Process for preparing ethylene-based polymers having low molecular weight

The present invention relates to a process for the preparation of additives to be used as cold flow improvers (CFI) for liquid hydrocarbons derived from oil distillation, in particular middle distillates such as gas oil.

Particularly the invention refers to a process for the preparation of ethylene and alpha-olefins copolymers, in particular propylene, or terpolymers obtained by adding a third dienic monomer or compositions comprising said polymers.

More particularly, the process relates to polymers having the structural characteristics described in EP 350072.

The copolymers (terpolymers) described in said patent have a value of X₂ and/or X₄ parameters equal to or lower than 0.02; X₂ and X₄ represent the fraction of methylenic sequences containing uninterrupted sequences of 2 and 4 methylenic groups between two successive methyl or methylene groups respectively in the polymeric chain, as compared with the uninterrupted total sequences of methylene groups determined by ¹³C-NMR.

This specific copolymer and/or terpolymer shows improved properties as CFI with respect to the other polymeric chains having the same base without the essential feature of X₂, X₄ cited above.

In the patent application EP 350072 are exemplified and described polymers having a high average molecular weight, calculated by viscosimetric method, with values varying from about 80,000 to about 120,000 as additives suitable for cold flow improvers (CFI).

In the same patent are also stated as suitable products of lower molecular weight obtained by high molecular weight polymers after a degradation process.

There are exemplified degradated polymers with viscosimetric average molecular weight ranging from about 20,000 to about 50,000.

In general it is stated in the specification that the suitable viscosimetric average molecular weights range between 1,000 and 200,000, preferably between 3,000 and 150,000.

In said patent the polymers are obtained by using high yield catalysts, in particular titanium salts supported on magnesium chloride, even if there are no limitations about possible catalysts provided that they can get the essential features of X₂ and X₄ of the copolymer or terpolymer stated above.

Object of the present invention is a process for the preparation of polymers suitable as cold flow improver (CFI) having the properties stated in the above cited patent which permits to obtain low molecular weight polymers, as defined below and by avoiding the degradation process.

According to the cited patent this step is stated as a preferred one to obtain polymers therein described with molecular weight lower than 100,000.

In practice this step is essential since the high molecular weight polymers induce into the system also viscostaticity characteristics.

Indeed in the cited prior art this step was unavoidable, otherwise the high molecular weight copolymer was not sufficiently soluble in the normal hydrocarbon solvent, for example toluene, cyclohexane and other hydrocarbon blendings specific in the gas oils distillation.

The practical result is that only low concentration additives can be prepared with evident industrial disadvantages, for example tranport costs since substantially it is transported the solvent and not the additive useful as CFI.

The additive concentration reaches maximum values at around 10% by weight for molecular weights of about 100,000 if one wants to obtain processable solutions at room temperature.

The industrial disadvantage is the need of a very expensive plant which involves the addition of units where it is carried out the degradation to obtain solutions containing the additive at higher concentrations.

In the cited patent there are not stated other processes for the obtainment of low molecular weight polymers for the following reasons.

It is well known in the art the preparation of elastomeric copolymers of ethylene with propylene or other higher alpha-olefins.

There are also known elastomeric terpolymers obtainable with the components indicated for the copolymers and the addition of a third monomer containing two double bonds (diene).

The known processes are substantially divided in two classes: solution processes (solvent) and suspension processes (bulk).

The solution processes take place in the presence of solvents, as for example hexane, cyclohexane, toluol, etc. bring to the production of elastomeric copolymers and terpolymers dissolved in the solvent.

The polymeric solution coming from the reactor shows a polymer content of about 5-10% by weight depending on the weight average molecular weight.

The obtained polymers have a high molecular weight, generally higher than 80,000 as weight average molecolar weight.

It must be considered that depending on the weight average molecular weight the concentration of the polymer in the solvent has a limit value, since over this limit the stirring of the reaction mass becomes difficult as well as the heat transfer and the monomer solubility does not decrease proportionally.

The polymerization process in solution can take place in a single reactor or in a series of reactors and the global process consists of more stages: the described polymerization, subsequent step of purification from catalytic residues followed by a stripping with steam to separate the unreacted monomers.

