HIGH-TEMPERATURE (CO)POLYMERIZATION OF ETHYLENE USING A CATALYST SYSTEM

Abstract: Catalyst system suitable for the (co)polymerization of ethy­ lene and optionally minor amounts of 1-alkenes and/or dienes at a tem­ perature of at least 180◊C, to be prepared by combining at least four components, which components comprise: 1. one or more titanium compounds 2. one or more vanadium compounds 3. one or more organoaluminium compounds 4. one or more chlorides, the atomic ratio of chlorine to the sum of titanium and vanadium being at least 6, and the components being fed, separately or in com­ bination, direct to the polymerization vessel.

Description: The invention relates to a process for the (co)polymerization of ethylene and optionally minor amounts of 1-alkenes and/or dienes at a temperature of at least 180¤C in a polymerization vessel using a catalyst system. There are numerous catalyst systems that are capable of bringing about polymerization of ethylene and/or 1-alkenes. Thus, for instance, so-called Phillips and Ziegler-Natta systems can be distinguished. Of these, a number relate to polymerization in the gas phase. Others are directed at polymerization in the presence of a liquid dispersant. The latter can be subdivided into the so-called suspension system, with polymerization taking place at temperatures below the dissolution temperature of polyethylene, and the so-called solution system, with a polymerization temperature above the dissolution temperature of the polyethylene formed. Solution polymerization requires special catalyst systems as the catalyst activity and the molecular weight of the polymer produced generally decrease with increasing polymerization temperature. It was not until the end of the sixties that a catalyst was developed the activity of which was such as to allow of solution polymerization of ethylene without there being any need to remove catalyst residues from the product (GB-A 1,235,062). Polymerization generally takes place at temperatures that are only little above the dissolution temperature of polyethylene, because the activity of catalysts customarily applied so far decreases at high polymerization temperatures. At unchanged residence times, this means that the polymer yield decreases, as a result of which the amounts of catalyst residues in the polymer increase and washing out of the polymer soon becomes necessary. A problem in this exothermic polymerization reaction is the dissipation of the heat of polymerization. Cooling through the wall or through cooling devices in the reactor may easily lead to polymer deposition on the cooling surfaces, especially at coolant temperatures below 150¤C. For this reason, strong cooling of the reactor feed is preferred. This, however, requires much energy and will become more expensive as fuel prices rise. Polymerization at high temperatures would have energy advantages also in another respect: not only can the strong cooling of the reactor feed be reduced or even be done without, there also no longer is any need during polymer upgrading to heat the product in order to evaporate the solvent. The reason for this is that the heat of evaporation decreases or even becomes zero as the solution temperature increases and approaches, or even exceeds, the critical temperature of the solvent, and as a result the enthalpy of evaporation becomes minimal. For the above reasons there is much demand for high-temperature catalysts. These catalysts should be so active as to retain sufficient activity also at very high polymerization temperatures (above 180¤C). Present-day legislation renders it even more difficult to meet this requirement by imposing clear limits as regards the amount of transition metals in products. In addition, the polymer produced is to meet the customary requirements as regards processability and applicability, which implies the molecular weight must be sufficiently high, or the melt index sufficiently low. The invention aims to find a process for the (co)polymerization of ethylene and optionally minor amounts of 1-alkenes and/or dienes at a temperature of at least 180¤C in a polymerization vessel by using a catalyst system that meets the above requirements and that is suitable for plant application without sacrificing activity or the capacity to form large polymer molecules at very high polymerization temperatures. It has, surprisingly, been found that in the claimed polymerization process using a catalyst system that is prepared by combining at least four components, which components comprise: 1. one or more titanium compounds 2. one or more vanadium compounds 3. only one organoaluminium compound 4. one or more chlorides, the atomic ratio of chlorine to the sum of titanium and vanadium being at least 6, and the components being fed, separately or in combination, direct to the reactor, very high polymerization temperatures can be used. An advantage of a catalyst system used in the process according to the invention is that very high temperatures can be used for the production of polyethylene meeting the customary requirements as regards