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
  • 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
  • C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
  • C08K13/00—Use of mixtures of ingredients not covered by one single of the preceding main groups, each of these compounds being essential
  • C08K13/02—Organic and inorganic ingredients
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C309/00—Sulfonic acids; Halides, esters, or anhydrides thereof
  • C07C309/63—Esters of sulfonic acids
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F5/00—Compounds containing elements of Groups 3 or 13 of the Periodic Table
  • C07F5/06—Aluminium compounds
  • C07F5/061—Aluminium compounds with C-aluminium linkage
  • C07F5/066—Aluminium compounds with C-aluminium linkage compounds with Al linked to an element other than Al, C, H or halogen (this includes Al-cyanide linkage)
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
  • C07F5/00—Compounds containing elements of Groups 3 or 13 of the Periodic Table
  • C07F5/06—Aluminium compounds
  • C07F5/069—Aluminium compounds without C-aluminium linkages
• • 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
  • C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
  • C08K5/00—Use of organic ingredients
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
  • C08K5/00—Use of organic ingredients
  • C08K5/0091—Complexes with metal-heteroatom-bonds
• • C—CHEMISTRY; METALLURGY
  • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
  • C08K—Use of inorganic or non-macromolecular organic substances as compounding ingredients
  • C08K5/00—Use of organic ingredients
  • C08K5/0008—Organic ingredients according to more than one of the "one dot" groups of C08K5/01 - C08K5/59
  • C08K5/0075—Antistatics

Definitions

• the invention relates to a process for preparing an antistatic for olefin polymerization, a corresponding antistatic and a process for olefin polymerization.
• antistatics are used to avoid electrostatic charging.
• the antistatically acting compounds comprised in these generally comprise organic compounds having polar functional groups such as acid or ester groups, amine or amide groups or hydroxyl or ether groups.
• polar functional groups such as acid or ester groups, amine or amide groups or hydroxyl or ether groups.
• constituents of typical antistatics are polysulfone copolymers, polymeric polyamines, oil-soluble sulfonic acids, polysiloxanes, alkoxyamines, polyglycol ethers, etc.
• metal alkyls are usually used as scavengers in olefin polymerization in order to protect the catalyst from being destroyed by the ever-present traces of polar compounds in the reactor.
• the scavengers react with the impurities before they can have an effect on the catalyst. A satisfactory activity is ensured in this way.
• At least one antistatically acting compound comprising at least one hydrogen atom bound to a nonmetallic heteroatom
• the at least one antistatically acting compound and the at least one metal alkyl are each present in a concentration of at least 0.01% by weight during contacting.
• concentration is based on the sum of the antistatically acting compounds comprising at least one hydrogen atom bound to a nonmetallic heteroatom or the sum of the metal alkyls.
• the concentrations of the antistatic and of the metal alkyl are significantly higher in the process of the invention. This increase in concentration leads to an increase in the rate constant by a number of orders of magnitude, so that essentially complete reaction of the hydrogen atoms bound to a nonmetallic heteroatom in the antistatic, hereinafter also referred to as active hydrogen, is presumably made kinetically possible.
• an antistatically acting compound is a chemical compound which is able to reduce negative or positive electrostatic charges in the reactor. It can be a single chemical compound or preferably also a mixture of a plurality of antistatically acting compounds.
• the at least one antistatically acting compound has at least one hydrogen atom bound to a nonmetallic heteroatom, hereinafter referred to as active hydrogen.
• Heteroatoms can in principle be all nonmetallic heteroatoms which are at least divalent and can therefore not only form a bond to a carbon but can additionally bond to at least one hydrogen atom.
• Preferred nonmetallic heteroatoms are O, N, S and P.
• the at least one antistatically acting compound preferably has an electrical conductivity of at least 0.05 ⁇ S/cm, more preferably at least 0.10 ⁇ S/cm, more preferably at least 0.20 ⁇ S/cm, more preferably 0.50 ⁇ S/cm, particularly preferably 1.0 ⁇ S/cm.
• at least one of the components should have a corresponding conductivity.
• Preferred antistatically acting compounds are those having a molar mass of at least 100 g/mol, more preferably at least 150 g/mol, particularly preferably at least 200 g/mol, with mixtures comprising at least one such antistatically acting compound also being preferred.