The catalytic residues must be removed by treating the polymeric solution at the reactor exit for example by an aqueous solution of caustic soda.

This stage of the process is simply an extraction, and it is more effective depending on the employed time and the number of washings.

The further stripping step consists in putting the washed solution in contact with heat water and steam so as to evaporate the monomers and the solvent.

It is thus obtained a gummy granules suspension of elastomeric copolymer or terpolymer in water.

The disadvantage of the solution process resides in that it is difficult to prepare low molecular weight polymers since these ones are difficult to be separated from the solution coming from the stripper.

Experiments carried out by the Applicant showed that polymers with weight average molecular weight lower than 80,000 give many drawbacks both in the depuration and in the stripping steps.

In fact the solution should be constituted by low molecular weight polymers and therefore would have a very low viscosity by causing emulsion phenomena in the stripping step and separation phenomena with the formation of two phases in which the polymeric part, having lower density, is in the upper part of the stripper so giving considerable processability problems and removal of unreacted monomers.

Therefore the process in solution, even if theorically could be used for the low molecular weight polymers synthesis, the total cycle for the obtainment of the low molecular weight polymers becomes disadvantageous both from the industrial and economic point of view, and technically could not be used.

Moreover it must be noted that the conversion of the monomers into polymer is very low with a subsequent low specific production of the reactors. At most it can be reached a value of 10% total solid with one sole reactor. This makes the process for our purposes of low industrial interest also from the store and transport point of view.

The alternative stated in the cited EP patent is to use a degradation process when low molecular weight polymers are desired.

It is known also the process in suspension in which the polymerization takes place for example in liquid propylene in which the obtained polymer is insoluble.

In the alternative it can be used mixtures of liquid propylene with propane, buthane acting as suspending agents of the reaction polymeric products.

From a technological point of view this process shows the following limits and drawbacks: the polymerization temperature cannot exceed 80°-90°C, this being the propylene critical temperature (92°C). By increasing the polymerization temperature the polymers start going into solution with consequent lowering of the ethylene solubility and with foulness of the reactor walls caused by the high molecular weight polymers.

This last gives drawbacks with regard to the stirring of the system which becomes difficult.

In this process due to the high polymerization rate, the catalysts can be left in the polymer, i.e. it is not necessary the process of depuration of the catalytic residues.

Nevertheless the aqueous stripping for the monomers recovery shows the same drawbacks stated for the process in solution.

Therefore, also with this process, as already said for the process in solution, it is not possible to obtain low molecular weight polymers.

Due to the indicated drawbacks it is evident what said in the above cited patent where the degradation is stated as a process for obtaining low molecular weight polymers, in practice less than 100,000.

Therefore there are no alternatives to the described industrial processes when a low molecular weight product is desired.

Therefore the object of the present invention is a polymerization process of elastomeric copolymers or terpolymers based on ethylene for cold flow improver (CFI) having a viscosimetric average molecular weight ranging between about 600 and about 16,000, preferably between 4,000 and 14,000, more preferably 6,000-12,000, comprising: <ul id="ul0001" list-style="none" compact="compact"><li>a) to carry out the polymerization of monomers in suspension in the presence of alpha-olephin having 3-12 carbon atoms, liquid in the reaction conditions, in the presence of an amount of solvent from about 5 to 30% by volume, preferably 10-20% of the reactor volume, with solubility parameter comparable to the liquid product, in the presence of a polymerization catalyst able to give the X₂ and X₄ parameters, as defined above;</li><li>b) forwarding of the polymer slurry into a flash pipe for the evaporation of the unreacted monomers and of minimum quantities of solvent, for example lower than 10%;</li><li>c) separation of the polymeric solution with the quantity of solvent introduced into the reactor as solvent foot, in solvent of the same type or different, so as to obtain the desired polymer concentrations, and disactivation of the catalyst by bubbling a wet air stream.</li></ul>

The Applicant has unexpectedly and surprisingly found that by carrying out the flash with the polymer slurry of the present invention, the monomers dissolved in the solution are almost totally removed. In general the remaining quantity is &lt; 3% by weight.

