PROCESS FOR THE ANIONIC POLYMERIZATION OF MONOMERS

Abstract: In a process for anionic polymerization of a monomer by (a) reacting batchwise at a temperature >/= 50 °C a monomer and anionic initiator, and (b) then reacting continuously or semi-continuously the product of step (a) with additional monomer, polymers having a narrow molecular weight distribution are obtained by commencing step (b) by continuously or semi-continuously adding monomer to the product of step (a), whilst remaining a molar ratio unreacted monomer in step (a) to initiator charge to step (a) of at least 1:1.

Description: The invention relates to a process for the anionic polymerization of a monomer comprising the following steps:- (a) contacting and reacting in a batch mode a charge of monomer suited for anionic polymerization and a charge of anionic polymerization initiator at a temperature, which exceeds within the polymerization mixture locally at least 50 °C, to a conversion of 95.0 to 99.9%; and (b) subsequently contacting and reacting in a continuous or semi-continuous mode the product of step (a) with additional monomer to continue the anionic polymerization reaction at a temperature, which exceeds within the polymerization mixture locally at least 50 °C in such a way that a certain quantity of unreacted monomer is maintained in the mixture. A variety of valuable synthetic thermoplastic rubber products are conventionally produced by anionic polymerization of monomers such as conjugated dienes, alkenyl-aromatic compounds and activated mono-olefins. Anionic polymerization is characterized by the initiation and propagation of what are commonly termed living polymer chains. When the chains are initiated at substantially the same time and grow at substantially the same rate, the polymerization reaction yields a product having a very narrow molecular weight distribution. The molecular weight of each individual polymer chain is relatively close to the average molecular weight of the overall product, i.e., the total weight of the monomer(s) consumed divided by the mol of initiator used. Uniformity of the polymer molecules in the products of anionic polymerization is an important factor from the standpoint of many of the desirable physical properties of the materials. In the practice of anionic polymerization processes, it is often the case, however, that a portion of the living polymeric chains are terminated before they reach their desired, or "target", molecular weight. Moreover, because these terminated chains do not reach their target molecular weight, the polymerization mixture contains an excess of monomer which was intended for reaction with the terminated chains. This excess monomer adds onto the remaining live chains to form chains having a molecular weight higher than that originally targeted. The net effect of chain termination is then a broadening of the molecular weight distribution of the product both below and above the target. It is recognized in the art that the principal mechanisms for chain termination in anionic polymerization are (i) a reaction between the active anionic polymerization site of the living chain and one or more impurities in the polymerization system, and (ii) thermal die-out of the active site at the higher polymerization temperatures, e.g., temperatures greater than about 10 °C. Termination via the impurities reaction can usually be avoided or at least controlled within acceptable limits by maintaining the purity of the monomer, polymerization initiator, and diluent in the polymerization mixture. Termination via thermal die-out, which is thought to involve the elimination of the living anionic site from the chain through a reaction forming a hydride, is in many cases more difficult to bring under control. It is the principal object of this invention to minimize the incidence of chain termination reactions in certain anionic polymerization processes, particularly termination which can be attributed to a thermal die-out mechanism. The invention is intended for application to anionic polymerization processes which are initiated in a batch mode, and then subsequently continued in a continuous (or semi-continuous) mode. Such processes are well known in the art and are in common commercial practice. For the batch mode process step, predetermined amounts of (i) one or more monomers suitable for anionic polymerization and (ii) an anionic polymerization initiator, are contacted to form and propagate the living polymeric chain. This step is strictly a batch operation in the sense that all monomer and all initiator are brought into contact at the same time; no further addition of monomer or initiator takes place during this step, nor is any removal made from the contact mixture of polymerization product. The relative proportions of monomer and initiator used in this step are such that the chains do not reach their target molecular weight in the batch step alone, and polymerization is subsequently continued (with the same and/or different monomer) in a second step which is operated in a continuous or semi-continuous mode. This second reaction step is termed continuous in the sense that monomer is added (continuously, or also suitably intermittently) to the reaction mixture as the polymerization proceeds. However, no removal of product is made until the chains reach the target molecular weight. It has now been found that, as they