Component formalising catalyst, process for its production, the catalyst for polymerization of olefins and polymerization of olefins using it

 

(57) Abstract:

The present invention relates to components formalising catalyst for polymerization of olefins CH2=CHR, where R represents a hydrogen atom or a C1-C12alkyl group, the catalysts derived from them, and their use in the polymerization of the above-mentioned olefins. Described component formalising catalyst containing a solid catalyst component containing Ti, Mg, halogen and an electron-donating compound capable of getting under standard conditions of polymerization of homopolymer propylene, characterized by the degree of insolubility in xylene at 25 ° C, exceeding 90%, which are used in the reaction of obtaining the prepolymer of ethylene carried out to such an extent that the amount of ethylene prepolymer comes to 100 g per 1 g of the aforementioned solid catalyst component, and the specified electron-donating compound is an internal donor is selected from simple 1,3-diesters. Also described is a method of obtaining a component formalising catalyst, the catalyst containing the component formalising catalyst connection alkylamine and, optionally, one or more elektronodonornogo catalytic activity, the high rate of isotacticity, aging resistance. 4 N. and 22 C.p. f-crystals, 4 PL.

The present invention relates to the components of the catalyst for polymerization of olefins CH2=CHR, where R represents a hydrogen atom or a hydrocarbon radical containing 1-12 carbon atoms, catalysts derived from them, and their use in the polymerization of the above-mentioned olefins.

In particular, the components of the catalyst of the present invention is very well suited to obtain a crystalline (co)polymers of propylene in the processes (co)polymerization in the gas phase, in suspension or in bulk.

The components of the catalyst, providing a high yield of the polymerization of olefins, in particular propylene, known from the prior art. In the General case they are obtained by applying dihalogenide magnesium compounds of titanium and electron-donating compounds as substances that control the selectivity of the reaction. The aforementioned components of the catalyst are then used together with alkylamines and, optionally, other donor (external) connection in the stereospecific polymerization of propylene. Depending on the type used donor electronicstore must be able to obtain the polypropylene (co)polymer, with the rate of isotacticity expressed in terms of insolubility in xylene greater than 90%.

The aforementioned components of the catalyst and catalysts derived from them, are mostly used on installations for the (co)polymerization of propylene, proceeding as in the liquid phase (suspension or in bulk) and in the gas phase. However, the use of catalyst components as such are not fully satisfactory. Indeed, when the installation is operated with the components of the catalyst as such, there are such problems as the formation of a polymer with irregular morphology and, in particular, very small particles, low bulk density and low activity of the catalyst.

In order to resolve these problems, there may be included an additional production line formation of the prepolymer, in which under controlled conditions is formed forprimary catalyst thereby to obtain forprimary catalyst having a good morphology. After terpolymerization catalysts also increase your stamina so that the tendency to their destruction in the conditions of polymerization decreases. Consequently, the reduced and also obrazovati of the final polymers. The use of an additional production line, however, makes the operation and design of the installation more difficult and costly; therefore, in some cases it is desirable to avoid.

One of the alternative solutions is the method consisting in applying at mount directly formalising catalyst, which can be obtained in another setting. This solution requires you to obtain formalising catalyst that meet certain requirements, such as ease of access and work with it, the ease of handling of resources, the lack of a minimum decrease of activity with time (aging), preferably in combination with basic high activity.

U.S. patent No. 5641721 describes a method of obtaining formalising catalyst comprising a stage (i) obtain pronatalistic the result of applying the compound of the transition metal on a suitable carrier, (ii) mixing the composition mentioned pronatalistic viscous substance and then terpolymerization mentioned composition pronatalistic with the monomer in the presence of the aforementioned viscous substances. The viscous material has a viscosity in the range from 1000 to 15000 CPs (from 1000 to 15000 MPa·s), Tortora does not change after 5 months, its selectivity, apparently, is reduced. Moreover, terpolymerization in this viscous substance makes getting formalising catalyst complex and in addition, has the effect of low activity of the catalyst.