processability and applicability and containing such a small amount of catalyst residues that washing out of the product is not necessary. In EP-A-0229422 the use of a catalyst system in a polymerization process is described which catalyst system comprises a titanium compound, a vanadium compound, a first organoaluminum compound and additionally a second organoaluminum compound that is added to the catalyst system separately from the first organoaluminum compound. The catalysts used in the process according to the subject invention not only are very active, hut also very rapid, so that very short residence times can be used. Short residence times have the great advantage that a small reactor can be used. Thus, in a 5 m³ reactor an annual production of more than 50,000 t can be reached when using the catalysts according to the invention. With these catalysts, residence times of 10 minutes or shorter will suffice. At residence times of 5 minutes the yields still are so high that no washing treatment for catalyst residue removal need be applied. Yet another advantage is that the components are fed direct to the reactor, that is, without heating, incubations, precipitate recovery and/or other treatments, which is a great advantage in plant application. The residence time of the various catalyst components in the feed lines generally is sufficient for obtaining an active catalyst system. In most cases this residence time will not be longer than some, for instance 5, minutes, and often even less, for instance less than 3 minutes or even less than 1 minute. Catalyst systems used in the process according to the invention have the highest activity at an atomic ratio of aluminium to the sum of titanium and vanadium of at least 3, in particular 5. It is recommendable for the atomic ratio of chlorine to the sum of titanium and vanadium to be at least 7.5, in particular at least 9. Furthermore, an atomic ratio of titanium to vanadium of at most 1, and in particular at most 0.8, is to be preferred. The atomic ratio of aluminium to the sum of titanium and vanadium will generally not exceed 200, and in particular it will not exceed 100. The atomic ratio of titanium to vanadium usually is at least 0.001, in particular at least 0.01. As titanium compounds, both tetra- and trivalent compounds of the general formulas Ti(OR¹) 4-n X¹ n and Ti(OR²) 3-m X² m , respectively, where the symbols R¹ and R² are equal or different and represent hydrocarbon residues with 1-20 carbon atoms, X¹ and X² halogen atoms, and 0 ≦ n ≦ 4 and 0 ≦ m ≦ 3, yield good results. Of these compounds, titanic acid esters such as TBT or TIPT are to be preferred. Titanium complexes such as, for instance TiCl₃.3 decanol, TBT.AlCl₃, TBT.0.2 Cr(acac)₂, TBT.x CrO₃ and TBT.x diethyl zinc (0 < x ≦ 1) may also be applied. Compounds such as, e.g., cresyl titanate polymer (CH₃C₆H₄[Ti(OC₆H₄CH₃)₂O]a OC₆H₄CH₃ with a ≧ 1) can likewise be applied (see the list of abbreviations hereinafter). As vanadium compounds, use can be made of compounds of the general formula VO(OR³) 3-p X³ p , where the symbols R³ are equal or different and represent a hydrocarbon residue with 1-20 carbon atoms, X³ is a halogen atom and 0 ≦ p ≦ 3, in particular vanadyl chloride and/or vanadyl butoxide. It is also possible to use vanadium compounds of the general formula VX⁴₃ or VX⁴₄, where X⁴ represents a halogen atom. X⁴ preferably is a chloride atom. Mixtures of titanium compounds and/or vanadium compounds can also be used as catalyst components. The organoaluminium compound can be chosen from a large group of compounds. Preference is given to an organoaluminium compound of the general formula R⁴ q AlX⁵ 3-q , where the symbols R⁴ are equal or different and represent a hydrocarbon residue with 1-20 carbon atoms, in particular alkyl, X⁵ represents a halogen atom, in particular chlorine, and 0 < a ≦ 3. Mixtures can also be applied. Examples of organoaluminium compounds are: DEAC, MEAC, MMAC, SEAC, SMAC, TEA, TIBA, TMA, as well as compounds with aluminium bonded to oxygen, including alkyl siloxalanes. Particularly SEAC, DEAC, TMA and/or TEA yield good results. (See the list of abbreviations hereinafter). The chlorides comprise alkyl chlorides (e.g. isopropyl chloride), acyl chlorides, aryl chlorides (e.g. benzyl chloride), hydrogen chloride, chlorides of elements from groups 3a and 4a of the Periodic System (Handbook of Chemistry and Physics, 52nd ed.), or combinations thereof. SiCl₄, SnCl₄ and/or BCl₃ are preferred. An active catalyst yielding a high polymer molecular weight, also at very high polymerization temperatures, is obtained also when the catalyst system further comprises one or more electron donors (Lewis bases), such as, for instance, DEA, EB, IPA, acetyl acetone and/or MPT. (See the list of abbreviations hereinafter). This electron donor is preferably supplied together with one of the other compounds, such as (one of) the transition metal compounds, for instance in the form of TBT, TIPT and/or VB, and in particular together with the organoaluminium compound. The catalyst components may be fed to the reactor