethoxypropane, 2-phenyl-1,3-dimethoxypropane, 2-tert-butyl-1,3-dimethoxypropane, 2-cumyl-1,3-dimethoxypropane, 2-(2-phenylethyl)-1,3-dimethoxypropane, 2-(2-cyclohexylethyl)-1,3-dimethoxypropane, 2-(p-chlorophenyl)-1,3-dimethoxypropane, 2-(diphenylmethyl)-1,3-dimethoxypropane, 2 (1-naphthyl)-1,3-dimethoxypropane, 2(p-fluorophenyl)-1,3-dimethoxypropane, 2(1-decahydronaphthyl)-1,3-dimethoxypropane, 2(p-tert-butylphenyl)-1,3-dimethoxypropane, 2,2-dicyclohexyl-1,3-dimethoxypropane, 2,2-diethyl-1,3-dimethoxypropane, 2,2-dipropyl-1,3-dimethoxypropane, 2,2-dibutyl-1,3-dimethoxypropane, 2,2-diethyl-1,3-diethoxypropane, 2,2-dicyclopentyl-1,3-dimethoxypropane, 2,2-dipropyl-1,3-diethoxypropane, 2,2-dibutyl-1,3-diethoxypropane, 2-methyl-2-ethyl-1,3-dimethoxypropane, 2-methyl-2-propyl-1,3-dimethoxypropane, 2-methyl-2-benzyl-1,3-dimethoxypropane, 2-methyl-2-phenyl-1,3-dimethoxypropane, 2-methyl-2-cyclohexyl-1,3-dimethoxypropane, 2-methyl-2-methylcyclohexyl-1,3-dimethoxypropane, 2,2-bis (p-chlorophenyl)-1,3-dimethoxypropane, 2,2-bis(2-phenylethyl)-1,3-dimethoxypropane, 2,2-bis(2-cyclohexylethyl)-1,3-dimethoxypropane, 2-methyl-2-isobutyl-1,3-dimethoxypropane, 2-methyl-2-(2-ethylhexyl)-1,3-dimethoxypropane, 2,2-bis(2-ethylhexyl)-1,3-dimethoxypropane, 2,2-bis(p-methylphenyl)-1,3-dimethoxypropane, 2-methyl-2-isopropyl-1,3-dimethoxypropane, 2,2-diisobutyl-1,3-dimethoxypropane, 2,2-diphenyl-1,3-dimethoxypropane, 2,2-dibenzyl-1,3-dimethoxypropane, 2-isopropyl-2-cyclopentyl-1,3-dimethoxypropane, 2,2-bis(cyclohexylmethyl)-1,3-dimethoxypropane, 2,2-diisobutyl-1,3-diethoxypropane, 2,2-diisobutyl-1,3-dibutoxypropane, 2-isobutyl-2-isopropyl-1,3-dimetoxypropane, 2,2-di-sec-butyl-1,3-dimetoxypropane, 2,2-di-tert-butyl-1,3-dimethoxypropane, 2,2-dineopentyl-1,3-dimethoxypropane, 2-iso-propyl-2-isopentyl-1,3-dimethoxypropane, 2-phenyl-2-benzyl-1,3-dimetoxypropane, 2-cyclohexyl-2-cyclohexylmethyl-1,3-dimethoxypropane.
Furthermore, particularly preferred are the 1,3-diethers of formula (II)
where the radicals RIV have the same meaning explained above and the radicals RIII and RV, equal or different to each other, are selected from the group consisting of hydrogen; halogens, preferably Cl and F; C1-C20 alkyl radicals, linear or branched; C3-C20 cycloalkyl, C6-C20 aryl, C7-C20 alkylaryl and C7-C20 arylalkyl radicals and two or more of the RV radicals can be bonded to each other to form condensed cyclic structures, saturated or unsaturated, optionally substituted with RVI radicals selected from the group consisting of halogens, preferably Cl and F; C1-C20 alkyl radicals, linear or branched; C3-C20 cycloalkyl, C6-C20 aryl, C7-C20 alkylaryl and C7-C20 arylalkyl radicals; said radicals RV and RVI optionally containing one or more heteroatoms as substitutes for carbon or hydrogen atoms, or both.
