Classifications

• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F4/00—Polymerisation catalysts
  • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
  • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
  • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
  • C08F4/62—Refractory metals or compounds thereof
  • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
  • C08F4/65—Pretreating the metal or compound covered by group C08F4/64 before the final contacting with the metal or compound covered by group C08F4/44
  • C08F4/651—Pretreating with non-metals or metal-free compounds
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
  • C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F4/00—Polymerisation catalysts
  • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
  • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
  • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
  • C08F4/62—Refractory metals or compounds thereof
  • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
  • C08F4/00—Polymerisation catalysts
  • C08F4/42—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors
  • C08F4/44—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides
  • C08F4/60—Metals; Metal hydrides; Metallo-organic compounds; Use thereof as catalyst precursors selected from light metals, zinc, cadmium, mercury, copper, silver, gold, boron, gallium, indium, thallium, rare earths or actinides together with refractory metals, iron group metals, platinum group metals, manganese, rhenium technetium or compounds thereof
  • C08F4/62—Refractory metals or compounds thereof
  • C08F4/64—Titanium, zirconium, hafnium or compounds thereof
  • C08F4/65—Pretreating the metal or compound covered by group C08F4/64 before the final contacting with the metal or compound covered by group C08F4/44
  • C08F4/652—Pretreating with metals or metal-containing compounds
  • C08F4/654—Pretreating with metals or metal-containing compounds with magnesium or compounds thereof

Definitions

• the present invention relates to a process for the preparation of catalyst components supported on Mg dichloride also comprising a Ti compound and an electron donor, and also relates to certain catalyst components therefrom obtained.
• These catalyst components when converted into a catalyst, are particularly suitable for the preparation of copolymers of ethylene with ⁇ -olefins due to their capability of homogeneously distribute the ⁇ -olefins along the polymer chain and among the various polymer chains.
• the catalysts including titanium compounds supported on magnesium halides are well known in the art. Catalysts of this type are described for example in the U.S. patent No.4,298,718. Said catalysts comprise titanium tetrahalides supported on halides of magnesium. Although the catalysts have high activity in the polymerization of alpha olefins like propylene, they are not very stereospecific. Substantial improvements to the stereospecificity have been reached by adding certain electron-donor compounds to the solid catalyst component. Modern recipes for the preparation of these catalysts include first the contact between a MgCb or its precursor, with the electron donor compound and a titanium compound (usually TiCLt), and then one or more treatments of the so obtained solid with hot liquid TiC .
• One kind of catalyst preparation able to fix high amounts of donor on the catalyst component is that described for example in USP 4,521,573 which comprises the use of a large excess of the electron donor compound that acts as a solvent in respect of MgCl 2 and the titanium compound.
• the catalyst component can then be separated from the solution by precipitation or crystallization.
• This process suffers from several drawbacks.
• certain donors are not usable because in view of their chemical structure they are not able to act as solvents.
• the polymerization activity showed by these catalysts are generally rather low.
• ED electron donor compound
• fresh reactant an amount of an essential compound which comes into contact for the first time with the reaction mixture.
• mixture in which it constitutes the main component we intend that the essential compound must be the main component in terms of molar amount, with respect to the other possible compounds excluded inert solvent or diluents used to handle the said mixture.
• esters are the alkyl esters of C1-C20 aliphatic carboxylic acids and in particular C1-C8 alkyl esters of aliphatic mono carboxylic acids such as ethylacetate, methyl formiate, ethylformiate, methylacetate, propylacetate, i-propylacetate, n-butylacetate, i- butylacetate.
• Preferred alkoxysilanes are those of formula R Rb Si(OR ) c , where a and b are integer from 0 to 2, c is an integer from 1 to 4 and the sum (a+b+c) is 4; R , R , and R , are alkyl, cycloalkyl or aryl radicals with 1-18 carbon atoms optionally containing heteroatoms. Particularly preferred are the silicon compounds in which a is 0 or 1, c is 2 or 3, R is an alkyl or cycloalkyl group, optionally containing heteroatoms, and R is methyl. Examples of such preferred silicon compounds are methyltrimethoxysilane, dimethyldimethoxysilane, Irimethylmethoxysilane and t-butyltrimethoxysilane.
