Process for producing an impact copolymer

Abstract: A gas phase, two stage process for the production of polypropylene impact copolymer wherein fouling of a second stage recycle loop and heat exchange unit incorporated therein is reduced by the addition to substantially gaseous material passing through the loop of a small amount of an alkylene compound.

Description: This invention relates a process for producing an impact copolymer composition comprising a propylene homopolymer phase and a propylene/α-olefin copolymer phase in which the degree of fouling within the reactor system is reduced. Propylene polymer compositions have gained wide commercial acceptance in numerous applications because of their relatively low cost and desirable properties. Propylene homopolymers, however, have the disadvantage of being brittle with low impact resistance, particularly at low temperatures. Most proposals for modifying the properties of polypropylene homopolymer to improve impact strength have included the provision of a polypropylene/other /other α-olefin copolymer phase in an otherwise homopolymeric polypropylene. A propylene/ethylene copolymer phase is particularly useful for this purpose. The structure of such products is not entirely certain with some sources referring to a block copolymer and other sources referring to other structures. However, such materials are well known and of substantial commercial importance. They are referred to as polypropylene impact copolymers, regardless of the precise nature of their structure, and are said to contain a homopolymer phase (often polypropylene homopolymer) and a rubber phase (the copolymer phase). A typical process for the production of a polypropylene impact copolymer is conducted in at least two stages in at least two reactors. The homopolymer phase is conventionally produced first in one or more reactors and the product of this first stage together with any unreacted monomer is then passed to a second stage where the copolymer phase is produced. It is in the second stage that a large proportion of the processing difficulties for the overall process are encountered. In slurry, bulk or other solvent/diluent based processes, swelling and partial dissolution of the rubbery second stage product can take place. As a result, the polymer product of the second stage is tacky and adheres to the walls of the reactor and other internal surfaces, e.g. stirring blades. Reaction system fouling is also a problem in fluidized bed gas phase processes wherein the second stage reactor has a recycle loop in which unreacted gaseous monomers are passed through a heat exchange unit to remove heat of reaction and then returned to the second stage reactor. Conventional heat exchange units contain a large number of relatively small diameter tubes and these restrictive passages are particularly vulnerable to fouling. The relative proportions of homopolymer phase and copolymer phase, as well as to some extent the degree of fouling in the second stage reactor, can be controlled by the addition of various materials to the reactor. In general, such additives include catalyst deactivators which "kill" or reduce catalyst activity. US-A-4,551,509 discloses the addition of a polyalkylene glycol to the reaction mixture of a reactor system for producing ethylene homopolymers or copolymers in order to deactivate the catalyst. US-A-4,650,841 discloses the use of certain amides, polyalkylene polyols or epoxides for a similar purpose but the additive is introduced into a monomer recycle stream after removal from a stream of polymer product. US-A-3,962,196 proposes the use of heterocyclic additives such a N-vinylpyrrolidone to reduce polymer deposits on the interior walls of a polymerization reactor. In EP-A-225,099 the properties of a polypropylene impact copolymer are said to be improved by catalyst deactivation with a polyalkylene glycol ether in a specified quantity relative to the quantity of the titanium component of the polymerization catalyst. The process was a batch, liquid phase process and the glycol ether was introduced in between the first and second stages or added directly to the second stage reactor. As a part of the overall effect of this addition of glycol ether, the activity of the second stage polymerization catalyst is reduced to 30% to 80% of the catalyst activity before addition. In JP-A-8846211 there is described a process, which may be gas phase, in which a polyalkylene glycol ether is added continuously in specified ratio relative to the titanium in the catalyst to the second stage reactor. The addition may be between the first and second stage reactors or directly to the second stage reactor. In the gas phase modification of the process, preference is stated for adding the glycol ether to the recycle loop downstream from the heat exchanger. In this process as well, the catalytic activity of the second stage polymerization catalyst is reduced to 30% to 80% of the activity before glycol ether addition. The addition to the recycle loop appears to be for convenience only and the addition of the glycol ether to the recycle loop before passage through the heat exchange unit is not contemplated. There are substantial