Preferably, in the 1,3-diethers of formulae (I) and (II) all the RIII radicals are hydrogen, and all the RIV radicals are methyl. Moreover, are particularly preferred the 1,3-diethers of formula (II) in which two or more of the RV radicals are bonded to each other to form one or more condensed cyclic structures, preferably benzenic, optionally substituted by RVI radicals. Specially preferred are the compounds of formula (III):
where the RVI radicals equal or different are hydrogen; halogens, preferably Cl and F; C1-C20 alkyl radicals, linear or branched; C3-C20 cycloalkyl, C6-C20 aryl, C7-C20 alkylaryl and C7-C20 arylalkyl radicals, optionally containing one or more heteroatoms selected from the group consisting of N, O, S, P, Si and halogens, in particular Cl and F, as substitutes for carbon or hydrogen atoms, or both; the radicals RIII and RIV are as defined above for formula (II).
Specific examples of compounds comprised in formulae (I) and (II) are:
1,1-bis(methoxymethyl)-cyclopentadiene;
1,1-bis(methoxymethyl)-2,3,4,5-tetramethylcyclopentadiene;
1, 1-bis(methoxymethyl)-2,3,4,5-tetraphenylcyclopentadiene;
1,1-bis(methoxymethyl)-2,3,4,5-tetrafluorocyclopentadiene;
1,1-bis(methoxymethyl)-3,4-dicyclopentylcyclopentadiene;
1,1-bis(methoxymethyl)indene; 1,1-bis(methoxymethyl)-2,3-dimethylindene;
1,1-bis(methoxymethyl)-4,5,6,7-tetrahydroindene;
1,1-bis(methoxymethyl)-2,3,6,7-tetrafluoroindene;
1,1-bis(methoxymethyl)-4,7-dimethylindene;
1,1-bis(methoxymethyl)-3,6-dimethylindene;
1,1-bis(methoxymethyl)-4-phenylindene;
1,1-bis(methoxymethyl)-4-phenyl-2-methylindene;
1,1-bis(methoxymethyl)-4-cyclohexylindene;
1,1-bis(methoxymethyl)-7-(3,3,3-trifluoropropyl)indene;
1,1-bis(methoxymethyl)-7-trimethyilsilylindene;
1,1-bis(methoxymethyl)-7-trifluoromethylindene;
1,1-bis(methoxymethyl)-4,7-dimethyl-4,5,6,7-tetrahydroindene;
1,1-bis(methoxymethyl)-7-methylindene;
1,1-bis(methoxymethyl)-7-cyclopentylindene;
1,1-bis(methoxymethyl)-7-isopropylindene;
1,1-bis(methoxymethyl)-7-cyclohexylindene;
1,1-bis(methoxymethyl)-7-tert-butylindene;
1,1-bis(methoxymethyl)-7-tert-butyl-2-methylindene;
1,1-bis(methoxymethyl)-7-phenylindene;
1,1-bis(methoxymethyl)-2-phenylindene;
1,1-bis(methoxymethyl)-1H-benz[e]indene;
1,1-bis(methoxymethyl)-1H-2-methylbenz[e]indene;
9,9-bis(methoxymethyl)fluorene;
9,9-bis(methoxymethyl)-2,3,6,7-tetramethylfluorene;
9,9-bis(methoxymethyl)-2,3,4,5,6,7-hexafluorofluorene;
9,9-bis(methoxymethyl)-2,3-benzofluorene;
9,9-bis(methoxymethyl)-2,3,6,7-dibenzofluorene;
9,9-bis(methoxymethyl)-2,7-diisopropylfluorene;
9,9-bis(methoxymethyl)-1,8-dichlorofluorene;
9,9-bis(methoxymethyl)-2,7-dicyclopentylfluorene;
9,9-bis(methoxymethyl)-1,8-difluorofluorene;
9,9-bis(methoxymethyl)-1,2,3,4-tetrahydrofluorene;
9,9-bis(methoxymethyl)-1,2,3,4,5,6,7,8-octahydrofluorene;
9,9-bis(methoxymethyl)-4 -tert-butylfluorene.