The Applicant has unexpectedly found that in the subsequent step of the catalyst disactivation by bubbling wet air stream (step c) the quantity of monomers dissolved in the polymeric solution was lower than 0.01% by weight.

In this case no further stripping steps are necessary with water or steam which should cause the above mentioned drawbacks.

Tests carried out by the Applicant showed that by carrying out the flash on high molecular weight polymers, about 80,000 as weight average molecolar weight, it is not possible to remove the monomers in high quantities and it is always necessary a stripping step with the above mentioned drawbacks.

The quantity of remaining monomers before stripping in these cases is higher than 5% by weight, in general it ranges between 7-10% by weight.

The flash and separation steps permit to obtain a polymer solution, optionally by adding solvent in this step.

As solubility parameter of the solvent in relation to the produced copolymer it is meant that one reported by Flory in cap. XII of "Principle of Polymer Chemistry" edited by Cornell University Press Ithaca (1953) N.Y. and confirmed by Collins in "Experiments in Polymer Science" edited by Wiley Interscience N.Y. 1973.

In the polymerization step the molecular weight is regulated at the desired value either by the temperature and/or by the addition of a molecular weight regulator.

The polymers can contain also units deriving from monomers having 6 to 20 carbon atoms, as for example styrene, alpha-metylstyrene; or deriving from polar monomers such as alkyl-methacrylates where the alkyl has 1-20 carbon atoms, preferably 1-6, for example metylmethacrylate.

The polymerization process temperature of this invention can range from -50°C to +200°C. One can work at atmospheric pressure or under pressure, for example up to 100 atm.

In the mixed process solution/suspension of the present invention the polymer is completely dissolved in the reaction solvent or highly swelled in the suspending monomer.

One can polymerize in propylene when ethylene/propylene copolymers are prepared, or in the presence of the alpha-olefin when no propylene is used.

In general the alpha-olefin has from 3 to 20 carbon atoms, preferably from 3 to 6. For example butene, 4-methylpentene-1, hexene-1 can be cited.

As solvents, for example, one can use aliphatic hydrocarbon solvents from 5 to 20 carbon atoms, alicyclic from 6 to 20 carbon atoms, aromatic from 6 to 20 carbon atoms, aromatic-substituted from 6 to 20 carbon atoms, for example alkylbenzenes, or aromatic containing eteroatoms in the aromating ring. It can be also used the well known hydrochlorofluorocarbon and hydrofluorocarbon solvents.

The sole requisite of the solvents is to be polymerization grade for the catalytic system used.

The copolymers and terpolymers of the present invention can be saturated or unsaturated. The latter are obtained when conjugated diolefinic monomers are used, for example from 4-10 carbon atoms, or non-conjugated from 6 to 20 carbon atoms, for example 1-4-hexadiene, ethylidennorbornene, cyclooctatriene, norbornene, methyltetrahydroindene.

Both heterogeneous and homogeneous catalysts can be used, the former ones derived for example from Ti, Zr and Hf salts, also supported for example on magnesium chloride, and the latter ones derived from metallocenes of the same metals.

The catalysts suitable for the process of the invention are in general those ones used for the polymerization of alpha-olefins, diolefins, acethylenic compounds, polyenes and carbon monoxide.

The following list is not exhaustive but simply illustrative of the variety of the usable catalysts.

For the ethylene-propylene-1.4-hexadiene synthesis one cas see for example the Italian patent application No. 22204 A/81; likewise for the ethylene-propylene-1.3-butadiene synthesys.

Other patents on catalysts for the saturated and unsaturated copolymers synthesys are for example the Italian patent applications No. 20386 A/85 and No. 19473 A/84. Moreover we can also cite US patents No. 3,658,770 and No. 3.651.032.

As regards catalysts for the synthesys of polymers from cyclic olefines, bifunctional cyclic olefines one can see US patents No. 4,567,244, No. 4,607,112, No. 4.645,814.

As regards catalysts for the synthesys of polymers starting from vinyl-aromatic monomers (for example styrene) one can cite patent applications WO 88-10275, EP 361,309, 389,939, 417,724, 421,659 and the US patents No. 4,774,301 and No. 4,808,680.

As regards olefins, diolefins, acethylenes, polyenes and carbon monoxide one can mention patents EP 416,815, 418,044, 468,651, 277,003, 277,004, 468,537 and WO 92-00333.