• Preferred alcohol are those of formula R OH " in which the R group is a C1-C20 hydrocarbon group.
• R is a C1-C10 alkyl group.
• Specific examples are methanol, ethanol, isopropanol and butanol.
• Preferred amines are those of formula NR 3 in which the R groups, are, independently, hydrogen or a C1-C20 hydrocarbon group with the proviso that they are not contemporaneously hydrogen.
• R is a C1-C10 alkyl group.
• Specific examples are dietilamine, diisopropylamine and triethylamine
• Preferred amides are those of formula R CONR 2 in which R and R are, independently, hydrogen or a C1-C20 hydrocarbon group. Specific examples are formamide and acetamide.
• Preferred nitriles are those of formula R CN where R has the same meaning given above.
• a specific example is acetonitrile.
• Preferred glycol are those having a total number of carbon atoms lower than 50. Among them particularly preferred are the 1,2 or 1,3 glycol having a total number of carbon atoms lower than 25. Specific examples are ethylenglycol, 1,2-propylenglycol and 1,3- propylenglycol.
• the ED compound is selected among, amides, esters and alkoxysilanes.
• suitable titanium compounds are the tetrahalides or the compounds of formula TiX n (OR )4-n, where 0 ⁇ n ⁇ 3, X is halogen, preferably chlorine, and R 1 is C 1 -C 10 hydrocarbon group.
• the titanium tetrachloride is the preferred compound.
• the MgCl 2 is the basic support even if minor amount of additional carriers can be used.
• the MgCb can be used as such or obtained from Mg compounds used as precursors that can be transformed into MgCb by the reaction with halogenating compounds.
• MgCb in active form which is widely known from the patent literature as a support for Ziegler-Natta catalysts.
• Patents USP 4,298,718 and USP 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 ASTM-card reference of the spectrum of the non-active halide is diminished in intensity and broadened.
• the X-ray spectra of preferred magnesium dihalides in active form said most intense line is diminished in intensity and replaced by a halo whose maximum intensity is displaced towards lower angles relative to that of the most intense line.
• the process of the present invention in his basic version, is simple to be carried out. In fact, it comprises first contacting the titanium compound and the Mg compound, preferably Mg dihalide, optionally in the presence of an inert medium, in order to prepare an intermediate product, containing a titanium compound supported on Mg dichloride, that, if desired can also be isolated.
• the ED compound is then contacted with this intermediate product under condition such that it is added to the reaction mixture alone or in a mixture with other compounds in which it represents the main component in terms of molar amount.
• the ED treated product can then be subject to washings with the proper solvents in order to recover the final product. If needed, the treatment with the ED compound desired can be repeated one or more times.
• preformed MgCb is used a starting compound, it is preferred that it is in active form.
• the patents USP 4,298,718 and USP 4,495,338 describe how to obtain MgCb in active form.
• the titanium compound is preferably titanium tetrachloride.
• a precursor of Mg dihalide can be used as starting essential Mg compound.
• This can be selected for example among Mg compound of formula MgR' 2 where the R' groups can be independently C1-C20 hydrocarbon groups optionally substituted, OR groups, OCOR groups, halogen, in which R is a C1-C20 hydrocarbon groups optionally substituted, with the obvious proviso that the R' groups are not simultaneously halogen.
• suitable as precursors are the Lewis adducts between Mg dihalides and suitable Lewis bases.
• a particular and preferred class being constituted by the MgX (R"OH)m adducts in which R" groups are C1-C20 hydrocarbon groups, preferably C1-C10 alkyl groups, X is halogen preferably chlorine and m is from 0.1 to 6, preferably from 0.5 to 3 and more preferably from 0.5 to 2.
• Adducts of this type can generally be obtained 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.
• MgCl 2 «(EtOH) m adducts in which m is from 0.15 to 1.7 obtained subjecting the adducts with a higher alcohol content to a thermal dealcoholation process carried out in nitrogen flow at temperatures comprised between 50 and 150°C until the alcohol content is reduced to the above value.
• a process of this type is described in EP 395083.
• the dealcoholation can also be carried out chemically by contacting the adduct with compounds capable to react with the alcohol groups.