In addition to the 1,-3 diethers above described the solid catalyst component (a) can also contain additional electron donors belonging to ethers, esters of aromatic or aliphatic mono or dicarboxylic acids, ketones, or alkoxyesters. Among them particularly preferred are the esters of succinic acids according to formula (I) of EP1088009.
The additional donors may be present in an amount such that the 1,3-diether/other donor molar ratio ranges from 0.1 to 10 preferably from 0.2 to 8.
As explained above, the catalyst components of the invention comprise, in addition to the above electron donors, Ti, Mg and halogen. In particular, the catalyst components comprise a titanium compound, having at least a Ti-halogen bond and the above mentioned electron donor compounds supported on a Mg halide. The magnesium halide is preferably MgCl2 in active form which is widely known from the patent literature as a support for Ziegler-Natta catalysts. Patents U.S. Pat. No. 4,298,718 and U.S. Pat. No. 4,495,338 were the first to describe the use of these compounds in Ziegler-Natta catalysis. It is known from these patents that the magnesium dihalides in active form used as support or co-support in components of catalysts for the polymerization of olefins are characterized by X-ray spectra in which the most intense diffraction line that appears in the spectrum of the non-active halide is diminished in intensity and is replaced by a halo whose maximum intensity is displaced towards lower angles relative to that of the more intense line.
The preferred titanium compounds used in the catalyst component of the present invention are TiCl4 and TiCl3; furthermore, also Ti-haloalcoholates of formula Ti(OR)n-yXy can be used, where n is the valence of titanium, y is a number between 1 and n-1, X is halogen and R is a hydrocarbon radical having from 1 to 10 carbon atoms.
The preparation of the solid catalyst component can be carried out according to several methods. According to one of these methods, the magnesium dichloride in an anhydrous state, the titanium compound and the electron donor compounds are milled together under conditions in which activation of the magnesium dichloride occurs. The so obtained product can be treated one or more times with an excess of TiCl4 at a temperature between 80 and 135° C. This treatment is followed by washings with hydrocarbon solvents until chloride ions have disappeared. According to a further method, the product obtained by co-milling the magnesium chloride in an anhydrous state, the titanium compound and the electron donor compounds are treated with halogenated hydrocarbons such as 1,2-dichloroethane, chlorobenzene, dichloromethane etc. The treatment is carried out for a time between 1 and 4 hours and at temperature of from 40° C. to the boiling point of the halogenated hydrocarbon. The product obtained is then generally washed with inert hydrocarbon solvents such as hexane.
According to another method, magnesium dichloride is preactivated according to well known methods and then treated with an excess of TiCl4 at a temperature of about 80 to 135° C. in the presence of the electron donor compounds. The treatment with TiCl4 is repeated and the solid is washed with hexane in order to eliminate any non-reacted TiCl4. A further method described in WO2005/095472 comprises reacting, in the presence of a 1,3-diether, a titanium compound having at least Ti—Cl bond with a precursor of formula MgCln(OR)2-nLBp in which n is from 0.1 to 1.9, p is higher than 0 4, and R is a C1-C15 hydrocarbon group. Preferably, the reaction is carried out in and an excess of TiCl4 at a temperature of about 80 to 120° C.