are conventionally practised, anionic polymerization processes which comprise a batch polymerization step followed by a continuous polymerization step provide an unexpected opportunity for premature chain termination by the thermal die-out mechanism. More particularly, it has been observed that thermal die-out is not only the result of elevated temperatures within the exothermic polymerization mixture. In certain limited circumstances, the thermal die-out mechanism has now been found to be a function of the concentration of unreacted monomer in the mixture. At temperatures above 50 °C, the rate of occurrence of termination by thermal die-out is markedly increased when monomer concentration in the mixture is reduced below certain levels. In conventional anionic polymerization processes having a batch step followed by a continuous step, it has been the practice to continue the batch step until substantially all of the monomer in the mixture has been depleted before commencing additional monomer addition in the continuous step. Monomer depletion at the conclusion of the batch step in this anionic polymerization process has now been identified as a major factor contributing to chain termination reactions. Accordingly, the invention provides a process for the anionic polymerization of a monomer comprising the following steps:- (a) contacting and reacting in a batch mode a charge of monomer suited for anionic polymerization and a charge of anionic polymerization initiator, at a temperature, which exceeds within the polymerization mixture locally at least 50 °C to a conversion of 95.0 to 99.9%; (b) subsequently contacting and reacting in a continuous or semi-continuous mode the product of step (a) with additional monomer to continue the anionic polymerization reaction at a temperature, which exceeds within the polymerization mixture locally at least 50 °C, in such a way that a certain quantity of unreacted monomer is maintained in the mixture; and (c) finally, after the target molecular weight is reached, discontinuing step (b) and withdrawing the product of the anionic polymerization reaction, in which process step (b) is commenced continuously or semi-continuously by addition of monomer to the product of batch step (a) while the molar ratio of the unreacted monomer in step (a) to the initiator charge to step (a) remains at least 1:1. In other words, the invention entails ending the batch polymerization step (a) by adding additional monomer to commence the subsequent continuous or semi-continuous polymerization step (b) before the monomer concentration is depleted to a level which, on a molar basis, is less than the concentration of the charge of the polymerization initiator. This requirement will entail continuing the batch step to a conversion of at least 95.0 per cent but no greater than 99.9 per cent of the original monomer charge. More in particular, from EP-A-0048111, a process for continuously polymerizing a block copolymer, comprising at least two polymer blocks composed mainly of an aromatic vinyl hydrocarbon and at least one polymer block composed mainly of conjugated diene in an inert hydrocarbon solvent; comprising the steps of: (a) batchwise preparing a living prepolymer containing at least one aromatic vinyl hydrocarbon polymer block having a number average molecular weight of at least 5000 and a weight average molecular weight to number average molecular weight ratio of less than 1.5 by using a portion of monomers to be formed into the block copolymer in the presence of an organic lithium, followed by (b) continuously preparing the block copolymer in at least one polymerization vessel, arranged in a continuous polymerization zone by continuously polymerizing the remainder of the monomers by continuously supplying the prepolymer to the first polymerization vessel and simultaneously supplying the remainder of the monomers in the form of at least one monomer group selected from the group consisting of a monomer group composed mainly of the aromatic vinyl hydrocarbon and a monomer group composed mainly of the conjugated diene continuously and separately, to the subsequent polymerization vessel or vessels. From US-A-3356763, also a continuous process was known for the polymerization of certain selected conjugated dienes and vinyl-substituted aromatic hydrocarbons with an organolithium initiator in the presence of a hydrocarbon diluent, comprising the use of a prereaction zone, wherein the polymerization is initiated, and passing the effluent from said prereaction zone into an elongated, tubular reaction zone and recovering from the latter zone a reaction mixture containing a block copolymer. Thus, under prior art practices, the dependence of the thermal die-out mechanism upon monomer content has not been appreciated and as a result the monomer content of the batch polymerization step has not been closely monitored. However, in typical operation of such processes, transition from the batch step to the continuous step has generally been effected only after the monomer content of the batch reaction was essentially depleted, e.g., to a molar concentration level substantially less than that of the initiator charge, and very typically after a monomer conversion in excess of 99.99 per cent. Essentially complete depletion of monomer in the batch reaction in practice according to the prior art has proved to be convenient to process