Surprisingly it was found that as a result of receiving terpolymerization with a specific monomer it is possible to obtain a catalyst for polymerization of olefins, which would have a high catalytic activity, would allow to achieve a high rate of isotacticity and which would not adversely impact the aging process.

Therefore, the object of the present invention is a component formalising catalyst for the (co)polymerization of olefins CH2=CHR, where R represents a hydrogen atom or C1-C12-alkyl group, characterized in that it comprises a solid catalyst component containing Ti, Mg, halogen and an electron-donating compound, which would produce under standard conditions of polymerization of homopolymer propylene, characterized by the degree of insolubility in xylene at 25 ° C, exceeding 90%, which will terpolymeric with ethylene so that the amount of ethylene prepolymer comes to 100 g per 1 g mentioned predpochtitelno mentioned a number less than 5 g per 1 g of solid catalyst component.

In particular, the components of the catalyst include a compound of titanium, having at least a link Ti-halogen, and the above-mentioned electron-donating compound, applied to the halide MD. The magnesium halides, preferably MgCl2in the active form used as a carrier for catalysts of the Ziegler-Natta, widely known from the patent literature. U.S. patent No. 4298718 and 4495338 were the first who described the use of these compounds in the processes of catalysis Ziegler-Natta. Of these patents, it is known that dihalogenide magnesium in the active form used as the carrier or joint carrier in the catalyst components for the polymerization of olefins, characterized by x-ray spectra in which the most intense diffraction line which appears in the spectrum of active halide, reduced in intensity, and instead there are halo, the maximum intensity of which is shifted towards smaller angles relative to the angle the more intense lines.

The preferred titanium compounds used in the catalyst component of the present invention, represent TiCl4and TiClB>ywhere n represents the valence of titanium and y is a number between 1 and n.

The internal electron-donor compound can be selected from esters, ethers, amines and ketones. Preferably it is selected from alkyl, cycloalkyl or aryl esters of monocarboxylic acids such as benzoic acid, or polycarboxylic acids, such as phthalic or malonic acid, while the aforementioned alkyl, cycloalkyl or aryl groups have from 1 to 18 carbon atoms. In addition, it can also be selected from simple 1,3-diesters described by formula (I)

where RI, RII, RIII, RVI, RVand RVIidentical or different, represent a hydrogen atom or hydrocarbon radicals having from 1 to 18 carbon atoms, and RVIIand RVIIIidentical or different, have the same value asI-RVIexcept that they cannot be hydrogen; one or more of the groups RI-RVIIImay be associated with the formation of the loop. Particularly preferred are simple 1,3-diesters in which RVIIand RVIIIselected from C1-C4-alsoat, diisobutylphthalate and 9,9-bis(methoxymethyl)fluorene. However, as explained above, the internal electron-donor compound should be selected so that was the final solid catalyst component which is able to provide under standard polymerization test, described below, of a propylene homopolymer having a degree of insolubility in xylene at 25 ° C, exceeding 90%.

Preparation of solid catalyst component can be carried out in accordance with a number of ways. In accordance with one of these methods, the magnesium dichloride in an anhydrous state, the connection of titanium and electron-donating compound described by formula (I), milled together under conditions in which activation of the magnesium dichloride. Thus obtained product can be treated one or more times with an excess of TiCl4at a temperature in the range from 80 to S. After this processing are performed washing the hydrocarbon solvents up until the chloride ions will not disappear. In accordance with another method, the product obtained by co-grinding the magnesium chloride in an anhydrous state, the titanium compounds and electrondonor orotan and the like, the processing is carried out for a time ranging from 1 to 4 hours at temperatures ranging from -40 ° C up to the boiling point of the halogenated hydrocarbon. The resulting product then in the General case washed using an inert hydrocarbon solvent such as hexane.

