TREATING AN EMULSION OF ONE OR MORE MONOMERS

Abstract: A process of treating an emulsion of one or more monomers is characterised by: (a) at least about 80 weight per cent of the one or more monomers have been polymerised; (b) subjecting the emulsion to temperature and pressure conditions at which the vapour pressure of water in the ambient environment is less than the vapour pressure of water in the emulsion without significantly degrading or destabilising the emulsion; and (c) introducing in the emulsion at least about 0.01 parts by weight of a free radical generator per 100 parts by weight of polymer in the emulsion per hour of treatment until the residual monomer content is not more than about 0.05 per cent by weight based on the emulsion. Graphs exemplify increased efficiency which is given by the process.

Description: The present invention pertains to the minimization of residual monomer in polymeric emulsions. Emulsion polymerization systems are well known for the production of many types of polymers e.g. rubbery styrene-butadiene polymers and polymers containing acrylonitrile. In commercially used processes it is desirable to minimize the amount of residual monomer in the latex. This is desirable from an environmental point of view to minimize exposure to hydrocarbon monomers which may be odiferious or may present more serious health concerns. From an economic point of view the saving of 1 to 0.5 per cent of free monomer is a significant cost saving to a plant. The current methods of reducing the residual monomer in a latex tend to be time consuming and slow down production. Furthermore, these processes tend to be energy intensive adding a further cost burden to the product. It is desirable to find a faster and less energy consuming method of reducing the residual monomer content in latices. Most preferably it is desirable to find a process that would tend to polymerize most of the residual monomer rather than trying to physically remove it. The paper "Monomer Removal from latex" by S. M. Englund, Chemical Engineering Progress, Aug. 1981 pg. 55, presents a good discussion of some of the problems the industry faces. In a latex the removal of residual hydrocarbon monomer is limited by the rate at which the latex can be contacted with a fresh stream of a fluid, usually steam, to remove that monomer. Thus the latex may be contacted with relatively high amounts of steam to ensure adequate removal of monomer. This may lead to many different types of problems such as foaming, latex destabilization or latex degradation. The B.F. Goodrich Company have developed a number of methods to remove residual acrylonitrile from aqueous polymeric emulsions. U.S. Patent 4,251,412 discloses a process for the reduction of residual acrylonitrile in a latex by adding a stoichiometric amount of amine to react with the acrylonitrile. U.S. Patent 4,272,425 discloses a process for reducing the acrylonitrile content in a latex by adding additional catalyst and co-monomer in excess of the free acrylonitrile after 90 per cent conversion of the monomers. U. S. Patent 4,278,582 discloses a process for reducing the residual acrylonitrile content of a latex by adding thereto ammonia, ammonium hydroxide, thiols. H₂S or alkali or alkaline earth metal carbonates, phosphates, and silicates. In addition to the foregoing, DD-A-132,588 teaches reducing the residual vinyl or vinylidene chloride content in emulsion polymers of vinyl or vinylidene chloride by introducing above the emulsion propylene at a pressure less than the monomer saturation pressure. DE-A-2,043,172 teaches reducing the residual vinyl acetate concentration in an emulsion polymerization by introducing additional ethylene subsequent to polymerization. EP-A-28,348 teaches reducing residual ACN in NBR type emulsion polymers by introducing additional butadiene and initiator following polymerization. The present invention provides a process of treating an emulsion of one or more monomers, in which : (a) at least about 80 weight per cent of said one or more monomers having been polymerized, said one or more monomers being selected from: C₈₋₁₂ vinyl aromatic monomers which may be unsubstituted or substituted by a C₁₋₄ alkyl or hydroxyalkyl radical or a chlorine or bromine atom; C₄₋₈ conjugated diolefins; C₃₋₉ ethylenically unsaturated carboxylic acids; C₃₋₉ ethylenically unsaturated aldehydes; amide derivatives of C₃₋₉ ethylenically unsaturated carboxylic acids which may be unsubstituted or further substituted at the nitrogen atom by a C₁₋₄ alkyl, alkanol, or alkylol radical; C₁₋₈ alkyl or alkanol esters of C₃₋₉ ethylenically unsaturated carboxylic acids in which the alkyl or alkanol radical may be branched or straight chained; and C₂₋₈ ethylenically unsubstituted nitriles; (b) subjecting said emulsion to temperature and pressure conditions at which the vapour pressure of water in the ambient environment is less than the vapour pressure of water in the emulsion without significantly degrading or destabilizing the emulsion; characterised by (c) incremently introducing into the emulsion, without the introduction of additional monomer, at least about 0.01 parts by weight of a feee radical generator per 100 parts by weight of polymer in the emulsion per hour of treatment until the residual monomer content is not more than about 0.05 per cent by weight based on the emulsion. As used in this specification, the term "free radical generator" is intended to