As regards dienic monomers, unsaturated nitriles, unsaturated aliphatics or halogenated aromatics one can see patent EP 476,671 for the acrylic monomers (methylmethacrylate) and US 4,728,706.

For 1.3-butadiene, 1.5-hexadiene and 1.4-hexadiene one can see the following patent applications WO 88-04672, 88-04673, 88-04674 and 90-01337.

A further object of the present invention is represented by the fact that the described process permits to prepare also copolymers derived from homogenous catalysts, for example based on vanadium salts, preferably VOCl₃, vanadium acetylacetonate, vanadium alcoholate, which permit to obtain highly random polymers.

These products can be used as viscosity index improvers since in general have a molecular weight between 50,000 and 125,000 viscosimetric molecular weight. In this case the X₂ and X₄ characteristics are not present since these products are not usable as CFI.

In this case a stripping step is necessary to remove the residual monomer after the flash step.

By the process of the present invention one can obtain, if desired, products for CFI also with molecular weights &gt; 16,000, preferably of 20,000, but also up to about 80,000, preferably &lt; 70,000.

Also in this case for high molecular weights after the flash step it is necessary the stripping step.

These copolymers can be mixed in low percentages with the products of the invention with lower molecular weight to obtain physical mixtures suitable to treat particular gas oils.

The products having low molecular weight, preferably comprised from 600 to 6000, can be used as synthetic lubricant oils. Another application of the polymers having molecular weight, gnerally between 600 to about 40,000-50,000, is the use as additives for plastic materials and rubbers. Preferably the polymers in solution are used as additives, the obtainment of which has already been described for the CFI.

In the process of the present invention the catalyst components can be fed into the reactor containing the monomers, in the dry state (that is in the absence of solvents or liquid suspending agents) or in the dispersed state in a paraffinic hydrocarbon.

Such paraffinic hydrocarbon can be solid or liquid at room temperature, so the catalyst can be fed as suspension in liquid paraffinic oil or as dispersion in paraffin wax.

The suspension can be carried out also in high-boiling hydrocarbons both aliphatic and aromatic and naphtenic.

A device and a process to carry out such a feeding in the powder state of the catalyst component in the solid state which can be used in the process of the present invention is described in the Italian patent application No. 25522 A/77.

In practice one works by forwarding separately to the reactor the described catalyst solid component and the cocatalyst, for example alkylaluminium or its reaction products with water, pure or dispersed in paraffinic oil or dissolved in aliphatic or aromatic hydrocarbons.

The molar ratio between aluminium and the transition metal is comprised between 1 and 10,000, preferably between 50 and 500.

By separated feeding, a molecular weight regulator can be forwarded to the reactor, for example hydrogen or diethyle zinc, optionally also dispersed in paraffinic oil.

The amount of aliphatic, aromatic or naphtenic solvent foot polymerization grade permits to reduce the polymeric solution viscosity. If the polymerization is carried out at temperatures higher than those critical of the most low-boiling reactive monomers, then the solvent must have a boiling temperature higher than that said critical temperature. For example in the case of propylene, the solvent must have a temperature higher than the critical one.

During the polymerization reaction it is continuously fed ethylene and propylene, or butene-1 or the desired alpha-olefins or their mixtures, maintaining constant the composition in the reactor through a chromatographic control of the gas phase of the reactor itself; the polymer viscosity in the reactor is measured through a viscosimeter, for example applied in parallel which gives the desired molecular weight of the polymer.

This last part is used to establish a priori the molecular weight of the polymer which is produced in the reaction.

The polymeric solution-suspension coming from the reactor which can reach also, for example a content of 60% by weight of the polymer product depending on its molecular weight and on the reaction temperature, is fed in continuous, keeping constant the reactor level, into a pipe where occurs the flash or almost instant evaporation of the non-converted monomers.

In such section occurs the further concentration of the polymer into the high-boiling solvent used to assure a predetermined viscosity of the medium.

The flash pipe can be of the type described in the US patents No. 3,428,619 and 4,126,743.