• organic antistatically acting compounds with those having at least 5, in particular at least 10, carbon atoms being particularly advantageous.
• the antistatically acting compound preferably has hydrogen-comprising functional groups selected from among -OH, -COOH, -NH 2 , -NHR 1 , -SH, -PH 2 , -PHR 1 and -SO 3 H, where R 1 is an alkyl, aryl, alkylaryl or arylalkyl radical in which one or more carbon atoms may also be replaced by heteroatoms.
• dodecylbenzenesulfonic acid phosphoric acid derivatives such as di(alkoxypolyethoxyethyl)phosphates of the general formula [RO(CH 2 CH 2 O) n J 2 POOM or phytic acid derivatives as disclosed, for example, in EP-A 453116
• cation-active deactivators such as quaternary ammonium salts of the general formula R 1 R 2 R 3 R 4 NX, where X is a halogen atom and R 1 to R 4 are, independently of one another, an alkyl radical, preferably one having at least 8 carbon atoms.
• metal complexes such as the cyanophthalocyanines disclosed in WO 93/24562.
• Particularly useful antistatically acting compounds are nonvolatile nitrogen-comprising compounds such as amines or amides or their salts, in particular oligomeric or polymeric amines and amides.
• examples which may be mentioned are polyethoxyalkylamines or polyethoxyalkylamides of the general formula R 1 N[(R 2 O) m R H(R 3 O) n H] or R 1 CON[(R 2 O) m R ][(R 3 O) n H], where R 1 to R 3 are alkyl radicals, in the case of R 1 preferably alkyl radicals having at least 8 carbon atoms, preferably at least 12 carbon atoms, and n, m are equal to or greater than 1 , as described in DE-A 31 088 43.
• salt mixtures comprising calcium salts of Medialanic acid and chromium salts of N- stearylanthranilic acid, as described in DE-A 3543360, or mixtures of a metal salt of Medialanic acid, a metal salt of anthranilic acid and a polyamine as described in EP-A 636 636.
• polyamines or polyamine copolymers or mixtures of such compounds with further compounds, in particular polymeric compounds are particularly useful antistatically acting compounds.
• suitable nonvolatile polyamines are advantageously obtained from the reaction of aliphatic primary monoamines such as n-octylamine or n-dodecylamine or N-alkyl-substituted aliphatic diamines such as N-n-hexadecyl-1 ,3-propanediamine and epichlorohydrin.
• aliphatic primary monoamines such as n-octylamine or n-dodecylamine or N-alkyl-substituted aliphatic diamines such as N-n-hexadecyl-1 ,3-propanediamine and epichlorohydrin.
• These polyaminopolyols have not only amino groups but also hydroxyl groups.
• An overview of such polyamine copolymers is given in US 3,9
• Polysulfone copolymers are particularly suitable polymers for use together with polyamines or polyamine copolymers.
• the polysulfone copolymers are preferably largely unbranched and are made up of olefins and SO 2 units in a molar ratio of 1 :1.
• An overview of suitable polysulfone copolymers is also given in US 3,917,466.
• 1-Decene polysulfone may be mentioned by way of example.
• Mixtures comprising polysulfone copolymers, a polyamine and a long-chain sulfonic acid are described in US 5026795 and US 4182810.
• the at least one antistatically acting compound comprises a polysulfone copolymer, a polymeric polyamine and an oil-soluble sulfonic acid.
• Mixtures of this type are described, for example, in WO 00/68274 or WO 02/040554. Reaction of these mixtures results, in particular, in the oil-soluble sulfonic acid comprising active hydrogen being converted into a compound which does not comprise any active hydrogen.
• Preferred sulfonic acids are monosubstituted or disubstituted phenylsulfonic or naphthylsulfonic acids.
• the antistatic comprises an oil-soluble metal alkylsulfonate which can be prepared by reacting a metal alkyl with such an oil-soluble sulfonic acid.
• the antistatic particularly preferably further comprises a polysulfone copolymer and a polymeric polyamine.