advantages to adding a catalyst deactivator to a recycle loop before reaching the heat exchanger. The amount of polymerization catalyst present in this recycle stream is necessarily small and consists mainly of catalyst fines and particles containing only a partial coating of polymer. As a result, the amount of catalyst deactivator needed to reduce the activity of the catalyst present in the recycle loop and therefore reduce fouling of the heat exchange tubes is also small. Particularly when the catalyst deactivator is efficient is the activity of the second stage reactor not substantially adversely influenced by catalyst deactivator which is eventually passed to the second stage reactor. It is known from EP-A-431626, that the addition of small amounts of certain aromatic esters, such as ethyl p-ethoxybenzoate, to the recycle loop upstream from the heat exchange unit is beneficial in reducing fouling of the heat exchange tubes without unduly adversely affecting the activity of the second stage polymerization catalyst. Nevertheless, it would be of advantage to provide more efficient catalyst deactivators for introduction into the recycle loop between the second stage reactor and the heat exchange unit in order more effectively to reduce the degree of fouling of the heat exchanger tubes. According to the present invention there is provided a process for producing an impact copolymer composition in a two stage gas phase process wherein a propylene homopolymer phase is produced in a first stage reactor and a copolymer phase is produced in a second stage reactor by the copolymerization of propylene and other α-olefin and wherein heat is removed from the second stage reactor by removing therefrom a portion of primarily gaseous material, passing said material through a recycle loop containing a heat exchange unit and returning cooled material to the second stage reactor, characterised in that an alkylene compound (as defined below) is introduced into the recycle loop ahead of the heat exchange unit. The polymerization process is conducted in the presence of a stereoregular olefin polymerization catalyst. Such catalysts are broadly well known and conventional and are employed in the polymerization of α-olefins of three or more carbon atoms to produce stereoregular products. In terms conventionally employed to describe such catalysts, the stereoregular catalysts of high activity contain as a first constituent a procatalyst which is a titanium-containing solid, usually a titanium halide-containing solid, and which often contains an electron donor. Suitable electron donors include ethers, esters, ketones, phenols, amines, amides, imides, nitriles, phosphines, phosphites, stilbenes, arsines, phosphoramides and alcoholates, which may be used singly or in combination. Preferred electron donors are aromatic esters and particularly preferred are ethyl benzoate and isobutyl phthalate. The second catalyst constituent, termed a co-catalyst, usually is an organoaluminum compound which may be partly or totally complexed with a third catalyst constituent, conventionally termed a selectivity control agent. Illustrative selectivity control agents include aromatic esters, amines and particularly hindered amines, aliphatic esters, phosphites, phosphates, silanes, particularly alkoxysilanes and aryloxysilanes, hindered phenols and mixtures of two or more thereof. Such stereoregular olefins polymerization catalysts are described in numerous patents and other references including US-A-4,728,705. Although various chemical compounds are useful as the constituents of the polymerization catalyst, a typical stereoregular olefin polymerization catalyst contains as a procatalyst a solid comprising magnesium halide, a titanium halide and an electron donor such as ethyl benzoate. The halide moieties of such procatalysts are customarily chloride moieties. The co-catalyst is typically triethylaluminum or triisobutylaluminum which is often at least partially complexed with an aromatic ester such as ethyl p-ethoxybenzoate or methyl p-methylbenzoate or with a silane such as diisobutyldimethoxysilane as the selectivity control agent. Use of a catalyst of this type results in a stereoregular polymeric product when α-olefins of three or more carbon atoms are polymerized. Many of the stereoregular olefin polymerization catalysts are also recognized as high activity catalysts capable of producing polymers of desirable properties without the necessity of removing catalyst residues of a de-ashing step. The polymerization process to which the present invention is applied is a gas phase process. A number of gas phase processes are available but one such process which is illustratively and suitably used in accordance with the invention is described in US-A-4,379,759 and is a fluidized bed, continuous gas phase process. A gas phase process is typically operated by charging to a suitable reactor an amount of preformed polymer particles and a lesser amount of catalyst components. The olefin(s) to be polymerized as a gas is (are) passed through the bed of particles at a high rate and under conditions of temperature and pressure sufficient to initiate polymerization. Upon passing through