• these dealcoholated adducts are also characterized by a porosity (measured by mercury method ) due to pores with radius due to pores with radius up to 0.1 ⁇ ranging
• the MgX 2 (R"OH)m adducts are generally converted into the corresponding halides through the reaction with dealcoholating compounds.
• the dealcoholating agent can be any chemical agent having functionalities capable to react with the OH groups.
• a particular group of dealcoholating agents is that of alkyl aluminum compounds.
• Suitable alkyl aluminum compounds are the trialkyl aluminum compounds such as for example triethylaluminum, triisobutylaluminum, tri-n-butylaluminum, tri-n-hexylaluminum, tri-n- octylaluminum and tris(2,4,4-trimethyl-pentyl)aluminum. It is also possible to use mixtures of trialkylaluminum compounds with alkylaluminum halides, alkylaluminum hydrides or alkylalu inum sesquichlorides, such as AlEbCl and Al Et 3 Cl3.
• alkylaluminum compounds can have a reducing activity with respect to the Ti compounds. Accordingly, if this activity is undesired, a deactivating agent, for instance O 2 , can be added before carrying out the step (b) and thus avoiding the reduction of the titanium compound.
• a deactivating agent for instance O 2
• Another group of usable dealcoholating agent is that of halogen-containing silicon compounds.
• silicon compounds include the silicon halides having formula SiX - n Yn, in which X and Y represent halogen atoms, e.g., CI and Br, and n is a number varying from zero to 3.
• X and Y represent halogen atoms, e.g., CI and Br
• n is a number varying from zero to 3.
• the dealcoholation reaction is carried out simultaneously with the step of reaction involving the use of a titanium compound. Accordingly, these adducts are reacted with the TiX n (OR ) 4 - n compound (or possibly mixtures thereof) mentioned above which is preferably titanium tetrachloride.
• the reaction with the Ti compound can be carried out by suspending the adduct in TiC (generally cold) the mixture is heated up to temperatures ranging from 80- 130°C and kept at this temperature for 0,5-2 hours.
• the treatment with the titanium compound can be carried out one or more times. Preferably it is repeated twice. It can also be carried out in the presence of an electron donor compound as those mentioned above.
• the solid is recovered by separation of the suspension via the conventional methods (such as settling and removing of the liquid, filtration, centrifugation) and can be subject to washings with solvents.
• the washings are typically carried out with inert hydrocarbon liquids, it is also possible to use more polar solvents (having for example a higher dielectric constant) such as halogenated hydrocarbons.
• the so obtained solid intermediate can also undergo a post-treatment with particular compounds suitable to impart to it specific properties. As an example, it can be subject to a treatment with a reducing compound for example an Al-alkyl compound, in order to lower the oxidation state of the titanium compound contained in the solid.
• Another example of treatment that can be carried out on the intermediate is a pre- polymerization step.
• the pre- pofymerization step can be carried out at temperatures from 0 to 80°C, preferably from 5 to 70°C, in the liquid or gas phase.
• the pre-polymerization of the intermediate with ethylene or propylene in order to produce an amount of polymer ranging from 0.5 to 20 g per gram of intermediate is particularly preferred.
• the pre-polymerization is carried out with the use of a suitable coatalyst such as organoaluminum compounds that can also be used in combination with one or more external donors that are below discussed in detail.
• a suitable coatalyst such as organoaluminum compounds that can also be used in combination with one or more external donors that are below discussed in detail.
• the intermediate product is then brought into contact with the ED compound under conditions able to fix on the solid an effective amount of donor. Due to the high versatility of this method, the amount of donor used can widely vary. As an example, it can be used in molar ratio with respect to the Ti content in the intermediate product ranging from 0.5 to 20 and preferably from 1 to 10. Although not strictly required the contact is typically carried out in a liquid medium such as a liquid hydrocarbon. The temperature at which the contact takes place can vary depending on the nature of the reagents.
• this contact step can last from 10 minutes to 10 hours more frequently from 0.5 to 5 hours. If desired, in order to further increase the final donor content, this step can be repeated one or more times.
• the solid is recovered by separation of the suspension via the conventional methods (such as settling and removing of the liquid, filtration, centrifugation) and can be subject to washings with solvents.