• metal alkyls are compounds of metals or semimetals with linear or cyclic alkyls, aryls, alkylaryls and/or arylalkyls which are able to react with the active hydrogen of the antistatics. It is also possible to use mixtures of metal alkyls here. Suitable metal alkyls are those of the general formula (I) 1 M G (R 1G ) r G(R 2G ) s G (R 3G )t ⁇ 5 (I)
• M G is Li, Na, K, Be, Mg, Ca, Sr, Ba, boron, aluminum, gallium, indium, thallium, zinc, in particular Li, Na, K, Mg, boron, aluminum or Zn,
• R 1G is hydrogen, Ci-C 10 -alKyl, C 6 -C 15 -aryl, alKylaryl or arylalkyl each having from 1 to 10 carbon atoms in the alkyl radical and from 6 to 20 carbon atoms in the aryl radical,
• R 2G and R 3G are each hydrogen, halogen, C 1 -Ci 0 -SlKyI, C 6 -Ci 5 -aryl, alkylaryl, arylalKyl or alKoxy each having from 1 to 20 carbon atoms in the alkyl radical and from 6 to 20 carbon atoms in the aryl radical, or alKoxy with Ci-C 10 -alKyl or C 6 -Ci 5 -aryl,
• r G is an integer from 1 to 3 and
• s G and t G are integers in the range from 0 to 2, with the sum r G +s G +t G corresponding to the valence of M G ,
• metal alKyls usually not being identical to the activators for the catalysts. It is also possible to use mixtures of various metal alkyls of the formula (I).
• M G is lithium, magnesium, boron or aluminum
• R 1G is d-Czo-alkyl.
• metal alKyls of the formula (I) are methyllithium, ethyllithium, n-butyllithium, methylmagnesium chloride, methylmagnesium bromide, ethylmagnesium chloride, ethylmagnesium bromide, butylmagnesium chloride, dimethylmagnesium, diethylmagnesium, dibutylmagnesium, n-butyl-n-octylmagnesium, n-butyl-n-heptylmagnesium, in particular n-butyl-n-octylmagnesium, tri-n-hexylaluminum, triisobutylaluminum, tri-n-butylaluminum, triethylaluminum, dimethylaluminum chloride, dimethylaluminum fluoride, methylaluminum dichloride, methylaluminum sesquichloride, diethylaluminum chloride,
• the antistatically acting compound and the metal alkyl are brought into contact in a concentration of in each case at least 0.01 % by weight, preferably at least 0.05% by weight, particularly preferably at least 0.1% by weight, in order to ensure sufficient reaction.
• a relatively high concentration is particularly important in the case of short contact times.
• the antistatically acting compound and the metal alkyl can be used in diluted or undiluted form, with the use of a solution being preferred. Use in an inert hydrocarbon or the monomer or one of the monomers is particularly preferred.
• the antistatically acting compound and the metal alkyl can, for example, be present in pure form, in solution or in suspension during contacting.
• One of the two components can also be present in supported form.
• the metal alkyl is used in an amount which is sufficient to bind the hydrogen bound to heteroatoms, hereinafter also referred to as active hydrogen. Particularly good results are achieved when the metal alkyl is used in an at least stoichiometric amount relative to the active hydrogen comprised in the antistatic compound. Particular preference is given to an excess of from 1.1 to 1.5 times the stoichiometric amount.
• the antistatic prepared in this way can be introduced into the reactor with the aid of all customary methods.
• the antistatic can be introduced into the reactor separately from other materials. However, it is preferably introduced as a solution in an inert solvent such as alkanes.
• the preparation of the antistatic by contacting the antistatically acting compound with a metal alkyl can be carried out in a separate apparatus prior to the polymerization, but preference is given to preparing the antistatic in the reactor immediately before use. Particular preference is given to carrying out contacting in a line leading to the reactor or a vessel connected to such a line.
• Contacting is carried out before the antistatic compound can come into contact with the catalyst and the contact time should be sufficient to ensure complete reaction of the active hydrogen.
• Contacting of the antistatically acting compound with the metal alkyl is preferably carried out for at least 5 s before introduction into the reactor. Preference is given to a contact time of from 10 s to 10 h, more preferably from 15 s to 1 h, particularly preferably from 20 s to 30 min, before introduction into the reactor.
• the present invention further provides a process for the polymerization of unsaturated monomers, in particular 1 -olefins, at temperatures of from 20 to 200 0 C and pressures of from 0.1 to 20 MPa in the presence of a polymerization catalyst using the antistatic mixture of the invention.