operations from the standpoint of monitoring and controlling the temperature of the exothermic polymerization system. There is the risk in such a process, if the second reaction step is commenced by addition of monomer to the polymerization system while a large quantity of monomer remains unconverted by the first, batch reaction step, that the rate of heat release may exceed the capabilities of the system for heat removal, resulting in higher than desired temperatures and possible degradation of the product. Complete depletion of monomer has also been used in the prior art as a means of preventing the formation of a "tapered" polymer block in cases of block copolymer preparation in which the continuous step involves a different monomer than that of the batch step. The performance of the invention with respect to minimizing the incidence of thermal die-out in this process and thereby improving the polymer product quality is considered unexpected in view of reports in the art, for instance that of US patent specification No. 3,687,913, that the occurence of chain termination reactions in anionic polymerization at elevated temperature is not affected by the concentration of the monomer in the reaction mixture. The process of the present invention is intended for application only to anionic polymerization processes, and only to processes in which the anionic polymerization of one or more monomers is commenced in a batch reaction step and thereafter continued in a reaction step characterized by operation in a continuous or semi-continuous mode. The process improvement of the invention specifically centres upon operations made in connection with the transition from the batch reaction step to the continuous reaction step. As a general rule, apart from practices in connection with such transition, the invention is suitably practised under conditions and procedures well known in the anionic polymerization art. In this respect, the invention is suitably applied to any one or more monomers which are susceptible to anionic polymerization. Useful monomers are known to include conjugated dienes, alkenyl-aromatics and activated alpha-olefins. Preferred conjugated dienes are those having from 4 to 12 carbon atoms per molecule, while the polymerization of conjugated dienes having 4 or 5 carbon atoms per molecule is generally of greatest commercial interest. Specific examples of preferred conjugated diene monomers are 1,3-butadiene, isoprene, 2,3-dimethyl-1,3-butadiene, 2-methyl-1,3-pentadiene, 2,3-dimethyl-1,3-pentadiene, 2-methyl-3-ethyl-1,3-pentadiene, and 2-phenyl-1,3-butadiene. Preferred alkenyl-aromatic monomers are the vinyl-substituted aromatic hydrocarbons such as styrene, 1-vinylnaphthalene, 2-vinylnaphthalene, 3 methylstyrene and the alkyl, cycloalkyl, aryl, aralkyl and arylalkyl derivatives thereof in which the total number of carbon atoms in the combined substituents is generally no greater than 12. Additional specific examples of such aromatic monomers include 3-methylstyrene, 3,5-diethylstyrene, 4-cyclohexylstyrene, 2,4,6-trimethylstyrene, 4-phenylstyrene, 2-ethyl-4-benzylstyrene, 4,5-dimethyl-1-vinylnaphthalene, 3,6-di-p-tolyl-1-vinylnaphthalene and 7-decyl-2-vinylnaphthalene. Other monomers suitable for anionic polymerization include, for example, acrylic and methacrylic esters, methyl vinyl ketones, vinylidene esters, nitroethylenes, and vinylidene cyanide, acrylonitrile and related cyano derivatives. From the standpoint of commercial interest, the invention is very advantageously applied to processes wherein the monomer or monomers used in both step (a) and step (b) is selected from the group consisting of butadiene, isoprene, styrene, and mixtures thereof. The polymerization initiators (also termed polymerization catalysts) suitably employed in the process according to the invention are likewise those which the art generally recognizes for anionic polymerization service. In general terms the initiator in any given process application is typically one or more alkali metals or organic alkali metal derivatives, preferably one or more organolithium compounds, and more preferably one or more monolithium compounds. Such initiators can, in the case of the monolithium compounds, be represented by the formula RLi or ROLi, wherein R is a hydrocarbon radical which can be aliphatic, cycloaliphatic, or aromatic. The carbon number of the hydrocarbon radical is not limited insofar as operability is concerned, although those of up to about 20 carbon atoms are generally preferred from the standpoint of availability. Aliphatic monolithium initiators form a particularly preferred class, including, for example, the specific compounds n-butyllithium, sec-butyllithium, t-butyllithium, n-decyllithium, eicosyllithium, lithium methoxide, and lithium ethoxide. Examples of aromatic initiators include phenyllithium, 1-naphthyllithium, and p-tolyllithium. A cycloaliphatic monolithium initiator is exemplified by cyclohexyllithium. Mixtures of initiators are very suitable. Still further, as is generally the case in the art, anionic polymerization in accordance with the invention is suitably carried out in the presence of an essentially inert diluent, comprising, for example, one or more diluents selected from the class consisting of alkanes, cycloalkanes, alkenes, and aromatic solvents. Specific examples of suitable diluents include