• the washings are typically carried out with inert hydrocarbon liquids, it is also possible to use more polar solvents (having for example a higher dielectric constant) such as halogenated or oxygenated hydrocarbons.
• the so obtained solid can undergo a post-treatment with particular compounds suitable to impart to it specific properties.
• a treatment with a reducing compound for example an AJ-alkyl compound in order to lower the oxidation state of the titanium compound contained in the solid. It has been already described that various donors in a wide range of amounts in respect of the titanium content can be used in the process of the invention.
• All the catalysts obtained generally show good performances in particular in the homopolymerization of ethylene and in its copolymerization with C3-C10 alpha olefins in order to produce ethylene alpha olefin copolymers containing up to 20%mol of alpha olefin.
• Particularly interesting are the catalyst components comprising a Ti compound and an electron donor (ED) selected from alcohol, ketones, amines, amides, nitriles, alkoxysilanes, aliphatic ethers, and esters of aliphatic carboxylic acids supported on Mg dichloride, in which the ED/Ti molar ratio ranges from 1.5 to 3.5 and the Mg/Ti molar ratio is higher than 5.5.
• ED electron donor
• the ED/Ti molar ratio preferably ranges from 2 to 3.4 and more preferably from 2.2 to 3.3.
• the Mg/Ti ratio ranges from 7 to 110,more preferably from 8 to 80 and particularly from 8 to 50.
• Preferred donors are those mentioned above.
• the aliphatic ethers and particularly the C2-C20 aliphatic ethers are also preferred.
• the cyclic ethers preferably having 3- 5 carbon atoms such as tetrahydrofurane (THF) or dioxane are especially preferred. Excellent results have been obtained with the use of esters like ethylacetate as ED compound.
• the catalysts having the sad composition which are also pre-polymerized are also preferred.
• the solid catalyst components according to the present invention are converted into catalysts for the polymerization of olefins by reacting them with organoaluminum compounds according to known methods.
• a catalyst for the polymerization of olefins CH 2 CHR, in which R is hydrogen or a hydrocarbyl radical with 1-12 carbon atoms, comprising the product of the reaction between:
• the alkyl- Al compound can be preferably selected from the trialkyl aluminum compounds such as for example trimethylaluminum (TMA), triethylaluminum (TEAL) , triisobutylaluminum (TIBA), 1ri-n-butylaluminum, tri-n-hexylaluminum, tri-n- octylaluminum.
• TMA trimethylaluminum
• TEAL triethylaluminum
• TIBA triisobutylaluminum
• 1ri-n-butylaluminum tri-n-hexylaluminum
• tri-n- octylaluminum trimethylaluminum halides and in particular alkylaluminum chlorides
• DEC diethylaluminum chloride
• DMAC dimethylaluminum chloride
• the external electron donor compound can be equal to or different from the ED used in the solid catalyst component.
• it is selected from the group consisting of ethers, esters, amines, ketones, nitriles, silanes and mixtures of the above.
• it can advantageously be selected from the C2-C20 aliphatic ethers and in particulars cyclic ethers preferably having 3-5 carbon atoms cyclic ethers such as tetrahydrofurane, dioxane.
• the electron donor compound can also be advantageously selected from silicon compounds of formula Ra Rb Si(OR ) c , where a and b are integer from 0 to 2, c is an integer from 1 to 3 and the sum (a+b+c) is 4; R , R , and R , are alkyl, cycloalkyl or aryl radicals with 1-18 carbon atoms optionally containing heteroatoms. Particularly preferred are the silicon compounds in which a is 0, c is 3, R is a branched alkyl or cycloalkyl group, optionally containing heteroatoms, and R is methyl. Examples of such preferred silicon compounds are cyclohexyltrimethoxysilane, t-butyltrimethoxysilane and thexyltrimethoxysilane.
• the above mentioned components (a)-(c) can be fed separately into the reactor where, under the polymerization conditions can exploit their activity. It constitutes however a particular advantageous embodiment the pre-contact of the above components, optionally in the presence of small amounts of olefins, for a period of time ranging from 0.1 to 120 minutes preferably in the range from 1 to 60 minutes.
• the pre-contact can be carried out in a liquid diluent at a temperature ranging from 0 to 90°C preferably in the range of 20 to 70°C.