the particle bed the unreacted gas is withdrawn from the reactor and recycled together with make-up feed gas. As catalyst is lost through incorporation of a minute amount of catalyst in the polymer product, additional catalyst is provided to the reactor, often through the use of an inert transport gas such as nitrogen or argon. The reaction temperature is suitably from 30°C to 120°C, preferably from 50°C to 90°C. The reaction temperature is maintained within this range at least in part through the use of a recycle loop. A portion of gaseous monomer is removed from the reactor, after passage through the particle bed, together with small amounts of entrained catalyst which primarily comprises catalyst fines and particles of catalyst which are only partly covered by polymer. The withdrawn monomer stream is then passed through a heat exchange unit to remove heat of reaction and returned to the reactor. It is the detrimental fouling of this recycle loop in the second stage reactor which is addressed by the present invention. The second stage reaction pressure is generally up to 6.9 MPa (1000 psi), with pressure from 0.69 to 27.6 MPa (100 to 400 psi) being preferred. An additional means of process and product control is achieved by providing for the addition of molecular hydrogen to the reactor and thus to the polymerization system. The addition of molecular hydrogen serves to control the molecular weight of the polymeric product and, in the second stage reactor, the relative proportions of homopolymer and copolymer portions. Although it is not desired to be limited by any particular theory it is likely that the molecular hydrogen serves as a chain transfer agent. The precise control of reaction conditions, the rate of addition of catalyst, feed gas and molecular hydrogen as well as the rate of recycle of unreacted monomer is broadly within the skill of the art. The gas phase process of the invention is operated as a two stage process wherein each stage operates in the gas phase in one or more reactors. In the first stage the homopolymer phase is produced which is predominantly but not necessarily propylene homopolymer. To obtain products of particular properties it may be useful to incorporate in the otherwise homopolymer portion a small amount, e.g. up to 6% by weight, of a second α-olefin such as ethylene, 1-butene or an even higher molecular weight α-olefin. The optional incorporation of other α-olefin is by conventional methods and serves to modify but not substantially change the properties of the homopolymer portion. When a small amount of other olefin is present, the polymer product is still referred to as the homopolymer phase although technically it is copolymeric. Homopolymeric phases produced substantially entirely from propylene, i.e. phases produced in the substantial absence of other α-olefin, are preferred. The olefin feed to the first stage reactor is passed through a particle bed therein and the desired polymer product is formed by growth of polymer product on the polymer particles provided to the reactor or as particles formed in the reactor. A portion of the product is formed by coating, either partially or completely, the catalyst particles provided to the reactor. The polymer product is removed from the reactor at a rate substantially equivalent to the rate of polymer production and passed to the second stage reactor. The product of the second stage reaction, which also may be conducted in one or more reactors, is predominantly a copolymer of ethylene and propylene although small amounts of other α-olefin moieties could optionally be present. Through control of the proportion of unreacted propylene from the first stage reaction and the proportion of ethylene provided to the copolymerization reactor it is possible, and conventional, to vary the proportion of ethylene in the ethylene/propylene copolymer phase. Within the impact copolymers produced according to the invention the proportion of ethylene in the copolymer phase is suitably from 35% to 95%, preferably 35% to 65%, by weight based on the total copolymer phase. It is also conventional to control the molecular weight of the copolymer phase as by introduction of molecular hydrogen and to control the relative amounts of the homopolymer and the copolymer phases. The copolymer phase of the total polypropylene impact copolymer is suitably from 10% to 60%, preferably 10% to 40%, by weight of the total impact copolymer composition. The polymerizations which take place in both reaction stages are exothermic reactions and some provision must be made for removal of the accumulated heat of reaction. Various methods are useful for this purpose but one method which is particularly useful is to remove from the reactor at least a portion of the primarily gaseous material which has passed through the catalyst bed and convey such material through a conduit which includes a compressor and a heat exchange unit and then return the relatively cool primarily gaseous material to the reactor for additional passage through the catalyst bed. This conduit is typically termed a recycle loop whose function is to maintain a desired reaction temperature by removal of heat by the heat exchange