propane, isobutane, n-pentane, n-hexane, n-heptane, 2,2,4-trimethylpentane (also referred to as "isooctane"), n-decane, cyclopentane, cyclohexane, methylcyclohexane, benzene, toluene, xylene and naphthalene. Diluent is typically used in a quantity such that the weight ratio of diluent to total monomer is in the range from 1:1 to 25:1, preferably in the range from 5:1 to 10:1. In the batch reaction step of the invention, the monomer, initiator and diluent are charged to a reactor which is equipped with means for stirring or otherwise agitating the polymerization mixture. The quantity of initiator charged to the reactor will determine the number of living polymer chains which form. The relative proportions of initiator and monomer charged will determine the molecular weight of the chains resulting from this process step. Preferably, the charge to the batch reactor has a molar ratio of monomer to initiator which is in the range from 40:1 to 10,000:1. For purposes of applying the invention as an improvement in such an anionic polymerization process, the batch polymerization step is, in whole or in part, necessarily conducted at a temperature of at least 50 °C. Specifically, it is the point in the operation of the process at which the batch reaction reaches a high level of monomer conversion e.g., 95 per cent or more, and is then discontinued by addition of monomer to commence the subsequent semi-batch or continuous step, that a temperature of at least 50 °C is critical. Only at temperatures in excess of 50 °C does the thermal die-out mechanism become a significant cause of polymer chain termination. Consequently, said semi-batch or continuous step also is conducted at a temperature of at least 50 °C. In one typical case, contact between the components for the batch polymerization step is commenced at a relatively low temperature, e.g., 30 °C. Temperature in the polymerization mixture then increases to levels greater than 50 °C, and very often to substantially greater levels, as the exothermic polymerization proceeds. It is therefore important to note with reference to this specification for process temperature that the invention is intended for application whenever local temperature in the polymerization mixture exceeds the 50 °C level, even though the average bulk temperature may be less than 50 °C. The invention is responsible for still greater improvements, in terms of inhibiting chain termination, at temperatures greater than 50 °C. In this regard, the invention is more beneficially applied to processes in which the batch polymerization temperature is at least 65 °C, and is still more beneficial in processes having a batch step in which temperature is at least 85 °C. Particular advantage is found in applying the invention to processes in which the batch polymerization step temperature reaches at least 95 °C, at the point of transition to the continuous or semi-continuous step. It is critical to the object of the invention for controlling chain termination by thermal die-out that polymerization in the batch mode not be continued beyond the point at which the number of molecules of unconverted monomer in the batch polymerization mixture remains at least as great as the number of living polymer chains in that mixture. In other words, it is necessary to maintain in the batch polymerization reaction mixture a content of unreacted monomer which does not fall below a level of 1 mol of monomer for each mol of the living polymer chains. Since the number of mol of living polymer chains is substantially equal to the number of mol of anionic polymerization initiator charged to the system, this requirement is alternatively, and more conveniently, expressed in terms of maintaining in the batch step of molar ratio of unreacted monomer to original initiator charge which is at least 1:1. The subsequent continuous or semi-continuous polymerization is commenced by addition of further quantities of monomer to the mixture, before the molar ratio falls below this 1:1 value. The occurence of thermal die-out reactions is now found to be markedly increased in reaction mixtures in which this ratio is allowed to fall significantly below this level. Still higher levels of monomer concentration are preferred in order to better inhibit the onset of increased thermal die-out. For instance, it is preferable that the monomer addition for the semi-batch or continuous polymerization step be commenced before the monomer level falls below a 2:1 ratio of mol of monomer to mol of initiator, more preferably before this ratio falls below 4:1, and most preferably before this ratio falls below 10:1. Although not strictly necessary to the practice of the invention, it is also generally preferable that the semi-batch or continuous polymerization step of the invention not be commenced too early in the process. If substantial quantities of unconverted monomer remain in the batch reaction mixture at the time when addition is made of further quantities of monomer, there is the danger of increasing the rate of reaction and the rate of heat generation and temperature build-up to unacceptable levels. It would also be undesirable in many cases to commence addition in a continuous or semi-continuous step of a monomer different from that remaining unconverted from the batch step. For such reasons it is generally desirable that the continuous or semi-continuous process step not be initiated before