In accordance with another method, magnesium dichloride is pre-activated by well known methods and then treated with excess TiCl4at a temperature in the range from 80 to S in the presence of electron-donating compounds. Processing using iCl4is repeated, and the solid phase is washed with hexane to remove unreacted TiCl4.

The next method involves the reaction between alcoholate or chloralkali magnesium (in particular chloralkali received in accordance with U.S. patent No. 4220554) and excess TiCl4in the presence of electron-donating compound (I) at a temperature approximately in the range from 80 to 120C.

Particularly preferred solid component of catalyst obtained by the reaction of the titanium compounds described by the formula Ti(OR)n-yXywhere n represents the valence of titanium and y is a number between 1 and n, preferably TiCl4with the adduct described by formula MgCl2·d, where p is the product can be suitably obtained with a spherical form by mixing alcohol and magnesium chloride in the presence of an inert hydrocarbon, not mixed with the adduct, the procedure is performed under conditions of agitation at a temperature of melting of the adduct (100-130C). Thereafter, the emulsion is quickly quenched, thereby stimulating the curing of the adduct in form of spherical particles. Examples of spherical adducts obtained in accordance with this procedure are described in U.S. patent No. 4399054. Thus obtained adduct can be used directly for the reaction with the compound of Ti or it may be first subjected to a thermally controlled dealcoholizing (80-130C) to obtain an adduct in which the number of moles of alcohol in General less than 3, preferably in the range from 0.1 to 2.5. Dealcoholizing adduct then suspendered cold TiCl4(in General, if you 0C); the mixture is heated to 80-130C and maintained at this temperature for 0.5-2 hours. Processing using TiCl4may be performed one or more times. The internal electron-donor compound can be added during processing using TiCl4. Processing electron-donating compound may be repeated one or more times.

Obtaining catalyst components in spherical form opisyal above characterized by the presence of surface area (according to the method of Brunauer-Emmett-teller) in General in the range from 20 to 500 m2/g and preferably in the range from 50 to 400 m2/g, and more preferably in the range from 100 to 400 m2/g; total porosity (according to the method of Brunauer-Emmett-teller) exceeding 0.2 cm3/g, preferably between 0.2 and 0.6 cm3/g, and more preferably between 0.3 and 0.5 cm3/year Porosity (mercury method) due to the presence of pores having a radius of up to 10 , generally is in the range from 0.3 to 1.5 cm3/g, preferably from 0.45 to 1 cm3/,

The following method of obtaining a solid component of catalyst of the present invention includes halogenoalkane connection dihydrogenmonoxide magnesium, such as dialkoxy or diarylike magnesium, using a solution of TiCl4in aromatic hydrocarbon (such as toluene, xylene, etc., at temperatures in the range from 80 to 130C. Processing using TiCl4in the solution of aromatic hydrocarbon may be repeated one or more times, and the internal electron-donor compound added during one or more of such treatments. In LK such or same alternatively, it can be obtained “on the spot” as a result of using an appropriate predecessor, possessing the ability to transform into the desired electron-donor compound by means, for example, of known chemical reactions such as esterification, transesterification, etc., In the General case, the internal electron-donor compound used in molar ratio to the MgCl2in the range from 0.01 to 1, preferably from 0.05 to 0.5.

As explained above, the catalytic component of the prepolymer can be obtained by obtaining the prepolymer of ethylene using a solid catalyst component. Obtaining prepolymer is usually carried out in the presence of Al-alkyl compounds.

The alkyl-Al compound (C) preferably is selected among compounds trialkylamine, such as, for example, triethylamine, triisobutylaluminum, tri-n-butylamine, tri-n-hexylamine, tri-n-octylamine. It is also possible to use mixtures of trialkylaluminium with halides alkylamine, hydrides alkylamine or sesquichloride alkylamine, such as AlEt2Cl and Al2Et3Cl3.

It is found that particularly advantageous provoke number can be to obtain the molar ratio Al/Ti in the range from 0.0001 to 50, preferably in the range of from 0.001 to 10, and more preferably in the range of from 0.01 to 1.