unit, and to provide gas flow for bed fluidization for that class of gas phase polymerizations. The primarily gaseous material comprises, as the major component, unreacted monomer gases that have passed through the catalyst bed. However, this material will also contain entrained particles of active catalyst, particularly those small irregular catalyst particles often referred to as "fines" as well as catalyst particles which are partially although not completely covered with polymer product. It is this mixture of monomer and active catalyst that leads to fouling of the reactor recycle loop, particularly the relatively small diameter passages of the heat exchange unit. Although this potential for fouling exists in both the first and the second stage reactor recycle loops, the nature of the homopolymer product of the first stage reactor is such that fouling is a rather minor problem. However, in the recycle loop of the second stage reactor a substantial problem exists and it is to this recycle loop fouling that the present invention is directed. The product of the second stage reactor is rather rubbery in character and, being somewhat "sticky" and "tacky", it can and will adhere to the walls of the conduit which comprises the second stage reactor recycle loop. Over time the buildup of such undesirable polymer will foul and eventually clog the heat exchanger tubes. As heat exchanger tubes accumulate fouling deposits, the pressure drop across the heat exchanger increases, and the deposits reduce the cooling efficiency of the heat exchanger, since they form an insulating boundary. With continued operation a point would be reached where either the pressure drop across the heat exchanger exceeds the compressor operational limit or the heat exchanger efficiency falls below the acceptable limit. In either event, the polymerization unit must be shut down. The present invention provides a selective catalyst deactivator introduced near the entrance and preferably within the recycle loop ahead of the heat exchanger, which will "kill" the catalyst entrained in the primarily gaseous material entering the recycle loop and thereby retard the production of rubbery copolymer within the recycle loop and reduce the fouling which would otherwise take place within that loop, particularly within the heat exchange unit component of the loop. Because the amount of active polymerization catalyst is rather small the amount of catalyst deactivator required is also small so that the fouling of the recycle loop can be retarded while not unduly reducing the catalytic activity within the second stage reactor. The process of the invention therefore comprises the provision of certain alkylene materials as catalyst deactivators introduced within the recycle loop or near the entrance thereof, but in all cases ahead of the heat exchanger, in quantities sufficient substantially to reduce or eliminate the catalytic activity of polymerization catalyst entering and passing through the recycle loop. The catalyst deactivator is provided by continuous or intermittent injection of substantially liquid deactivator into the substantially gaseous material entering the recycle loop. Contact of this deactivator and entrained catalyst particles serves to reduce or eliminate the catalyst activity of such particles as well as production of rubbery copolymer within the recycle loop and the fouling that results from the production of polymer. The catalyst deactivators to be provided to the recycle loop are alkylene compounds which are alkylene glycols and alkylene glycol derivatives of alkylenediamines, or ether or ester derivatives thereof. The alkylene glycols and their derivatives can be represented by the formula wherein n is 2 or 3, each R independently is hydrogen, alkyl of up to 20 carbon atoms or acyl of up to 20 carbon atoms, and each x is a number from 1 to 10. Formula (I) includes compounds wherein random incorporation (in a statistical sense) or blocked sequences of different alkylene oxide species, e.g. propylene oxide and ethylene oxide, are copolymerized as part of the structure. At least one R is preferably alkyl or acyl. The alkylene glycol derivatives of alkylenediamines or derivatives thereof can be represented by the formula wherein R, n and x are as previously defined and y is 0 or a number from 1 to 10 including the compounds having random or blocked sequences of different alkylene oxide species. Illustrative R groups include such alkyl groups as methyl, ethyl, hexyl, octyl and tetradecyl as well as such acyl groups as acetyl, butyryl and dodecanoyl. The term n is independently 2 or 3 but within any given alkylene moiety n will be constant. The term x represents the total number of alkylene oxide moieties present and may be an integer but may also be an average of alkylene oxide moieties in a mixture of compounds so that x is not necessarily a whole number. Suitable alkylene glycol compounds and ether and ester derivatives thereof are illustrated by ethylene glycol, propylene glycol, diethylene glycol, tetrapropylene glycol, hexaethylene glycol, decapropylene glycol, ethylene glycol monomethyl ether, diethylene glycol dihexyl ether, tripropylene glycol monooctyl