The pressure inside the pipe is practically the atmospheric one, in any case lower than that of the polymer solution-suspension in the reactor. Also the vacuum can be used to obtain a pressure lower than the atmospheric one.

Such a pipe, for the purposes of the present invention, is provided with an external jacket in which a fluid flows, for example water/steam, oil, at a temperature comprised between 30°C and 200°C, preferably between 50°C and 150°C.

It can be linear or have a different form, have constant or increasing cylindric section.

The terminal section of the flash pipe can also be elbow-shaped, if desired.

Preferably, but not necessarily, together with the polymer solution-suspension it is introduced into the flash pipe a stream of warm fluid at a temperature between 30°C and 150°C, preferably and depending on the polymerization temperature, between 30°C and 100°C, for example gas propylene, propane.

The speed inside the pipe is preferably higher than 15 m/sec., preferably between 25 m/sec and 50 m/sec depending on the boiling temperature of the used solvent, on the viscosity of the polymeric solution and on the pressure difference between that of the reactor and that of the flash unit.

The solution-dispersion temperature at the end of the pipe is in the range of -10°C and +80°C.

At the exit of the flash pipe the polymeric solution-suspension is viscous and contains a very low quantity of monomers, generally lower than 3% by weight.

For this reason no stripping step is requested.

After this flash step, the polymeric solution is forwarded to a degasing unit at high temperature where, under vacuum and with an inert, for example wet nitrogen or wet air, takes place the removal of the last traces of unreacted monomers and the extinction of the catalytic residues.

The propylene recovered at the head of the flash pipe can be compressed and if necessary condensed and directly recycled into the reactor.

It is possible to use chemical grade propylene such as produced by cracking with a propane content of 5-6%. In the described process it is possible to reach a propane content of 40-50% by weight in the reacting mixture and a solvent content of 53% by weight without decreasing either of the catalytic activity or of the yield.

The volume of solvent and liquid monomer is about 50-60% of the total volume of the reactor.

The so obtained polymeric solution can be further diluted with solvent to obtain the desired title; and optionally other additives well known in the art can be added.

The process is particularly suitable to the preparation of ethylene-propylene copolymers containing from 10 to 90% by weight of propylene and preferably from 25 to 65%.

When a diene is present, the quantities are lower, generally of about 10% by weight.

The advantages of the process object of the present invention can be summarized: one can use all the known catalytic systems for the polyolefines synthesys provided they fulfill the requisite to give polymers with the above indicated X₂ and X₄ parameters, when the products are to be used as cold flow improvers; in the polymerization no foulness of the reactor occurs; the obtained polymer can reach also concentrations &gt;40% by weight in the final solvent and however the desired concentrations, optionally by adding solvent.

The process results particularly cheap, flexible to obtain saturated and unsaturated copolymers or terpolymers, ecologically attractive since it discharges nothing into the atmosphere other than the process drains eliminating in bar.

In the process object of the present invention, as already said, the stripping step with steam is eliminated, which step is essential for solution or suspension processes having the purpose to remove the unreacted monomers from the polymer.

As already said this step would be very expensive for low molecular weight polymers, of low reliability due to packing and/or demixing between the aqueous and the organic phases and very pollutant for the high quantity of water to be recycled.

The process of the present invention permits to avoid the expensive chemical depuration operations of the catalytic residues and the stripping.

The main advantage of the process object of the present invention is the possibility to prepare CFI in highly concentrated solutions but maintaining the high properties as CFI shown by the high molecular weight polymers.

The following experimental examples are reported to better illustrate the present invention but without limiting the same.