the monomer concentration falls to a level such that the molar ratio of monomer to initiator charge is less than 100:1, more preferably not until this ratio is less than 50:1, and most preferably not until this ratio is less than 20:1. In the application of this invention, these broader levels of remaining monomer concentration will correspond to continuing the batch step to conversions of the initial monomer charge which are in the range from 95.0 to 99.9 per cent. Conversions of monomer in the range from 98 to 99.9 per cent are common in preferred operations under the invention, while conversions in the range from 99.0 to 99.8 per cent are typical of the application of the invention to many particularly desirable operations. As will be understood by those skilled in the art, the progress of such batch polymerization reactions, e.g., in terms of the concentration of unreacted monomer, is often monitored by calculations based on known or predetermined reaction rates for the particular materials and conditions employed and by measurements of the rate of temperature change in the polymerization mixture, rather than on the basis of actual measurements of concentration in the ongoing reaction. Such methods of reaction monitoring and control have proved very useful in practice of this invention. The requirement for maintaining unreacted monomer in the polymerization mixture during operation at temperatures of 50 °C or more is, for purposes of this invention, satisfied by ending practice of the batch step before it depletes monomer to a concentration below the level associated with the desired ratio of monomer to initiator charge. The batch step ends, and the continuous or semi-continuous step begins with addition to the reactor of a quantity of monomer beyond that initially charged to the batch reactor. In the subsequent continuous or semi-continuous polymerization step, monomer (either the same monomer as, or a different monomer from that polymerized in the batch step) is added either intermittently or continuously to continue the growth of the living chains resulting from the batch step. As the term semi-continuous is used herein, it is intended to describe a process step in which monomer is intermittently or continuously added to and mixed with the living polymer chains in the polymerization reactor, for example, a single well-mixed vessel, if desired, the same reactor used in the batch step. The monomer is added to the mixture until the polymer chains reach a target molecular weight, and only then is monomer feed discontinued and product withdrawn. The term continuous, on the other hand, is intended to describe a steady state process in which there is essentially no change over time in the composition of the feed or exit streams from the reactor. A continuous anionic polymerization step is exemplified by passing the mixture resulting from the batch step, together with additional monomer, through a plug-flow tubular reactor. Procedures for carrying out anionic polymerization in a continuous reaction mode are described, for instance, in US patent specification No. 3,356,763 and the aforementioned US patent specification No. 3,687,913. Since the continuous or semi-continuous polymerization step is conducted at a local temperature of at least 50 °C, it is preferable that the rate of monomer addition in this step be "programmed" to maintain a quantity of unreacted monomer in the reaction mixture and thereby inhibit chain termination in this step of the process as well. Maintaining monomer content at a particular level in this process step is, however, not considered to be an aspect of the invention now claimed. Still, for best results in the overall process, monomer addition in the continuous or semi-continuous step should maintain a molar ratio of unconverted monomer to total initiator charge to the system which is at least 1:1, preferably at least 2:1, more preferably at least 4:1, and most preferably at least 7:1. Although it is suitably applied to any anionic polymerization process practiced in a two-stage (batch step and continuous or semi-continuous) manner, the invention is most advantageously applied to the preparation of block copolymers, that is, polymers wherein the molecule comprises at least two distinct blocks along the main polymer chain, each block a sequence representing the polymerization of different monomers or different types of monomers. The polymer chain may be, for example, a diblock polymer comprising two such blocks and having the general configuration A-B, a triblock polymer comprising three such blocks and having the general configuration A-B-C or A-B-A. The invention is considered particularly useful in the preparation of block copolymers of the configuration A-(B-A) n , wherein each A represents a monovinylarene polymer block, e.g., a polystyrene block, and each B represents a conjugated diene polymer block, e.g., a butadiene or isoprene block. Block copolymers of this type are described in more detail in US Reissue patent specification No. 27,145. The invention is further illustrated by reference to the following examples. Example 1 A mixture of styrene monomer and cyclohexane solvent was charged to a stirred reactor, followed by addition to the reactor of sec-butyllithium initiator. Temperature of the reactor was initially about 30 °C. A batch polymerization reaction commenced and continued under