ether tetradecaethylene glycol dipropyl ether, ethylene glycol monoacetate, dipropylene glycol dibutyrate, tetraethylene glycol monohexanoate and hexapropylene glycol didecanoate. Mixtures of any of the above, and particularly of mono and di-esters and ethers, are contemplated in this invention. In general, the alkylene glycol ethers and esters are preferred over the corresponding alkylene glycols. Also preferred are those alkylene glycol compounds or ether and ester derivatives thereof wherein the term x is a whole number from 1 to 4 and each n is 2 or 3. Especially preferred are dipropylene glycol mono and diethers, and diethylene glycol mono and diesters. The alkylene glycol derivatives of alkylene diamine are illustrated by compounds such as N,N,N',N'-tetra(2-hydroxyethyl)ethylenediamine, N,N,N',N'-tetra(3-hydroxypropyl)-1,3-propylenediamine, N,N'-di(2-methoxyethyl)ethylenediamine, N,N,N'-tri(3-propanoylpropyl)propylenediamine, N-(2-hydroxyethyl)-N,N'-di (2-propyloxyethyl)ethylenediamine and N,N,N',N'-tetra(2-acetyloxyethyl)propylenediamine. In the case of these alkylene glycol derivatives of alkylene diamine, those compounds of formula II wherein each R is hydrogen are preferred as are derivatives of ethylenediamine. A particularly preferred class of such compounds is produced by sequential reaction of propylene oxide and ethylene oxide with ethylenediamine. Certain of these compounds are commercially available and are marketed by BASF/Wyandotte under the trademark TETRONIC ® Polyols. The catalyst deactivator is introduced into the second stage recycle loop at a point between the entrance to the loop from the second stage reactor and the heat exchanger. The precise point of introduction is not critical, but best results are obtained when the point of introduction is near the compressor inlet, wherein the compressor is situated ahead of the heat exchanger in the recycle loop. The amount of catalyst deactivator is rather small because of the relatively small amount of catalyst present in the recycle loop stream. Amounts of the catalyst deactivator continuously added should be at least nearly equimolar with aluminum alkyl carry-over to the recycle loop with fines (0.5/1 to 12.0/1 on a molar ratio basis of deactivator to aluminum alkyl). It is preferred that the ratio be from 0.7/1 to 2.0/1. The catalyst deactivator is suitably applied by introducing it simultaneously with the passage of unreacted monomer through the recycle loop and the addition is preferably continuous for so long as material passes through the recycle loop, although addition of catalyst deactivator in increments at short intervals is also satisfactory. It appears likely that the added catalyst deactivator serves to coat the walls of the recycle loop and the catalyst particles entrained in the gaseous material passing through the recycle loop and thereby reduce or prevent the formation of copolymer in the recycle loop and particularly in the heat exchange unit through which the gaseous material passes. In any event, however, the fouling of the recycle loop is substantially reduced, which enables extended operation of the process without the need for shut-down to remove fouling deposits, and any small amount of the catalyst deactivator which does pass through the recycle loop and back to the second stage reactor is sufficiently small so as not to substantially reduce the activity of the catalyst in the second stage reactor. The net effect of the addition of catalyst deactivator to the recycle loop of the second stage reactor is to permit operation for longer periods because of reduced fouling while maintaining a high catalyst activity in the second stage reactor. These improvements are most easily recognized in the improved economics of the overall polymerization process. The invention is further illustrated by the following Comparative Example and Examples which should not be regarded as limiting. Comparative Example In order to demonstrate the effect of employing a small amount of a catalyst deactivator in the second stage recycle loop, a production run was made wherein polypropylene impact copolymer was produced utilizing a commercial-type, high activity, stereoregular olefin polymerization catalyst. The catalyst deactivator ethyl p-ethoxybenzoate was used as the deactivator. The degree of fouling in the recycle loop was measured as a function of the increase in pressure drop across the heat exchanger incorporated within the loop. No increase in the pressure drop is interpreted as evidence of little or no fouling. The ethyl p-ethoxybenzoate was introduced into the reactor loop upstream from the heat exchanger in a quantity of 0.09 kg/h (0.2 1b/h), which is approximately equimolar relative to the aluminum content of the catalyst particles entrained in the vapors passing through the recycle loop. For so long as the addition of ethyl p-ethoxybenzoate was continued, no increase in the pressure drop across the heat exchanger was observed. As a test, the addition of the ethyl p-ethoxybenzoate was stopped. After a one day induction period, the pressure drop increased 20.7 kPa (3 psi) over a 3 day period. At this time the flow of ethyl p-ethoxybenzoate was restarted and