In addition, it was found advantageous to terpolymerization in the absence of external donor compounds.

Terpolymerization can be carried out in the liquid phase (suspension or solution) or in the gas phase at temperatures in General smaller than 80 ° C, preferably in the range from -20 to 50C. In addition, it is preferably carried out in a liquid diluent, in particular selected from liquid hydrocarbons. Among them, preferred pentane, hexane and heptane.

As already explained, thus obtained components formalising catalyst can be used in the polymerization of olefins, in particular propylene, making it possible to provide a high activity of the catalyst and obtain polymers with high stereoregularity, high bulk density and very good morphology, thus demonstrating its special suitability for liquid-phase (in bulk or in suspension) and gas-phase processes. In addition, as demonstrated in the examples are solved and the problems associated with starenka time in a few months. Accordingly, the components of the catalyst of the present invention particularly suitable for use in installations for liquid-phase or gas-phase polymerization of olefins, functioning without the production line obtain prepolymer.

In particular, the above-mentioned polymerization processes of olefins can be carried out in the presence of a catalyst containing (A) component formalising catalyst; (C) Al-alkyl compound of this type, as was described above, and, optionally, (C) one or more electron-donor (external) connections.

The latter may be of the same type or it can be different from the internal donor, as described above. Suitable external electron-donor compounds include silicon compounds, ethers, esters, amines, heterocyclic compounds, in particular 2,2,6,6-tetramethylpiperidine, ketones and simple 1,3-diesters described General formula (I) above.

Another class of preferred external donor compounds is that class of silicon compounds described by the formula, R5aR6bSi(OR7), where a and b represent integers in the range from 0 to 2, p represents samocinny, cycloalkyl or aryl radicals with 1-18 carbon atoms optionally containing heteroatoms. Particularly preferred are the silicon compounds in which a is 1, b is 1, is 2, at least one of R5and R6selected from branched alkyl, cycloalkyl or aryl groups with 3-10 carbon atoms, optionally containing heteroatoms, a R7represents a C1-C10alkyl group, in particular methyl. Examples of such preferred silicon compounds are methylcyclohexanecarboxylic, diphenylmethylsilane, methyl-tert-butyldimethylsilyl, dicyclopentadienyliron, 2-ethylpiperidine-2-tert-butyldimethylsilyl and 1,1,1-cryptochrome-2-ethylpiperidine-dimethoxysilane. In addition, also preferred silicon compounds in which a is 0, C is 3, R6represents a branched alkyl or cycloalkyl group, optionally containing heteroatoms, and R7represents a methyl group. Examples of such preferred silicon compounds are cyclohexyltrichlorosilane, tert-butyldimethylsilyl and hexyltrimethoxysilane.

In Casati, external donor compound is selected from the class t-amoxicillinsee is the most preferred. In addition to this can be used a mixture of this donor with others and, in particular, with the donor selected from the class of compounds of silicon. In this case, the most preferred methylcyclohexanecarboxylic and dicyclopentadienyliron.

Electron-donating compound (C) is used in such quantity that could molar ratio between alumoorganic compound and the above-mentioned electron-donating compound in the range from 0.1 to 500, preferably in the range from 1 to 300, and more preferably from 3 to 100.

The above-described polymerization process can be carried out under the conditions of polymerization, known to experts in the relevant field. Accordingly, the polymerization in General carried out at temperatures in the range from 20 to 120C, preferably in the range from 40 to 80C. If the polymerization is carried out in the gas phase, the working pressure in the General case is in the range from 0.5 to 10 MPa, preferably in the range from 1 to 5 MPa. When polymerization in the mass of the working pressure in the General case is erization processes (liquid-phase or gas-phase polymerization) components, forming a catalyst (A), (b) and, optionally, (C) can be pre-entered in contact with each other before adding them to the polymerization reactor. Mentioned are preliminary contact can be carried out in the absence of the polymerized olefin or, optionally, in the presence of the above-mentioned olefin in the amount of up to 3 g per 1 g of solid component of catalyst. The components forming the catalyst can be introduced into contact with each other when using a liquid inert hydrocarbon solvent such as propane, n-hexane or n-heptane, at a temperature of less than about 60, and preferably in the range of about from 0 to 30 ° C over a period of time ranging from 10 seconds to 60 minutes.