EXAMPLE A

The following test has been carried out in a 20 l pilot plant where ethylene, propylene, catalysts and molecular weight regulator were continuously fed. In a 20 l reactor are fed: <tables id="tabl0001" num="0001"><table frame="all"><tgroup cols="2" colsep="1" rowsep="0"><colspec colnum="1" colname="col1" colwidth="78.75mm" /><colspec colnum="2" colname="col2" colwidth="78.75mm" /><tbody valign="top"><row><entry namest="col1" nameend="col1" align="left">propylene</entry><entry namest="col2" nameend="col2" align="right">5.9 Kg/h</entry></row><row rowsep="1"><entry namest="col1" nameend="col1" align="left">ethylene</entry><entry namest="col2" nameend="col2" align="right">900 g/h</entry></row></tbody></tgroup></table></tables> catalyst component: <tables id="tabl0002" num="0002"><table frame="all"><tgroup cols="2" colsep="1" rowsep="0"><colspec colnum="1" colname="col1" colwidth="78.75mm" /><colspec colnum="2" colname="col2" colwidth="78.75mm" /><tbody valign="top"><row><entry namest="col1" nameend="col1" align="left">11.1% by weight of Ti supported on MgCl₂ prepared according to example 15 of patent 20386 A/85</entry><entry namest="col2" nameend="col2" align="left">0,0173 g/h (as catalyst of a 10% by weight suspension in vaseline)</entry></row><row><entry namest="col1" nameend="col1" align="left">Al-triisobutyl</entry><entry namest="col2" nameend="col2" align="left">4.16 g/h (as a 10% by weight Al-triisobu til solution in toluene)</entry></row><row><entry namest="col1" nameend="col1" align="left">hydrogen</entry><entry namest="col2" nameend="col2" align="left">50 g/h</entry></row><row rowsep="1"><entry namest="col1" nameend="col1" align="left">toluene</entry><entry namest="col2" nameend="col2" align="left">1 Kg/h</entry></row></tbody></tgroup></table></tables> Polymerization temperature and pressure were kept at 50°C and 58 Ate. The polymer concentration in the reaction mixture was 20% by weight. The average time into the reactor was 1 hour. The polymer solution-suspension is continuously discharged into a stainless steel flash pipe with cylindrical section, having a 20 mm diameter and a 6 m length and exchange coefficients between 500 and 2000 Kcal/h.m².°C. An external jacket of the same material in which flows water at 80°C keeps the flash pipe at such a constant temperature; the polymeric solution has a speed of 30 m/sec. at the entrance of the flash. At the end of the flash the remaining unreacted propylene monomer is about 2.5% by weight, determined by gaschromatography (GC). The dispersion-solution of the polymer coming from the flash pipe has a speed of 30 m/sec. From the flash pipe it is conveyed to a hopper kept at a temperature of 100°C. From the bottom of this hopper 1.7 Kg/h of a polymeric solution at 100°C were discharged with about 40% by weight of polymer. The so-obtained polymer contains 34% by weight of propylene with an intrinsic viscosity in tetraline at 135°C of 0.35. The viscosimetric average molecular weight was 13,000 calculated from the viscosity obtained according to the Moraglio formula cited in example 1.

EXAMPLE 1

The reactor temperature of Example A was maintained at 21°C and its total pressure was 12.9 Ate. The ethylene molar percent in the gaseous phase was 32.7%. The fed propylene was 5.4 Kg/h, ethylene was 1 Kg/h, toluene solvent was 1 Kg/h, the catalyst based on titanium salts supported on active magnesium chloride of example A was fed at 0,057 g/h. The molecular weight regulator, in this case zinc diethyl, was 2.5 g/h, as zinc diethyl of a 10% by weight toluene solution. The molar ratio between aluminium derived from aluminium triisobutyl used as cocatalyst and the titaniun of the catalyst was 150. The Al-triisobutyl was 3.29 g/h. The residence time was about 1 h. 2 Kg/h were obtained of polymeric solution at 50% by weight of polymer having an intrinsic viscosity in tetraline at 135°C of 0.4, with a viscosimetric molecular weight of 15,600, obtained according to the Moraglio formula published in "Chimica e Industria (Milano) <u>10</u>, 984 - 1959". The so-obtained copolymer showed a composition of 40% by weight of propylene; the solution at the end of the flash was 50% by weight of polymer in toluol. After flash the C₃ determined by GC in the polymeric solution was 2% by weight. The product was completely soluble in toluene at 25°C, the yield with respect to the catalyst was about 160 Kg of copolymer/g of titanium.