According to a preferred method, the solid catalyst component can be prepared by reacting a titanium compound of formula Ti(OR)n-yXy, where n is the valence of titanium and y is a number between 1 and n, preferably TiCl4, with a magnesium chloride deriving from an adduct of formula MgCl2pROH, where p is a number between 0.1 and 6, preferably from 2 to 3.5, and R is a hydrocarbon radical having 1-18 carbon atoms. The adduct can be suitably prepared in spherical form by mixing alcohol and magnesium chloride in the presence of an inert hydrocarbon immiscible with the adduct, operating under stirring conditions at the melting temperature of the adduct (100-130° C.). Then, the emulsion is quickly quenched, thereby causing the solidification of the adduct in form of spherical particles. Examples of spherical adducts prepared according to this procedure are described in U.S. Pat. No. 4,399,054 and U.S. Pat. No. 4,469,648. The so obtained adduct can be directly reacted with Ti compound or it can be previously subjected to thermal controlled dealcoholation (80-130° C.) so as to obtain an adduct in which the number of moles of alcohol is generally lower 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 (generally 0° C.); the mixture is heated up to 80-130° C. and kept at this temperature for 0.5-2 hours. The treatment with TiCl4 can be carried out one or more times. The electron donor compounds can be added during the treatment with TiCl4. They can be added together in the same treatment with TiCl4 or separately in two or more treatments. The preparation of catalyst components in spherical form are described for example in European Patent Applications EP-A-395083, EP-A-553805, EP-A-553806, EPA601525 and WO98/44001.
The solid catalyst components obtained according to the above method show a surface area (by B.E.T. method) generally between 20 and 500 m2/g and preferably between 50 and 400 m2/g, and a total porosity (by B.E.T. method) higher than 0.2 cm3/g preferably between 0.2 and 0.6 cm3/g. The porosity (Hg method) due to pores with radius up to 10.000 Å generally ranges from 0.3 to 1.5 cm3/g, preferably from 0.45 to 1 cm3/g. The solid catalyst component has an average particle size ranging from 5 to 120 μm and more preferably from 10 to 100 μm.
The alkyl-Al compound (b) is preferably selected from the trialkyl aluminum compounds such as for example triethylaluminum, triisobutylaluminum, tri-n-butylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum. It is also possible to use mixtures of trialkylaluminum's with alkylaluminum halides, alkylaluminum hydrides or alkylaluminum sesquichlorides such as AlEt2Cl and Al2Et3Cl3.
The ester (c) is used as external electron donor and is preferably selected from the compounds in which R is a C1-C6 linear or branched alkyl, preferably ethyl or isobutyl. In the esters (c) n is preferably from 2 to 7, more preferably from 4 to 6 and especially from 4 to 5.
Non limitative examples of esters (c) are diethyl succinate, diethyl glutarate, diethyl adipate, diethyl suberate, diethyl pimelate and the corresponding esters deriving from substitution of ethyl with methyl, isobutyl, or 2-ethylhexyl.
The catalyst of the invention is able to polymerize any kind of CH2═CHR olefins in which R is hydrogen or a C1-C10 hydrocarbon group or mixtures of such olefins. However, as mentioned above, it is particularly suited for the preparation of propylene polymers due to the fact that it shows increased hydrogen response with respect to the most common used alkylalkoxysilane, while maintaining high stereospecificity expressed by a percentage of xylene insolubility at 25° C. generally of 97% or higher. The Molecular Weight Distribution (expressed as polydispersity index determined as described hereinafter) remains narrow, generally lower than 4 and preferably lower than or equal to 3.5. Another important advantage is that hydrogen response and high stereospecificity are retained while maintaining a very good level of polymerization activity.
Any kind of polymerization process can be used with the catalysts of the invention that are very versatile. The polymerization can be carried out for example in slurry using as diluent a liquid inert hydrocarbon, or in bulk using the liquid monomer (propylene) as a reaction medium, or in solution using either monomers or inert hydrocarbons as solvent for the nascent polymer. Moreover, it is possible to carry out the polymerization process in gas-phase operating in one or more fluidized or mechanically agitated bed reactors.
The process of the present invention is particularly advantageous for producing said isotactic propylene polymers with high fluidity in liquid phase because in such a type of process the pressure problems connected to the use of increased amounts of hydrogen is more evident. As mentioned, the liquid phase process can be either in slurry, solution or bulk (liquid monomer). This latter technology is the most preferred and can be carried out in various types of reactors such as continuous stirred tank reactors, loop reactors or plug-flow ones. The polymerization is generally carried out at temperature of from 20 to 120° C., preferably of from 40 to 85° C. When the polymerization is carried out in gas-phase the operating pressure is generally between 0.5 and 10 MPa, preferably between 1 and 5 MPa. In the bulk polymerization the operating pressure is generally between 1 and 6 MPa preferably between 1.5 and 4 MPa.