If you are using a process gas-phase polymerization, it may be carried out in accordance with known methods, using one or more reactors with fluidized or mechanically mixed layer. Inert fluids such as nitrogen or lower hydrocarbons such as propane, can be used as pseudoviruses component, and in order to improve the heat transfer inside Reiki, includes introduction to the reactor liquids, optionally in a mixture with the gas. Preferably the fluids are fresh or prepared according to the standard of the monomers. Such techniques are described, for example, in patents EP-A-89691, EP-A-241947, US 5352749, W0 94/28032 and EPA-695313.

The following examples are given to illustrate the present invention without limiting it.

Examples

Characterization

The determination of the degree of insolubility in xylene

2.5 g of polymer was dissolved in 250 ml of o-xylene under stirring at C for 30 min, then the solution was cooled to 25 ° C, and after 30 minutes the insoluble polymer was filtered. The resulting solution was evaporated in a stream of nitrogen, and the solid residue was dried and weighed to determine the percentage of soluble polymer and then, by difference, the magnitude of the degree of insolubility in xylene in %.

General procedure standard test for the polymerization of propylene.

Was used a 4-liter steel autoclave, equipped with stirrer, pressure gauge, thermometer, feed system catalyst lines for feeding monomer and thermostatic jacket. In the reactor is Oh, to obtain the molar ratio Al/donor equal to 20. In addition, were added to 3.2 l of propylene and 1.5 liters of hydrogen. The system under stirring, they were heated to 70 C for 10 min and kept at these conditions for 120 minutes At the end of the polymerization, the polymer was extracted after removal of unreacted monomers and dried under vacuum.

Determination of melt index

ASTM D 1238 condition “L”.

Examples 1-2 and comparative example 3

Obtaining a solid component of catalyst

In chetyrehosnuju round flask of 500 ml, purged with nitrogen, was placed 250 ml of TiCl4at 0C. With stirring, was added 10 g microspheroidal gl2·2H5HE, containing about 54 wt.% the alcohol. The flask was heated to 40C, after this was introduced 6 mmol of diisobutylphthalate. The temperature was increased to 100C, and it was kept at this level for two hours, after which the stirring was discontinued, the solid product was left to settle and the supernatant liquid was drained by the siphon.

Processing using TiCl4was repeated and the resulting solid phase was washed 6 times with anhydrous hexane (6100 ml) at 60C and after Timiriazev propylene are given in table. 1.

Terpolymerization ethylene

The components of the catalyst obtained in accordance with the above procedure, were terpolymerization with ethylene under the conditions shown in table. 2. In comparative example 4 obtaining prepolymer was not conducted.

Polymerization of propylene

Received terpolymerization the catalyst was then used for the polymerization of propylene is carried out in a pilot plant for polymerization in bulk under the following conditions:

Al/catalyst (wt. ratio): 8.

Al/donor (wt. ratio): 6.

Donor/catalyst (wt. ratio): 1,3.

Time (min): 80.

Temperature (C): 70.

The results are shown in table. 3.

Example 4-5 and comparative example 6

The receiving component catalyst

The components of the catalyst were obtained in accordance with the procedure of example 1, but using ethylbenzoic instead of diisobutylphthalate. The properties of the catalyst components and the results of the procedure to test for propylene polymerization are shown in table. 1.

Terpolymerization ethylene

The components of the catalyst obtained in accordance with the positive example 6 obtaining prepolymer was not conducted.

Polymerization of propylene

The obtained catalyst component was then used for propylene polymerization, which was carried out in pilot plant for polymerization in bulk under the following conditions:

Al/catalyst (wt. ratio): 4,6.