• the process is suitable, in particular, for the polymerization of olefins and especially for the polymerization of 1 -olefins ( ⁇ -olefins), i.e. hydrocarbons having terminal double bonds, without being restricted thereto.
• Suitable monomers can be functionalized olefinically unsaturated compounds such as ester or amide derivatives of acrylic or methacrylic acid, for example acrylates, methacrylates, or acrylonitrile.
• Preference is given to nonpolar olefinic compounds, including aryl-substituted 1 -olefins.
• Particularly preferred 1 -olefins are linear or branched
• C 2 -C 12 -I -alkenes in particular linear C 2 -C 10 -I -alkenes such as ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-decene or branched C 2 -C 10 -I -alkenes such as 4-methyl-1-pentene, conjugated and nonconjugated dienes such as 1 ,3-butadiene, 1 ,4-hexadiene or 1 ,7-octadiene or vinylaromatic compounds such as styrene or substituted styrene.
• linear C 2 -C 10 -I -alkenes such as ethylene, propylene, 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-decene or branched C 2 -C 10 -I -alkenes such as 4-
• Suitable olefins also include ones in which the double bond is part of a cyclic structure which can have one or more ring systems. Examples are cyclopentene, norbornene, tetracyclododecene or methylnorbornene or dienes such as 5-ethylidene-2-norbornene, norbornadiene or ethylnorbornadiene. It is also possible to polymerize mixtures of two or more olefins.
• the process can be used in particular for the homopolymerization or copolymerization of ethylene or propylene.
• comonomers in ethylene polymerization preference is given to using up to 40% by weight of C 3 -C 8 -I -alkenes, in particular 1-butene, 1-pentene, 1-hexene and/or 1-octene.
• Preferred comonomers in propylene polymerization are up to 40% by weight of ethylene and/or butene.
• Particular preference is given to a process in which ethylene is copolymerized with up to 20% by weight of 1-hexene and/or 1-butene.
• single-site catalysts are catalysts based on chemically uniform transition metal coordination compounds.
• Particularly suitable single-site catalysts are those comprising bulky sigma- or pi-bonded organic ligands, e.g. catalysts based on bis-cp or mono-cp complexes, hereinafter also referred to collectively as metallocene catalysts, or catalysts based on later transition metal complexes, in particular iron-bisimine complexes.
• Phillips catalysts based on chromium oxide or Ti-based Ziegler catalysts are catalyst systems which have at least two different types of active sites derived from at least two chemically different starting materials.
• the different active sites can be active sites which are comprised in various single-site catalysts.
• hybrid catalysts are those comprising late transition metal complexes, in particular iron-bisimine complexes, and at least one further mono-cp or bis-cp metallocene or a Ziegler catalyst.
• the process can be carried out using all industrially known low-pressure polymerization methods at temperatures in the range from 0 to 200 0 C, preferably from 25 to 15O 0 C and particularly preferably from 40 to 13O 0 C, and under pressures of from 0.05 to 10 MPa and particularly preferably from 0.3 to 4 MPa.
• the polymerization can be carried out batchwise or preferably continuously in one or more stages.
• Solution processes, suspension processes, stirred gas-phase processes and gas-phase fluidized-bed processes are all possible. Processes of this type are generally known to those skilled in the art.
• gas- phase polymerization in particular in gas-phase fluidized-bed reactors, solution polymerization and suspension polymerization, in particular in loop reactors and stirred tank reactors, are preferred.
• polymerization is usually carried out in a suspension medium, preferably in an inert hydrocarbon such as isobutane or mixtures of hydrocarbons or else in the monomers themselves.
• Suspension polymerization temperatures are usually in the range from -20 to 115°C, and the pressure is in the range from 0.1 to 10 MPa.
• the solids content of the suspension is generally in the range from 10 to 80%.
• the polymerization can be carried out both batchwise, e.g. in stirring autoclaves, and continuously, e.g. in tube reactors, preferably in loop reactors. In particular, it can be carried out by the Phillips PF process as described in US- A 3 242 150 and US-A 3 248 179.
• Suitable suspension media are all media which are generally known for use in suspension reactors.