• the so formed catalyst system can be used directly in the main polymerization process or alternatively, it can be pre-polymerized beforehand especially if a prepolymerization of the intermediate solid was not carried out.
• a pre-polymerization step is usually preferred when the main polymerization process is carried out in the gas phase.
• the pre-polymerization step can be carried out at temperatures from 0 to 80°C, preferably from 5 to 70°C, in the 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 or propylene in order to produce an amount of polymer ranging from 0.5 to 20 g per gram of catalyst component is particularly preferred.
• the pre-polymerized catalyst component can also be subject to a further treatment with a titanium compound before being used in the main polymerization step. In this case the use of TiCl 4 is particularly preferred.
• the reaction with the Ti compound can be carried out by suspending the prepolymerized catalyst component in the liquid Ti compound optionally in mixture with a liquid diluent; the mixture is heated to 60-120°C and kept at this temperature for 0.5-2 hours.
• gas-phase processes wherein it is possible to use the catalysts of the invention are described in WO 92/21706, USP 5,733,987 and WO 93/03078. These processes comprise a pre-contact step of the catalyst components, a pre-polymerization step and a gas phase polymerization step in one or more reactors in a series of fluidized or mechanically stirred bed.
• C1-C10 hydrocarbon group up to forming amounts of polymer from about 0.1 up to about 1000 g per gram of solid catalyst component (a); and (iii) polymerizing in the gas-phase ethylene, or mixtures thereof with ⁇ -olefins
• CH 2 CHR in which R is a hydrocarbon radical having 1-10 carbon atoms, in one or more fluidized or mechanically stirred bed reactors, in the presence of the product coming from (i) or (ii).
• the catalysts of the present invention are particularly suitable for preparing linear low density polyethylenes (LLDPE, having a density lower than 0.940 g/cm ) and very-low-density and ultra-low-density polyethylenes (NLDPE and ULDPE,
• 3 3 having a density lower than 0.920 g/cm , to 0.880 g/cm ) consisting of copolymers of ethylene with one or more alpha-olefins having from 3 to 12 carbon atoms, having a mole content of units derived from ethylene of higher than 80%.
• polyolefin products including, for example, high density ethylene polymers (HDPE, having a density higher than 0.940 g/cm ), comprising ethylene homopolymers and copolymers of ethylene with alpha-olefins having 3-12 carbon atoms; elastomeric copolymers of ethylene and propylene and elastomeric terpolymers of ethylene and propylene with smaller proportions of a diene having a content by weight of units derived from ethylene of between about 30 and 70%; isotactic polypropylenes and crystalline copolymers of propylene and ethylene and/or other alpha-olefins having a content of units derived from propylene of higher than 85% by weight; impact resistant polymers of propylene obtained by sequential polymerization of propylene and mixtures of propylene with ethylene, containing up to 30% by weight of ethylene; copolymers of propylene and 1-but
• the properties are determined according to the following methods:
• Fraction soluble in xylene The solubility in xylene at 25°C was determined according to the following method: About 2.5 g of polymer and 250 ml of o-xylene were placed in a round-bottomed flask provided with cooler and a reflux condenser and kept under nitrogen. The mixture obtained was heated to 135°C and was kept under stirring for about
• ⁇ -olefins higher than 1-butene were determined via frifra-Red analysis.
• Determination of CI has been carried out via potentiometric titration.
• a magnesium chloride and alcohol adduct containing about 3 mols of alcohol was prepared following the method described in example 2 of USP 4,399,054, but working at 2000 RPM instead of 10000 RPM.
• Adducts containing decreasing amounts of alcohol (47 %wt, 35 %wt, 25 %wt and 15
• %wt were prepared via a thermal treatment, under nitrogen stream, over a temperature range of 50-150 °C.
• a 4.5 liter stainless-steel autoclave equipped with a magnetic stirrer, temperature and pressure indicators, feeding line for ethylene, propane, 1-butene, hydrogen, and a steel vial for the injection of the catalyst, was purified by fluxing pure nitrogen at 70°C for 60 minutes. It was then washed with propane, heated to 75°C and finally loaded with 800 g of propane, 1-butene (amount as reported in table 2 and 4), ethylene (7.0 bar, partial pressure) and hydrogen (as in table 2 and 4).