EXAMPLE 2

In a polymerization test analogous to the preceeding one, the reactor temperature of example 1 was 20°C with a total pressure of 12.5 Ate and a propylene feed of 5.8 Kg/h and ethylene 0.85 Kg/h. The percent by moles of ethylene in the gas phase was 19.4. The same catalyst of example 1 was fed in quantity of 0.07 g/h. As molecular weight regulator 2 g/h of zinc dietyl were used. The catalyst was the same as in example 1. The average ratio between aluminium triisobutyl and titanium was 150 and Al triisobutyl was 4.88 g/h. The residence time was about 1 hour. The used toluene quantity was 0.8 Kg/h. There were obtained 1.9 Kg/h of polymeric solution at 58% by weight of polymer in toluene. A polymer was obtained with 55% by weight of propylene with a yield of 140 Kg of copolymer/g of titanium. The product was completely soluble in toluene at 25°C and showed an instrinsic viscosity of 0.23 corresponding to a viscosimetric molecular weight of 7400 according to the Moraglio formula. After flash the C₃ in the polymeric solution was lower than 1%.

EXAMPLE 3

In a test similar to example 1 with a reactor temperature of 12°C and a total reactor pressure of 12.5 Ate the same catalyst of example 1 was used. There were fed 5.8 Kg/h of propylene, 1.28 Kg/h of ethylene, 0.017 g/h of the catalyst of example 1 and 3 g/h of zinc dietyl as molecular weight regulator. The molar ratio between aluminium, derived from aluminium triisobutyl used as cocatalyst and titanium was 260, the Al triisobutyl was 2.32 g/h. The used quantity of toluene was 0.8 Kg/h and the stay time was about 1 h. The ethylene percent in the gaseous phase was 46% by moles. 1.3 Kg/h of polymeric solution was obtained at 38% by weight of polymer in toluene. A copolymer was obtained with a yield of 260 Kg of product/g of titanium and a percent by weight of propylene of 30 with an intrinsic viscosity of 0.5 soluble for 95% by weight in toluene at 25°C. The viscosimetric average molecular weight was 21.000. After flash the C₃ was 1.5% by weight in the polymeric solution.

EXAMPLE 4

Example 3 was repeated using hydrogen as molecular weight regulator and a third monomer (butadiene). The temperature was 40°C and the total pressure was 18 Ate, the composition in the gas phase was 15% molar of ethylene, 20% molar of hydrogen and 1.2% molar of the third monomer, in this case butadiene. The fed quantities were 0.7 Kg/h of butadiene and 0.7 Kg/h of toluene. The stay time was half an hour. The reactor was continuously fed with 27 g/h of hydrogen, 9 Kg/h of ethylene, 11.5 Kg/h of propylene, 5 Kg/h of propane. The catalyst used was the same of example 1 in quantity of 0.031 g/h; the molar ratio between aluminium derived from aluminium triisobutyl and titanium was 100, the quantity of Al triisobutyl was 1.4 g/h. The yield was 120 Kg of copolymer/g of titanium with a content of propylene of 42% by weight. The third monomer content, butadiene, was 1.7% by weight. The obtained product was 1.1 Kg/h of polymeric solution at 36% by weight of polymer in toluene. The viscosity was 0.32 with a viscosimetric average molecular weight of 11,500 calculated according to the Moraglio formula. The product was completely soluble in toluene at 25°C.

EXAMPLE 5

The polymerization was carried out in an autoclave with 5 l volume, containing 1.3 l of n-hexane, using 50 mg of a catalyst consisting of an active magnesium chloride and supported on it a titanium tetrachloride with 3% by weight of titanium, obtained according to Italian patent No. 20203 A/81 with lower titanium percent, and 7 millimoles of aluminium triethyl as cocatalyst, corresponding to a molar ratio Al/Ti = 200. It is operated at 90°C, at a pressure of 15 Ate for a time of 3 hours, in the presence of hydrogen as molecular weight regulator. The ratio between the hydrogen and ethylene + propylene pressures was 1.5. In practice the pressure due to hydrogen was 10 atmospheres, of the remaining 5 atmospheres, 1/3 was due to ethylene. In the gas phase the ratio etylene:propylene was 1:3. At the end of the polymerization it was obtained a solution of copolymer in hexane at 25% by weight with a viscosity of 500 poise at 25°C. The polymer showed an intrinsic viscosity of 0.08 and a viscosimetric average molecular weight of 1780 and a composition of 38% by weight of propylene.