• the suspension medium should be inert and be liquid or supercritical under the reaction conditions and should have a boiling point which is significantly different from those of the monomers and comonomers used in order to make it possible for these starting materials to be recovered from the product mixture by distillation.
• Customary suspension media are saturated hydrocarbons having from 4 to 12 carbon atoms, for example isobutane, butane, propane, isopentane, pentane and hexane, or a mixture of these, which is also known as diesel oil.
• the polymerization takes place in a cascade of 2 or preferably 3 or 4 stirred vessels in the presence of a Ziegler catalyst.
• the molar mass of the polymer fraction prepared in each of the reactors is preferably set by addition of hydrogen to the reaction mixture.
• the polymerization process is preferably carried out with the highest hydrogen concentration and the lowest comonomer concentration, based on the amount of monomer, being set in the first reactor.
• the hydrogen concentration is gradually reduced and the comonomer concentration is altered, in each case once again based on the amount of monomer.
• Ethylene or propylene is preferably used as monomer and a 1 -olefin having from 4 to 10 carbon atoms is preferably used as comonomer.
• the Ziegler catalyst generally suffers a reduction in its polymerization activity with rising hydrogen concentration and because a process-related dilution of the suspension with increasing total conversion occurs, the reacting polymer particles in the first reactor have the longest mean residence time. For this reason, the highest conversion of the added monomer to homopolymer or of the added monomer and comonomer to copolymer is achieved in the first reactor, compared to the downstream reactors.
• the polymerization mixture is pumped continuously through a cyclic reactor tube.
• continual mixing of the reaction mixture is achieved and the catalyst introduced and the monomers fed in are distributed in the reaction mixture.
• the pumped circulation prevents sedimentation of the suspended polymer.
• the removal of the heat of reaction via the reactor wall is also promoted by the pumped circulation.
• these reactors consist essentially of a cyclic reactor tube having one or more ascending legs and one or more descending legs which are enclosed by cooling jackets for removal of the heat of reaction and also horizontal tube sections which connect the vertical legs.
• the impeller pump, the catalyst feed facilities and the monomer feed facilities and also the discharge facility, thus in general the settling legs, are usually installed in the lower tube section.
• the reactor can also have more than two vertical tube sections, so that a meandering arrangement is obtained.
• the polymer is generally discharged continuously from the loop reactor via settling legs.
• the settling legs are vertical attachments which branch off from the lower reactor tube section and in which the polymer particles can sediment. After sedimentation of the polymer has occurred to a particular degree, a valve at the lower end of the settling legs is briefly opened and the sedimented polymer is discharged discontinuously.
• the suspension polymerization is carried out in a loop reactor at an ethylene concentration of at least 10 mol%, preferably 15 mol%, particularly preferably 17 mol%, based on the suspension medium.
• the suspension medium is not the input suspension medium such as isobutane alone but rather the mixture of this input suspension medium with the monomers dissolved therein.
• the ethylene concentration can easily be determined by gas-chromatographic analysis of the suspension medium.
• a preferred polymerization process is that carried out in a horizontally or vertically stirred or fluidized gas phase.
• the circulated reactor gas is usually a mixture of the 1 -olefin to be polymerized, if desired a molecular weight regulator such as hydrogen and inert gases such as nitrogen and/or lower alkanes such as ethane, propane, butane, pentane or hexane.
• a molecular weight regulator such as hydrogen and inert gases such as nitrogen and/or lower alkanes such as ethane, propane, butane, pentane or hexane.
• propane if appropriate in combination with further lower alkanes, is preferred.
• the velocity of the reactor gas has to be sufficiently high firstly to fluidize the mixed bed of finely divided polymer present in the tube and serving as polymerization zone and secondly to remove the heat of polymerization effectively (noncondensed mode).
• the polymerization can also be carried out in the condensed or supercondensed mode, in which part of the circulating gas is cooled to below the dew point and returned to the reactor together as a two-phase mixture or separately as a liquid and a gas phase in order to make additional use of the enthalpy of vaporization for cooling the reaction gas.
• the cooling capacity depends on the temperature at which the (co)polymerization in the fluidized bed is carried out.
• the process is advantageously carried out at temperatures of from 30 to 160 0 C, particularly preferably from 65 to 125°C, with temperatures in the upper part of this range being preferred for copolymers of relatively high density and temperatures in the lower part of this range being preferred for copolymers of lower density.