Al/donor (wt. ratio): 1,4.

Donor/catalyst (wt. ratio): 3,2.

Time (min): 80.

Temperature (C): 70.

using p-ethoxyethylacetate as an external donor. The results are shown in table. 3.

Example 7 and comparative example 8

The components of the catalyst were obtained in accordance with the method of example 4, but using 9,9-bis(methoxymethyl)fluorene instead of ethylbenzoic.

The properties of the catalyst components and the results of the propylene polymerization test are given in table. 1.

Terpolymerization ethylene

The components of the catalyst obtained in accordance with the above procedure, were terpolymerization with ethylene under the conditions shown in table. 2. In comparative example 8 terpolymerization not implemented.

Polymerization of propylene

Received terpolymerization catalyst after that would the SSE under the following conditions:

Al/catalyst (wt. ratio): 13,7.

Time (min): 80.

Temperature (C): 70.

without using an external donor. The results are shown in table. 3.

The evaluation of the properties associated with aging

The components of the catalyst obtained in accordance with examples 4 and 5 were tested for the polymerization of propylene in order to evaluate their properties associated with aging. The first test was conducted after receipt of the prepolymer, and the subsequent testing was conducted after 120 days. All test were conducted in accordance with the General standard procedure, but using p-ethoxyethylacetate as an external donor in such a quantity to obtain a molar ratio Al/donor 1.8. The results are shown in table. 4.

1. Component formalising catalyst for polymerization of olefins CH2=R, where R represents a hydrogen atom or a C1-C12is an alkyl group, characterized in that it comprises a solid catalyst component containing compound of titanium with at least one link Ti-halogen and an electron-donating compound deposited on a Gal who Jena, with the degree of insolubility in xylene at 25 ° C, exceeding 90%, while mentioned solid catalyst component will terpolymeric with ethylene so that the amount of ethylene prepolymer comes to 100 g per 1 g of solid component of catalyst, and the specified electron-donating compound is an internal donor is selected from simple 1,3-diesters described by formula (I):

where RI, RII, RIII, RIV, RVand RVIidentical or different, represent a hydrogen atom or hydrocarbon radicals having 1 to 18 carbon atoms, and RVIIand RVIIIidentical or different, have the same meaning as RI-RVIexcept that they cannot be hydrogen; one or more of the groups RI-RVIIImay be associated with the formation of the loop.

2. Component of the catalyst under item 1, characterized in that the amount of the ethylene polymer is less than 15 g per 1 g of solid catalyst component.

3. Component of the catalyst under item 2, characterized in that the amount of the ethylene polymer is less than 5 g per 1 g of solid catalyst component.

4. Component of the catalyst under item 1, wherein t is electron-donating compound, put on a Mg halide in active form.

5. Component of the catalyst according to any one of paragraphs. 1-4, characterized in that the solid catalyst component produced by the reaction of the titanium compounds described by the formula Ti(OR)n-yXywhere n represents the valence of titanium and y is a number between 1 and n, with the adduct described by formula gl2·R, where p is a number between 0.1 and 6, and R represents a hydrocarbon radical having 1-18 carbon atoms.

6. Component of the catalyst according to any one of paragraphs. 1-5, characterized in that the compound of titanium is a Til4.

7. Component of catalyst according to p. 6, characterized in that the internal donor is chosen from the group consisting of ethylbenzoic and diisobutylphthalate.

8. Component of catalyst according to p. 7, wherein RVIIand RVIIIselected from C1-C4-alkyl radicals, and group RIII-RIVassociated with the formation of the loop.

9. The method of producing a component formalising catalyst according to one of paragraphs. 1-8 carried out as a result of terpolymerization ethylene in the presence of solid component kata is own by p. 9, wherein the Al-alkyl compound is chosen among compounds trialkylamine and halides alkylamine.