separately or in combination. The mixing sequence of the components is of little importance. First, for instance, a titanium compound and a vanadium compound can he mixed, subsequently an organoaluminium compound, optionally in combination with an electron donor, can be added, and finally the chloride. It also is possible to first mix the organoaluminium compound with the chloride, and subsequently with a titanium compound and a vanadium compound. Another possibility is to add the organoaluminium compound to one of the transition metal compounds before adding the second transition metal compound. It may be preferable for the vanadium and titanium compounds to be mixed beforehand, especially when one of the two is less stable, such as VOCl₃. There is advantage in using the mixing sequence: 1. organoaluminium compound (optionally with premixed electron donor); 2. one of the two transition metal compounds; 3. the other transition metal compound; 4. the chloride. It also is possible to supply the catalyst components separately to the reator using separate feed lines. In that case for instance a combination of the transition metals can be fed through one feed line and a combination of the organoaluminium compound and the chloride through another feed line, or a combination of the transition metals and the chloride through one and the organoaluminium compound through another feed line. In so far as the catalyst components are mixed before being supplied to the reactor, it is recommendable to effect this at a temperature below 125¤C, in particular below 75¤C, more in particular below 50¤C. The temperature will generally not be below -60¤C. The presence or absence of monomer(s) during mixing of the catalyst components has little effect on catalyst activity. The polymers obtained by the process according to the invention comprise ethylene, one or more 1-alkenes with 3 to 18 carbon atoms in an amount of 0 to 15 moles % relative to the total polymer, and one or more dienes with at least 7 carbon atoms in an amount of 0 to 10 moles % relative to the total polymer. Good properties are found in particular in polymers in which the dienes contain at least two non-conjugated double bonds capable of being polymerized by means of transition metal catalysts and in which the amount of dienes does not exceed 0.1 mole % relative to the total polymer. These polymers may contain the customary additives, such as stabilizers, lubricants, and also, for instance, crosslinking agents and fillers. Polymers obtained by means of a catalyst used in the process according to the invention possess the customary, commercially desirable properties, such as a sufficiently high molecular weight (low melt index) and good processability. They can be used for the preparation of cast film and blown film with good mechanical and optical properties, while also the rheological and welding properties meet the normal requirements. The polymers also are suitable for many other customary applications, e.g. injection moulding, blow moulding, rotational moulding. Polymerization can subsequently be effected in a manner known per se, both batchwise and continuously. In general the catalyst components are added in such amounts that the amount of titanium in the polymerization medium is 0.001 to 4 mmole/l, preferably 0.005 to 0.5 mmole/l, and more in particular 0.01 to 0.05 mmole/l As dispersant, both in catalyst preparation and in polymerization, use can be made of any liquid that is inert relative to the catalyst system, for instance one or more sutarated, straight or branched aliphatic hydrocarbons, such as butanes, pentanes, hexanes, heptanes, pentamethylheptane or petroleum fractions such as light or regular-grade petrol, isopar, naphtha, kerosine, gas oil. Aromatic hydrocarbons, for instance benzene or toluene, are usable, but such solvents will generally not be used in technical-scale production, both for cost considerations and for safety considerations. By preference, therefore, as solvent in technical-scale polymerizations use is made of the cheap aliphatic hydrocarbons, or mixtures thereof, as marketed by the petrochemical industry. In many cases, pretreatments of such solvents, for instance drying or purification, are required. This will present no problems whatsoever to the average person skilled in the art. Of course, cyclic hydrocarbons such as cyclohexane and decalin can also be used as solvent. Polymerization is effected at temperatures above 180¤C, and more in particular at temperatures above 200¤C. For practical considerations the temperatures will generally not exceed 300¤C. The polymer solution obtained upon polymerization can subsequently be upgraded in a way known per se, the catalyst generally being deactivated at some stage of upgrading. Deactivation can be effected in a way known per se. The catalysts used in the process according to the present invention have such a high activity that the amount of catalyst in the polymer, notably the transition metal content, is so low that removal of catalyst residues can be done without. Of course the polymer