• a multizone reactor in which two polymerization zones are linked to one another and the polymer is passed alternately a plurality of times through these two zones, with the two zones also being able to have different polymerization conditions.
• a reactor is described, for example, in WO 97/04015 and WO 00/02929.
• the different or else identical polymerization processes can also, if desired, be connected in series and thus form a polymerization cascade.
• a parallel arrangement of reactors using two or more different or identical processes is also possible.
• the polymerization is preferably carried out in a single reactor.
• the chromium content of the catalyst was determined photometrically via the peroxide complex.
• the density of the polymer samples was determined in accordance with DIN EN ISO 1183-1 , variant A.
• the determination of the intrinsic viscosity ⁇ which indicates the limit value of the viscosity number on extrapolation of the polymer concentration to zero, was carried out using an automatic Ubbelohde viscometer (Lauda PVS 1) at a concentration of 0.001 g/ml in decalin as solvent at 135 0 C in accordance with ISO 1628-1 :1998.
• the molar masses were determined by high-temperature gel permeation chromatography by means of a method based on DIN 55672 using 1 ,2,4-trichlorobenzene as solvent and a flow of 1 ml/min at 140 0 C. Calibration was carried out by means of PE standards on an Waters 150C. Evaluation of the data was carried out using the software Win-GPC from HS- Engineeringsgesellschaft fur letone Hard- und Software mbH, Ober-Hilbersheim.
• the bulk density was measured on polymer powder in accordance with DIN 53468.
• melt mass flow rates MFR 2 (Ml), MFR 2 i (HLMI) were determined at a temperature of 190 0 C and a weight of 2.16 or 21.6 kg in accordance with ISO 1133.
• the fine dust content is the proportion of polymer particles which have a particle size of less than 125 ⁇ m.
• the particle size was determined by sieve analysis. The invention is illustrated below by means of examples, without being restricted thereto.
• the catalyst having a content of 1 % by weight of chromium was prepared as described in EP A 0 589 350.
• the activation of the catalyst precursor was carried out at the calcination temperatures indicated in Table 1. 2.5% by weight of ammonium hexafluorosilicate (ASF), based on the total mass of the catalyst, were added. To carry out the activation, the catalyst precursor was heated to 35O 0 C over a period of one hour, maintained at this temperature for 1 hour, subsequently heated to the calcination temperature, maintained at this temperature for 2 hours and subsequently cooled, with cooling below a temperature of 35O 0 C being carried out under nitrogen.
• ASF ammonium hexafluorosilicate
• the polymerizations were carried as suspension processes in isobutane in a 0.2 m 3 PF loop reactor.
• the melt mass flow rate (MFR 2 i) and the density were set via the ethylene concentration or hexene concentration.
• the reactor pressure was 3.9 MPa.
• Example 1 pure Costelan AS 100 (0.44% by weight in hexane) was used in the polymerization, and in Example 1 an antistatic which had been prepared by mixing 2 parts of a 0.44% strength by weight solution of Costelan AS 100 (from Costenoble, Eschborn, Germany) in hexane with 1 part of a 0.40% strength by weight solution of trihexylaluminum (THA) in hexane was used.
• TSA trihexylaluminum
• the antistatic mixture of the invention leads to a higher productivity and bulk density combined with a lower fine dust content and MFR drop (difference between the MFR measured on the granules after homogenization and that measured on the powder) of the kneading material.
• the poisoning effect of the antistatic mixture with THA on the catalyst is significantly lower than that of pure antistatic, and the antistatic action is surprisingly even improved.
• the mixture of the invention enables the production costs to be considerably lowered as a result of the higher catalyst efficiency and the higher bulk density (i.e. higher reactor polymer density) and at the same time enables improved product quality to be achieved.
• Processes of the ungranulated polymer powder can increase the throughput of processing plants as a result of the higher bulk density.
• Costelan AS 100 with trihexylaluminum (THA) were prepared. Both Costelan AS 100 and also THA were present as dilute solutions in hexane, and the solutions were mixed in a ratio of 2:1. A homogeneous solution was obtained in all cases. All measurements were carried out at a temperature of 20 0 C. The concentrations of Costelan AS 100 and THA in hexane in the mixture are shown in Table 2.

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