The catalyst of the present invention can be used as such in the polymerization process by introducing it directly into the reactor. In the alternative, the catalyst can be pre-polymerized before being introduced into the first polymerization reactor. The term pre-polymerized, as used in the art, means a catalyst which has been subject to a polymerization step at a low conversion degree. According to the present invention a catalyst is considered to be pre-polymerized when the amount the polymer produced is from about 0.1 up to about 1000 g per gram of solid catalyst component.
The pre-polymerization can be carried out with the a-olefins selected from the same group of olefins disclosed before. In particular, it is especially preferred pre-polymerizing ethylene or mixtures thereof with one or more a-olefins in an amount up to 20% by mole. Preferably, the conversion of the pre-polymerized catalyst component is from about 0.2 g up to about 500 g per gram of solid catalyst component.
The pre-polymerization step can be carried out at temperatures from 0 to 80° C. preferably from 5 to 50° C. in liquid or gas-phase. The pre-polymerization step can be performed in-line as a part of a continuous polymerization process or separately in a batch process. The batch pre-polymerization of the catalyst of the invention with ethylene in order to produce an amount of polymer ranging from 0.5 to 20 g per gram of catalyst component is particularly preferred.
The following examples are given in order to better illustrate the invention without limiting it.
Characterization
Determination of X.I.
2.5 g of polymer and 250 ml of o-xylene were placed in a round-bottomed flask provided with a cooler and a reflux condenser and kept under nitrogen. The obtained mixture was heated to 135° C. and was kept under stirring for about 60 minutes. The final solution was allowed to cool to 25° C. under continuous stirring, and the insoluble polymer was then filtered. The filtrate was then evaporated in a nitrogen flow at 140° C. to reach a constant weight. The content of said xylene-soluble fraction is expressed as a percentage of the original 2.5 grams and then, by difference, the X.I. %.
Melt Flow Rate (MFR)
Determined according to ISO 1133 (230° C., 2.16 Kg)
Polydispersity Index (Pd.)
Determined at a temperature of 200° C. by using a parallel plates rheometer model RMS-800 marketed by RHEOMETRICS (USA), operating at an oscillation frequency which increases from 0.1 rad/sec to 100 rad/sec. The value of the polydispersity index is derived from the crossover modulus by way of the equation:
P.I.=105/Gc
in which Gc is the crossover modulus defined as the value (expressed in Pa) at which G′=G″ wherein G′ is the storage modulus and G″ is the loss modulus.
General Procedure for Preparation of the Spherical Adduct
An initial amount of microspheroidal MgCl2.2.8C2H5OH was prepared according to the method described in ex.2 of WO98/44009 but operating on larger scale. The solid adduct so obtained were then subject to thermal dealcoholation at increasing temperatures from 30 to 130° C. and operating in nitrogen current until reaching an alcohol content of 2.1 moles per mol of MgCl2.
General Procedure A for the Preparation of the Solid Catalyst Component (Examples 1-17, Comp. 1-3)
Into a 500 ml round bottom flask, equipped with mechanical stirrer, cooler and thermometer 250 ml of TiCl4 were introduced at room temperature under nitrogen atmosphere. After cooling to 0° C., while stirring, the internal donor 9,9-bis(methoxymethyl)fluorene and 10.0 g of microspheroidal MgCl2.2.1C2H5OH (prepared as described above) were sequentially added into the flask. The amount of 9,9-bis(methoxymethyl)fluorene was specifically charged in order to have a Mg/donor molar ratio of 6. The temperature was raised to 100° C. and maintained for 1 hour. Thereafter, stirring was stopped, the solid product was allowed to settle and the supernatant liquid was siphoned off maintaining the temperature at 100° C. After the supernatant was removed, additional 250 ml of fresh TiCl4 were added. The mixture was then heated at 110° C. and kept at this temperature for 60 minutes. Once again the stirring was interrupted; the solid product was allowed to settle and the supernatant liquid was siphoned off maintaining the temperature at 110° C. A third aliquot of fresh TiCl4 (250 ml) was added, the mixture was maintained under agitation at 110° C. for 30 minutes and then the supernatant liquid was siphoned off The solid was washed with anhydrous hexane six times (6×100 ml) in temperature gradient down to 60° C. and one time (100 ml) at room temperature. The solid was finally dried under vacuum and analyzed. The amount of Ti bonded on the catalyst resulted in 3.9% wt., while the amount of internal donor bonded resulted in 12% wt.