after 4 hours no further increase in pressure drop was observed. Example 1 To compare the relative effectiveness of candidate catalyst deactivators in deactivating commercial-type, high activity, stereoregular olefin polymerization catalysts, a series of experiments was conducted, for convenience, in a gas phase, fluidized bed reactor lined-out under polypropylene homopolymerization conditions substantially similar to those of a commercial production. The several candidate deactivators were diluted in isopentane and charged to the reactor after polymerization was proceeding. The flow of propylene feed and the hydrogen employed for molecular weight control continued, but no additional catalyst agents were added and product discharge from the reactor was halted. As a measure of continuing catalyst activity, the increase in the weight of the polymer bed was determined over time. A relatively large increase in bed weight is considered to reflect continued polymer production and catalyst activity and therefore demonstrate a relatively ineffective catalyst deactivator. A relatively low gain in bed weight is considered to reflect loss of catalyst activity and thus an effective catalyst deactivator. The candidate catalyst deactivators tested were A. Ethyl p-ethoxybenzoate (control), B. Dipropylene glycol monomethyl ether, C. Diethyleneglycol laurate: 35-40%w monoester, 50-55%w diester, 8%w laurate soaps (K or Na), 2%w free fatty acid, and D. Diisobutyldimethoxysilane (control). The results of the evaluation are shown in Table 1. Catalyst deactivator ppm by mole basis propylene Weight gain in 1 hour kg (lbs) None, 0 13.65 (30.09) A, 50 11.87 (26.16) A, 75 4.94 (10.89) A, 100 4.94 (10.89) B, 25 10.28 (22.67) B, 50 4.42 (9.74) C, 25 11.59 (25.56) C, 50 7.83 (17.27) D, 250 12.68 (27.95) D, 500 12.29 (27.10) Example II To determine the relative effectiveness of several candidate catalyst deactivators on the catalytic activity of several commercial-type, high activity, stereoregular olefin polymerization catalysts, production of propylene/ethylene copolymer was conducted in a 1 liter autoclave. For convenience, the candidate deactivators were added directly to the autoclave during production of a copolymer which was 40% by weight ethylene. The reactor was designed to maintain a constant propylene pressure and an ethylene pressure that was stoichiometric relative to the propylene. Propylene was added, and correspondingly ethylene, as required to maintain the desired pressure. The relative efficiency of the catalyst deactivator was measured by the decrease of the rate of propylene fed to the reactor. A constant feed rate was taken as an indication of constant polymer production and catalytic activity and therefore an inefficient catalyst deactivator. A large decrease in propylene feed rate was interpreted as indicative of a substantially reduced rate of polymer production and therefore an effective catalyst deactivator. The results of the evaluation are shown in Table II wherein the term "Ratio" is the weight ratio of catalyst deactivator to titanium in the polymerization catalyst. The deactivators tested were A. Ethyl p-ethoxybenzoate (control), B. Dipropyleneglycol monomethyl ether, and C. Diisobutyldimethoxysilane (control). Deactivator Ratio Propylene flow rate decrease, % Catalyst 1 C 271.25 46.6 C 1111.25 75.0 C 2231.25 93.5 A 271.25 40.0 A 1111.25 64.0 A 2231.25 68.0 B 61.25 60.4 B 271.25 94.0 B 1111.25 93.5 Catalyst 2 C 271.25 50.0 C 1111.25 81.0 C 2231.25 82.6 A 271.25 61.9 A 1111.25 74.4 B 61.25 27.0 B 271.25 74.2 B 1111.25 100.0

Claims: A process for producing an impact copolymer composition in a two stage gas phase process wherein a propylene homopolymer phase is produced in a first stage reactor and a copolymer phase is produced in a second stage reactor by the copolymerization of propylene and other α-olefin and wherein heat is removed from the second stage reactor by removing therefrom a portion of primarily gaseous material, passing said material through a recycle loop containing a heat exchange unit and returning cooled material to the second stage reactor, characterised in that an alkylene glycol of the formula or an alkylene glycol alkylenediamine derivative of the formula wherein each R independently is hydrogen, alkyl of up to 20 carbon atoms or acyl of up to 20 carbon atoms, n is 2 or 3, each x is a number from 1 to 10 and each y is 0 or a number from 1 to 10 is introduced into the recycle loop ahead of the heat exchange unit. A process according to claim 1 wherein the alkylene glycol is the product of sequential polymerization of propylene oxide and ethylene oxide with ethylenediamine. A process according to claim 1 wherein the alkylene glycol is a diethylene glycol mono- or di-ester or a dipropylene glycol mono- or diether. A process according to any one of the preceding claims wherein the alkylene glycol is introduced in a molar ratio of 0.7/1 to 2.0/1 relative to the aluminium alkyl catalyst carried over into the recycle loop.

Inventors: MCCULLOUGH JAMES DOUGLAS JR, MCCULLOUGH, JAMES DOUGLAS, JR.
Applicants: SHELL OIL CO, SHELL OIL COMPANY
Application year: 1991
Main classification: C08F2
IPC codes: C08F210, C08F10, C08F2