essentially adiabatic conditions to reach a styrene conversion of 99.8 per cent. At this point butadiene monomer and additional cyclohexane solvent were added to the batch polymerization mixture. Polymerization of the living chains then continued as temperature in the batch reaction rose to about 65 °C. At this point, the butadiene content of the mixture had decreased to a level corresponding to 100 mol of butadiene monomer per mol of initiator charge, and a continuous addition of butadiene was commenced. The process was continued in a semi-continuous mode, with addition of further butadiene monomer programmed to maintain a molar ratio of monomer content to initiator charge greater than 4:1. Examples 2 and 3 and Comparative Experiments A and B The advantages of the invention with regard to controlling the occurence of chain termination reactions in anionic polymerization are illustrated by the results of a series of four experiments. Two of these experiments (designated Comparative Experiments A and B) demonstrate the occurrence of chain termination reactions in prior art practice of anionic polymerization in a batch mode. The other two experiments (Examples 2 and 3) illustrate the advantages of the invention in the control of chain termination. For Comparative Experiment A, 0.16 mol of the polymerization initiator sec-butyllithium was charged to a jacketed stainless steel stirred reactor, together with 8 kg of butadiene. The mixture was allowed to react at a constant controlled temperature of 85 °C in a batch mode (i.e., without further addition of initiator or monomer or withdrawal of polymer product) for 25 minutes, during which the reaction reached a conversion of monomer calculated to be 99.991 per cent. Another 8 kg of butadiene monomer was then added to the mixture and the polymerization was allowed to continue for an additional 15 minutes before the reaction was terminated by addition of alcohol to the mixture. The resulting product was then analyzed by gel permeation chromatography (GPC) to determine the quantity of thermal die-out chain fragments. Overall, the initiator (0.16 mol) and the monomer (16 kg) were charged to the reactor in relative quantities designed to yield a target molecular weight for the product of about 100,000. The product analysis indicated, however, that 6.6 per cent of the living chains had been terminated (at a molecular weight of about 50,000) at the end of the initial 25 minutes batch reaction, when the molar ratio of unreacted monomer to original initiator charge was permitted to fall to 0.08:1. In Example 2, the reactor was again charged with 0.16 mol of initiator and a total of 16 kg of butadiene monomer. In this case, however, the monomer was added to the reactor continuously over a total of 30 minutes reaction time, in order to prevent depletion of monomer to undesirable levels at any time during the reaction, i.e., to maintain a molar ratio of unreacted monomer to initiator charge which is at least 1:1. The mixture was then maintained at 85 °C for an additional 10 minutes to consume all monomer. Analysis of the product after the total of 40 minutes reaction at 85 °C indicated that only 1.0 per cent of the chains has undergone termination at less than the target molecular weight. A comparison of the results of Comparative Experiment A and Example 2 illustrates the influence of monomer concentration in the polymerization mixture upon the thermal die-out mechanism of chain termination. Comparative Experiment B and Example 3 were similar to Comparative Experiment A and Example 2 respectively, although run at higher temperature (95 °C). In Comparative Experiment B, the reactor was charged with 0.16 mol of the sec-butyllithium initiator and 8 kg of the butadiene monomer. The mixture was batch reacted to essentially complete (99.999998 per cent, calculated) conversion of monomer over a period of 25 minutes. Addition was then made of a further 8 kg of monomer and the reaction continued to a total time of 15 minutes. Target molecular weight was again about 100,000. Analysis of the product of Comparative Experiment B indicated that chain termination had occurred in 13.6 per cent of the polymer molecules at a molecular weight of 50,000, at the time when monomer was depleted to a very low level, i.e., a molar ratio of unreacted monomer to initiator charge of 0.00002:1. In Example 3, a total of 6.8 kg of butadiene was charged continuously (377 g per minute) over the course of 18 minutes to the reactor containing the 0.068 mol of initiator, in order to prevent monomer depletion to undesirable levels. Analysis of the product showed that only 2.0 per cent of the molecules had undergone chain termination at a molecular weight substantially below the target of 100,000. Comparison of the results of Comparative Experiment B and Example 3 again illustrates the importance of maintaining monomer in the polymerization mixture as a means to inhibit thermal die-out and chain termination. These experiments also confirm that it is the thermal die-out mechanism which is responsible for the chain termination at low concentrations of monomer in the anionic polymerization mixture and which is inhibited by operating without depletion of monomer. For both the batch and continuous additions of butadiene, the percentage of die-out fragments found after reaction at 95 °C is about twice that found after reaction at 85 °C.