General Procedure B for the Preparation of the Solid Catalyst Component (Examples 18-21, Comp. 4)
Into a 500 ml round bottom flask, equipped with mechanical stirrer, cooler and thermometer 250 ml of TiCl4 were introduced at room temperature under nitrogen atmosphere. After cooling to 0° C., while stirring, the internal donors 9,9-bis(methoxymethyl)fluorene and diethyl 2,3-diisopropylsuccinate and 10.0 g of microspheroidal MgCl2.2.1C2H5OH (prepared as described above) were sequentially added into the flask. The amount of 9,9-bis(methoxymethyl)fluorene and diethyl 2,3-diisopropylsuccinate were specifically charged in order to have a Mg/total donor molar ratio of 8. The temperature was raised to 100° C. and maintained for 1 hour. Thereafter, stirring was stopped, the solid product was allowed to settle and the supernatant liquid was siphoned off maintaining the temperature at 100° C. After the supernatant was removed, additional 250 ml of fresh TiCl4 were added. The mixture was then heated at 110° C. and kept at this temperature for 60 minutes. Once again the stirring was interrupted; the solid product was allowed to settle and the supernatant liquid was siphoned off maintaining the temperature at 110° C. A third aliquot of fresh TiCl4 (250 ml) was added, the mixture was maintained under agitation at 110° C. for 30 minutes and then the supernatant liquid was siphoned off The solid was washed with anhydrous hexane six times (6×100 ml) in temperature gradient down to 60° C. and one time (100 ml) at room temperature. The solid was finally dried under vacuum and analyzed. The amount of Ti bonded on the catalyst resulted in 3.7% wt., while the amount of internal donors bonded resulted in 2.8% wt. for 9,9-bis(methoxymethyl)fluorene and 8.7% wt. for diethyl 2,3-diisopropylsuccinate.
A 4 litre steel autoclave equipped with a stirrer, pressure gauge, thermometer, catalyst feeding system, monomer feeding lines and thermostating jacket, was purged with nitrogen flow at 70° C. for one hour. Then, at 30° C. under propylene flow, were charged in sequence with 75 ml of anhydrous hexane, 0.76 g of AlEt3, the ester (c) reported in Table 1 (AlEt3/ester molar ratio of 20) and 10 mg of solid catalyst component reported in Table 1. The autoclave was closed; subsequently the amount of hydrogen reported in Table 1 was added. Then, under stirring, 1.2 Kg of liquid propylene was fed. The temperature was raised to 70° C. in five minutes and the polymerization was carried out at this temperature for two hours. At the end of the polymerization, the non-reacted propylene was removed; the polymer was recovered and dried at 70° C. under vacuum for three hours. Then the polymer was weighed, analyzed and fractionated with o-xylene to determine the amount of the xylene insoluble (X.I.) fraction. Polymer analyses, as well as catalyst activity, are reported in Table 1.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10167165.9 | Jun 2010 | EP | regional |
This application is the U.S. national phase of International Application PCT/EP2011/059267, filed Jun. 6, 2011, claiming priority to European Patent Application 10167165.9 filed Jun. 24, 2010, and the benefit under 35 U.S.C. 119(e) of U.S. Provisional Application No. 61/398,654, filed Jun. 29, 2010; the disclosures of International Application PCT/EP2011/059267, European Patent Application 10167165.9 and U.S. Provisional Application No. 61/398,654, each as filed, are incorporated herein by reference.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2011/059267 | 6/6/2011 | WO | 00 | 12/21/2012 |
| Number | Date | Country | |
|---|---|---|---|
| 61398654 | Jun 2010 | US |