can be subjected to a washing treatment to reduce the residual content of catalyst components even further, if this is desired. Polymerization can be effected at atmospheric pressure but also at elevated pressure, up to about 1000 bar, or at even higher pressures, both in continuous and in discontinuous manner. By polymerizing under pressure, the polymer yield can be increased further, which may contribute to the preparation of a polymer with a very low content of catalyst residues. Polymerization is preferably effected at pressures of 1-200 bar, and more in particularly of 10-100 bar. Pressures in excess of 100 bar soon give rise to technological objections. However, pressures that are much higher, of 1000 bar and more, can be used if polymerization takes place in so-called high-pressure reactors. In the subject process, modifications known per se can be applied. Thus, for instance, the molecular weight can be controlled by addition of hydrogen or other agents customarily applied for the purpose. Polymerization can also be effected in several stages, connected either in parallel or in series, in which, if desired, differing catalyst compositions, temperatures, residence times, pressures, hydrogen concentrations, are applied. It is, for instance, possible to prepare products with a broad molecular weight distribution by choosing the conditions, for instance pressure, temperature and hydrogen concentration, in one stage such that a polymer with a high molecular weight is formed, while the conditions in another stage are chosen such that a polymer with a low molecular weight is formed. The invention will now be elucidated with reference to some examples, without, however, being restricted thereto. List of abbreviations used : - Acac = acetylacetonate - BzCl = benzyl chloride - DEA = diethylamine - DEAC = diethylaluminium chloride - EB = ethyl benzoate - IPA = isopropyl alcohol - IPCl = isopropyl chloride - MEAC = monoethylaluminium dichloride - MMAC = monomethylaluminium dichloride - MPT = methylparatoluate - SEAC = sesquiethylaluminium chloride (ethyl 1.5 AlCl 1.5 ) - SMAC = sesquimethylaluminium chloride (methyl 1.5 AlCl 1.5 ) - TBT = tetrabutoxytitanium - TEA = triethylaluminium - TIBA = triisobutylaluminium - TIPT = tetraisopropoxytitanium - TMA = trimethylaluminium - VB = vanadyl butoxide Polymerization experiments were conducted at 240◊C in a one-litre gas-liquid reactor with 500 ml purified and dried pentamethylheptane (PMH) as dispersant and ethylene to a reactor pressure of 17 bar. The catalyst components were premixed in PMH during 1 minute at 25◊C and subsequently pumped into the reactor. The polymerization time was 10 minutes. The polymer was stabilized, if necessary, dried and weighed. The yield is expressed in g polymer per mmole titanium + vanadium. The activity α of the catalyst system is expressed as g PE/mmole (Ti + V). 10 minutes. The melt index (M.I.) of the polymer, expressed in dg/min, is determined in accordance with ASTM D 1238, cond. E. Example I SEAC, TBT, VB and SiCl₄ were mixed in this sequence and fed to the reactor so that the amounts present during polymerization were 0.6, 0.04, 0.06 and 0.1 mmole/l, respectively. The catalyst had an activity α of 1012. The melt index of the polymer prepared was 9.5 dg/min. Example II Example I was repeated, this time with 0.16 mmole/l SiCl₄. The polymer had a melt index of 8.7 dg/min, while α was 1154. Example III Example I was repeated, now with 0.2 mmole/l SiCl₄. α was 1264, and the melt index 12.5 dg/min. Comparative example 1 Example I was repeated without chloride. The melt index was 15.2, and α 798. Example IV The catalyst system of Example III was applied in a copolymerization of ethylene and octene-1. Before the ethylene, 25 ml octene-1 was fed to the reactor. The density of the copolymer was 933 kg/m³ (ASTM D 1505), the melt index 9.7, and α 1203. Example V Example IV was repeated in the presence of 50 ml 1-octene. The density was 929 kg/m³, the melt index 6.0 dg/min and α 932. Example VI Example III was repeated, but now with benzyl chloride instead of SiCl₄. α was 1164, the melt index 10 dg/min. Comparative example 2 Example III was repeated, but this time with 0.1 mmole/l TBT and without vanadium compound. The catalyst was not active. Example VII Example III was repeated, but now with isopropyl chloride instead of SiCl₄. α was 1103, the melt index 11 dg/min. Comparative example 3 SEAC, TBT and VOCl₃ were mixed in this order and fed to the reactor so that during the polymerization 0.6, 0.04 and 0.06 mmole/l, respectively, were present. α was 566. Example VIII DEAC and ethyl benzoate were mixed in such a ratio that 0.1 and 0.2 mmole/l, respectively, were present during polymerization. The catalyst system further consisted of TBT, VB and BzCl, in amounts of 0.04, 0.06 and 0.2 mmole/l, respectively, during polymerization. The order of addition was (DEAC + ethyl benzoate), TBT, VB, BzCl. α was 1083, the melt index 10 dg/min. Example IX Example VIII was repeated, but now with 0.2 mmole/l SiCl₄ instead of BzCl. α was 1009, the melt index 7.8 dg/min.