Claims: A process for the anionic polymerization of a monomer comprising the following steps: (a) contacting and reacting in a batch mode a charge of monomer suited for anionic polymerization and a charge of anionic polymerization initiator at a temperature which exceeds 50°C at least locally within the polymerization mixture to a conversion of 95.0 to 99.9 %; (b) subsequently contacting and reacting in a continuous or semi-continuous mode the product of step (a) with additional monomer to continue the anionic polymerization reaction at a temperature which exceeds 50°C at least locally within the polymerization mixture in such a way that a certain quantity of unreacted monomer is maintained in the mixture; and (c) finally, after the target molecular weight is reached, discontinuing step (b) and withdrawing the product of the anionic polymerization reaction, in which process step (b) is commenced continuously or semi-continuously by addition of monomer to the product of batch step (a) while the molar ratio of the unreacted monomer in step (a) to the initiator charge to step (a) remains at least 1:1. A process as claimed in claim 1 in which the continuous or semi-continuous step (b) is commenced by addition of monomer to the product of batch step (a) while the molar ratio of the unreacted monomer in step (a) to the initiator charge to step (a) remains at least 2:1. A process as claimed in claim 2 in which the continuous or semi-continuous step (b) is commenced by addition of monomer to the product of batch step (a) while the molar ratio of the unreacted monomer in step (a) to the initiator charge to step (a) remains at least 4:1. A process as claimed in claim 3 in which the continuous or semi-continuous step (b) is commenced by addition of monomer to the product of batch step (a) while the molar ratio of the unreacted monomer in step (a) to the initiator charge to step (a) remains at least 7:1. A process as claimed in claim 4 in which the molar ratio of unreacted monomer to initiator charge is less than 100:1. A process as claimed in any one of the preceding claims in which the molar ratio of unreacted monomer to initiator charge is less than 20:1. A process as claimed in any one of the preceding claims, in which monomer is added to the product of batch step (a) after between 98 and 99.9 per cent of the monomer charge to step (a) has been converted in the batch reaction. A process as claimed in claim 7, in which monomer is added to the product of batch step (a) after between 99.0 and 99.9 per cent of the monomer charge to step (a) has been converted in the batch reaction. A process as claimed in any one of the preceding claims, in which the polymerization reaction is carried out at a temperature of at least 65 °C at the time when step (b) is commenced. A process as claimed in any one of the preceding claims in which step (b) is a semi-continuous step. A process as claimed in any one of the preceding claims, in which the monomer in step (a) and step (b) is butadiene, isoprene, styrene or a mixture thereof. A process as claimed in any one of the preceding claims, in which the monomer reacted in step (b) is a different monomer from that reacted in step (a). A process as claimed in claim 11 or 12, in which butadiene and styrene are used as monomers in step (a) and (b), respectively.

Inventors: BEAN, ARTHUR ROBINSON, JR.
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1986
Main classification: C08F4
IPC codes: C08F2, C08F4, C08F297, C08F236, C08F36