• a series of catalyst components was prepared using different electron donor (ED) compounds.
• the catalysts were prepared using spherical MgCb(EtOH) adducts, prepared according to the procedure described above containing 25%wt. of EtOH, that were first treated with TiCU for preparing the intermediate according to the procedure disclosed above and then contacted, according to the general procedure, with the specific ED compound used in the feed ratio reported in Table 1.
• Example 15 The so obtained catalysts were then used in the copolymerization of ethylene carried out according to the general procedure reported above and under the specific conditions listed in Table 2 which also contain the data relating to the characterization of the polymer.
• Examples 13-14 The catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as electron donor with the difference that the molar feed ratio ED/Ti was 8, 4 and 1 respectively.
• the so obtained catalysts were then used in the copolymerization of ethylene carried out according to the general procedure reported above and under the specific conditions listed in Table 4 which also contain the data relating to the characterization of the polymer.
• Example 15 The so obtained catalysts were then used in the copolymerization of ethylene carried out according to the general procedure reported above and under the specific conditions listed in Table 4 which also contain the data relating to the characterization of the polymer.
• a solid intermediate prepared according to the general procedure was injected into an autoclave and kept at 30°C stirring in anhydrous hexane (the concentration of the solid was 40g/L) under nitrogen atmosphere.
• An amount of propylene equal to 0.7 times the initial quantity of the solid was then slowly fed with a rate suitable to keep the temperature constant at 30°C. After 30 minutes the polymerization was stopped.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the temperature at which the contact took place was 0°C.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the contact was carried out at 100°C in heptane instead of hexane.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the contact was carried out in toluene instead of hexane.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the contact step was carried out for two times. The first one was carried out at AcOEt/Ti feed molar ratio of 1 for 30 minutes, in the second, carried out after having washed the solid with hexane, the AcOEt/Ti feed molar ratio was 4 and the contact lasted 2.5 hours.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the ED contact step was carried out for 1 hour.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the ED contact step was carried out for 2 hours.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that the ED contact step was carried out for 5 hours.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the solid intermediate prepared according to the general procedure was stirred in anhydrous heptane, at 90°C (the concentration of the solid was 40g/L) with aluminium diethyl monochloride (DEAC),under nitrogen atmosphere, using DEAC at a molar Al/Ti ratio of 10. After 1 hour the stirring was discontinued, the solid product was allowed to settle and the supernatant liquid was siphoned off. A second DEAC treatment in the same conditions as the previous one was then performed. The solid was washed once with anhydrous heptane at 90 °C and twice with anhydrous hexane at room temperature.
• DEAC aluminium diethyl monochloride
• Example 25 The characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 using AcOEt as ED with the difference that in the preparation of the solid intermediate the TiCU treatment was performed at 100 °C instead of 130 °C and a second TiCU treatment at 100 °C (30 minutes) was inserted prior to the washing steps. (Ti 1.9%wt; Mg 19.4%wt). The characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• the catalyst was prepared according to the same procedure disclosed in Examples 1-12 with the difference that in the ED contact step the ED was constituted by a AcOEt/THF mixture (1/1 mol mol). The total ED/Ti molar ratio was equal to 4. The characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4.
• a MgCb precursor was prepared by following the procedure described in example 1(a) of USP 4,220,554.
• the so obtained solid was then treated with TiCU in order to prepare the solid intermediate, in accordance with the general procedure, with the difference that the TiCU treatment was performed at 120 instead of 130 °C and further two TiCU treatments at 120°C (30 minutes) were inserted prior to the washing steps.
• the contact step with AcOEt was carried out according to the general procedure.
• the characteristics of the catalyst component are reported in Table 3 and the results of the copolymerization are reported in Table 4. Examples 28-30
• the catalyst components were prepared according to the same procedure disclosed in Examples 1-13 using AcOEt as electron donor with the difference that the starting spherical MgCb(EtOH) adducts had an alcohol content by weight of 47.3%, 35%, and 14.3% respectively.
• the characteristics of the catalyst components are reported in Table 3 and the results of the copolymerization are reported in Table 4.

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