11. The method according to p. 10, characterized in that the Al-alkyl compound selected from triethylaluminum, triisobutylaluminum, Trinh-butylamine, tri-n-hexylamine, tri-n-octylamine.

12. The method according to any of paragraphs. 9-11, characterized in that terpolymerization performed with the use of such quantities of the alkyl-Al compound, to obtain a molar ratio Al/Ti in the range of 0.0001 - 50.

13. The method according to p. 12, characterized in that the molar ratio Al/Ti is in the range 0.001 - 10.

14. The method according to p. 13, characterized in that the molar ratio Al/Ti is in the range from 0.01 to 1.

15. The method according to p. 9, characterized in that terpolymerization carried out in a liquid diluent selected from liquid hydrocarbons.

16. The catalyst for polymerization of olefins CH2=CHR, where R represents a hydrogen atom or a hydrocarbon radical containing 1-12 carbon atoms containing component formalising catalyst according to any one of paragraphs. 1-8, the connection alkylamine and, optionally, one or more electron-donating compound.

17. The catalyst Poinsot.

18. The catalyst p. 17, characterized in that as the external donor is used a mixture of benzoate and compounds of silicon.

19. The catalyst p. 18, characterized in that ethylbenzoic is an internal donor, and p-amoxicillinsee is an external donor.

20. The catalyst p. 18, characterized in that ethylbenzoic is an internal donor, and an external donor comprises a mixture of p-ethoxyethylacetate and dicyclopentadienyliron.

21. The method of polymerization of olefin CH2=CHR, where R represents a hydrogen atom or a hydrocarbon radical containing 1-12 carbon atoms, carried out in the presence of a catalyst containing (A) component formalising catalyst according to one of paragraphs. 1-8; (B) A1-alkyl compound and, optionally, (C) an external donor compound.

22. The method according to p. 21, characterized in that the components forming the catalyst (A), (B) and, optionally, (C) previously come into contact with each other before adding them to the polymerization reactor.

23. The method according to p. 21, characterized in that the olefin is propylene.

24. The method according to p. 21, wherein the external electron donor is chosen from compounds kremniem General formula (I).

25. The method according to p. 24, wherein the external donor is selected from silicon compounds described by the formula, R5aR6bSi(OR7)cwhere a and b represent integers in the range 0 to 2, p is an integer in the range 1 to 3 and the sum (a+b+C) equals 4; R5, R6and R7represent alkyl, cycloalkyl or aryl radicals with 1-18 carbon atoms optionally containing heteroatoms.

26. The method according to p. 25, characterized in that a equals 1, b equals 1, C is 2, at least one of R5and R6is selected from branched alkyl, cycloalkyl or aryl groups with 3-10 carbon atoms, and R7represents a C1-C10is an alkyl group.

 

Same patents:

The invention relates to methods for macromolecular higher poly-alpha-olefins, in particular polyacene, and catalysts for carrying out the method

The invention relates to the components of the catalyst for polymerization of olefins CH2=CHR, where R is hydrogen or a hydrocarbon radical with 1-12 carbon atoms, comprising Mg, Ti, halogen and at least one 1,3-W, which forms complexes with anhydrous magnesium dichloride in an amount of less than 60 mmol per 100 g of MgCl2and without substitution reactions with TiCl4or reacting in the amount less than 50 mol%, and at least one ester of mono - or polycarboxylic acid, and 1,3-diesters selected from compounds of the formula (II)

where the group RIIIidentical or different, represent hydrogen or C1-C18hydrocarbon group; groups of RIVidentical or different, have the same meaning as RIIIexcept that they cannot be hydrogen; each of the groups RIII- RIVmay contain heteroatoms selected from Halogens, N, O, S and Si, and the radicals RVidentical or different, are selected from the group consisting of hydrogen; Halogens, preferably C1 or F; C1-C20alkyl radicals with a straight or branched chain; C3-C20cycloalkyl,6e radicals Rvcan be connected to each other to form a condensed cyclic structures, saturated or unsaturated, optionally substituted, RVIradicals selected from the group consisting of halogen, preferably C1 or F; C1-C20alkyl radicals, linear or branched; C3-C20cycloalkyl, C6-C20aryl, C7-C20alkalinic and C7-C20Uralkalij radicals; the radicals RVand RVIoptionally contain one or more heteroatoms as substitutes for carbon or hydrogen atoms, or both