Claims: Process for the (co)polymerization of ethylene and optionally minor amounts of 1-alkenes and/or dienes at a temperature of at least 180¤C in a polymerization vessel using a catalyst system, in which process the catalyst system is prepared by combining at least four components, which components comprise: 1. one or more titanium compounds 2. one or more vanadium compounds 3. only one organoaluminium compound 4. one or more chlorides, the atomic ratio of chlorine to the sum of titanium and vanadium being at least 6, and the components being fed, separately or in combination, direct to the polymerization vessel. Process according to claim 1, characterized in that the atomic ratio of aluminium to the sum of titanium and vanadium is at least 3. Process according to any one of claims 1-2, characterized in that the atomic ratio of chlorine to the sum of titanium and vanadium is at least 7.5. Process according to any one of claims 1-3, characterized in that the atomic ratio of titanium to vanadium is lower than or equal to 1. Process according to any one of claims 1-4, characterized in that the titanium compound belongs to the compounds of the general formula (Ti(OR¹) 4-n X¹ n and/or Ti(OR²) 3-m X² m , where the symbols R¹ and R² are equal or different and represent hydrocarbon residues with 1-20 carbon atoms, X¹ and X² halogen atoms, 0 ≦ n ≦ 4 and 0 ≦ m ≦ 3. Process according to claim 5, characterized in that the titanium compound is a titanic acid ester. Process according to claim 6, characterized in that the titanium compound is tetrabutoxytitanium. Process according to any one of claims 1-7, characterized in that the vanadium compound belongs to the compounds of the general formula VO(OR³) 3-p X³ p , where the symbols R³ are equal or different and represent a hydrocarbon residue with 1-20 carbon atoms, X³ a halogen atom, and 0 ≦ p ≦ 3. Process according to claim 8, characterized in that the vanadium compound is vanadyl chloride and/or vanadyl butoxide. Process according to any one of claims 1-7, characterized in that the vanadium compound belongs to the compounds of the general formula VX⁴₃ or VX⁴₄, where X⁴ represents a halogen atom. Process according to any one of claims 1-10, characterized in that also one or more electron donors are present. Process according to any one of claims 1-11, characterized in that the organoaluminium compound belongs to the compounds of the general formula: R⁴ q AlX⁵ 3-q , where the symbols R⁴ are equal or different and represent a hydrocarbon residue with 1-20 carbon atoms, X⁵ represents a halogen atom and 0 < q ≦ 3. Process according to claim 12, characterized in that the organoaluminium compound is trialkylaluminium, dialkylaluminium chloride and/or sesquialkylaluminium chloride. Process according to any one of claims 1-13, characterized in that the chloride is an alkyl chloride, acyl chloride and/or aryl chloride a hydrogen chloride, one or more chlorides of elements from groups 3a and 4a of the Periodic System, or combinations of these. Process according to claim 14, characterized in that the chloride is BCl₃, SiCl₄ and/or SnCl₄. Process according to any one of claims 1-15, characterized in that the catalyst components are in combination supplied to the reactor. Process according to claim 16, characterized in that first the organoaluminium compound, then the titanium compound or vanadium compound, subsequently the other transition metal compound and lastly the chloride are combined with one another. Process according to any one of claims 1-15, characterized in that the organoaluminium compound and a combination of the titanium compound with the vanadium compound are separately fed to the reactor, the chloride being combined with the titanium compound and the vanadium compound and/or with the organoaluminium compound. Process according to any one of claims 16-18, characterized in that the organoaluminium compound is mixed with an electron donor before being combined with the other catalyst components. Process according to any one of claims 16-19, characterized in that the catalyst components are mixed at a temperature below 125¤C. Process according to claim 20, characterized in that the catalyst components are mixed at a temperature below 75¤C.

Inventors: BLENKERS, JOHANNES, COOSEMANS, LUC MARIA CONSTANT, VAN DEN BOSCH, FRANS
Applicants: DSM N.V.
Application year: 1988
Main classification: C08F4
IPC codes: C08F4, C08F10