The invention relates to a component of a solid catalyst for polymerization of olefins CH2=CHR, where R is hydrogen or a hydrocarbon radical with 1-12 carbon atoms, comprising Mg, Ti, halogen and an electron donor selected from substituted succinates formula

The invention relates to a method for producing a catalyst for polymerization of olefins and method of polymerization of olefin monomers with its use

The invention relates to a method (generowania type in a suspension of liquid monomer) obtain ethylene-propylene elastomers (EP) and ternary ethylene-propylene-diene elastomers (EPDM)

The invention relates to methods of producing ultra-high molecular weight polyethylene (UHMWPE), synthesized in powder form in the conditions of suspension polymerization of ethylene in the environment of a hydrocarbon diluent at temperatures of 40-70oWith the use of supported catalysts ziperovich type

The invention relates to methods of producing polymers-olefins, effectively reducing the hydrodynamic resistance of hydrocarbon liquids and can be used for transporting petroleum products in pipelines

The invention relates to a multistage process for the polymerization of olefins of the formula CH2= CHR where R is hydrogen or alkyl, cycloalkyl or aryl group with 1-10 carbon atoms), carried out in two or more reactors

The invention relates to a method of liquid-phase polymerization to obtain a polyolefin elastomer, for acetalization forming cation, to activate metallocene pronatalistic to get the polyolefin elastomer

The invention relates to a new the ethylene copolymer and the method of its production

The invention relates to a method of production of new high-performance immobilized catalyst, and method for the synthesis of Homo - and copolymers of olefins such immobilized catalyst that allows the use of triisobutylaluminum as socializaton and conduct the polymerization at 20-70°C

The invention relates to a method for producing low molecular weight polyisobutylene and may find application in the synthetic rubber industry, and the obtained product can be used as the basis for operations and thickening additives

The invention relates to a method for producing low molecular weight polyisobutylene and may find application in the synthetic rubber industry, and the obtained product can be used as the basis for operations and thickening additives

The invention relates to techniques for polymerization of isobutylene, and the obtained product is used as a thickening additive for lubricating oils for the manufacture of sealants, adhesives and many other purposes

The invention relates to the field of technology of synthetic polymeric materials, in particular to a method for producing low molecular weight polyisobutylenes and polybutene, and may find application in petrochemical industry

The invention relates to a method of improving the strength at the melting of polypropylene, comprising a stage of mixing the polypropylene with at least one PEROXYDICARBONATE; the interaction of these polypropylene and PEROXYDICARBONATE at a temperature of from 150 to 300oWith provided that PEROXYDICARBONATE does not have the form of aqueous dispersions in polar environments, with at least 90 wt

The invention relates to the chemistry of polymers, and to methods of producing stereoregular polypropylene, and can be used in the chemical industry in the manufacture of plastics

The invention relates to a new organoboron compound having catalytic activity, of the formula I

[RjM-Xd-MRj]a-bAc+(I)

in which R are, independently of one another, identical and denote C1-C40alkyl; X is, independently from each other, equal or different and denote C1-C40alkyl; M is, independently of one another, identical or different and denote an element of IIIa, IVa, Va group of the Periodic system of elements, provided that one M is boron, a is a cation of an element Ia, IIa and IIIa groups of the Periodic system of elements, carbene-hydronium - or sulfonyl - cation or compound Quaternary ammonium, and a is an integer from 0 to 10, b is an integer from 0 to 10, C is an integer from 0 to 10 and a = C; d is 1; j is an integer from 1 to 3
Up!