include a free radical generating agent per se and/or a combination of two or more chemicals which generates free radicals such as a peroxide and a reducing agent. If two or more chemicals are used in the free radical generator the amount of agent specified refers to the total addition of all agents. The process is particularly useful in situations where one or more monomers are soluble in the resulting polymer. In these cases, the treatment is continued until the residual content of the monomer soluble in the polymer is not more than about 0.05 weight per cent based on the emulsion. Preferably the process is used with emulsions of a polymer formed by polymerizing a monomeric mixture comprising: 30-100 weight per cent of one or more monomers selected from C₈₋₁₂ vinyl aromatic monomer, C₂₋₈ ethylenically unsaturated nitrile or a mixture thereof; 0-60 weight per cent of a C₄₋₈ conjugated diolefin; 0-10 weight per cent of one or more monomers selected from C₃₋₉ ethylenically unsaturated acid, C₃₋₉ ethylenically unsaturated aldehydes, amide derivatives of said C₃₋₉, ethylenically unsaturated acids, and C₁₋₈ alkyl or alkanol derivatives of C₃₋₉, ethylenically unsaturated carboxylic acids. The preferred vinyl aromatic monomers are styrene, α-methyl styrene, p-methyl styrene, chlorostyrene, bromostyrene, and divinyl benzene. The preferred nitrile is acrylonitrile. Preferably these monomers are initially present in an amount from 30 to 100 weight per cent of the total monomer composition. The preferred dienes are isoprene and butadiene. These monomers may be present in an amount up to about 60 weight per cent of the total monomer mixture. The initial monomer mixture may optionally contain up to 10 weight per cent of a functional monomer. Functional monomers are e.g. ethylenically unsaturated acids, ethylenically unsaturated aldehydes, ethylenically unsaturated amides which may be unsubstituted or substituted by C₁₋₄ alkyl or alkanol radicals and C₁₋₈ alkyl or alkanol esters of a C₃₋₉ ethylenically unsaturated acids. Some functional monomers are acrylic acid, methacrylic acid, fumaric acid, itaconic acid, acrolein, methacrolein, cinnamaldehyde, arcylamide, methacrylamide, N-methylolacrylamide, N-methylol-methacrylamide, methylacrylate, methyl methacrylate, ethylacrylate, ethylmethacrylate, hydroxyethyl acrylate, hydroxyethyl methacrylate, ethylhexyl acrylate, and ethylhexyl methacrylate. The process of the present invention is particularly useful with monomer compositions of styrene, α-methyl styrene, p-methyl styrene, butadiene or isoprene together with one or more of the above functional monomers. The process of the present invention is carried out under temperature and pressure conditions to avoid significantly degrading or destabilizing the latex. At 100°C the vapour pressure of water is 760 mm of mercury. In the process of the present invention some temperatures and pressures range from about 50 to about 100°C at about 92 to about 760 mm of Hg. Preferred temperature/pressure conditions are from about 50°C at about 92 mm of mercury to about 80°C at about 355 mm of mercury. The most preferred temperature/pressure conditions are from about 50°C at about 92 mm of mercury to about 70°C at about 283 mm of Hg. It is important that the heat history during the process be such that no significant destabilization or degradation of the latex occur. One having the ordinary skill in the art may easily test a small sample of the latex to see if it is significantly degraded or destabilized on being exposed to a specific temperature and pressure conditions over a given period of time. In accordance with the present invention at least about 0.01 parts by weight of a free radical generator are added to the latex per 100 parts by weight of the polymer in the latex. The free radical generator may consist of a chemical or a chemical combination which decomposes at the temperature of the treatment to generate free radicals e.g. hydrogen perioxide or an organic azo or diazo compound containing up to about 12 carbon atoms. Care should be taken to select a peroxide of azo or diazo material which will decompose under the conditions of use in a controlled manner. Some free radical generators may comprise redox systems comprising an oxidizing agent hydrogen peroxide or an organic peroxide or hydroperoxide containing up to about 12 carbon atoms mixed with a reducing agent. Some reducing agents are reducing sugars, their acid derivatives, reducing sulphur compounds e.g. an alkali metabisulphite, or transition metal compounds. Some peroxides and hydroperoxides are hydrogen peroxide, benzoyl peroxide, C₁₋₄ alkyl peroxides or C₁₋₄ hydroperoxides, e.g. t-butyl hydroperoxide. Some reducing agents are iron or cobalt complexes, or reducing sugars or their derivatives e.g. mannitol or gluconates. The reducing agent may be a sulphur containing compound e.g. an alkali or alkaline earth sulphate or bisulphite. A preferred reducing agent is sodium metabisulphite. A particularly useful free radical generator system for use with styrene-butadiene type latices is t-butyl hydroperoxide and sodium metabisulphite. Preferably, the total free radical generator is present in an amount of about 0.08 parts by weight per 100 parts of polymer in the latex, consisting of about equal parts of peroxide and metabisulphite. The free radical generating system is added to the latex in an amount of at least about 0.01 parts by weight per 100 parts by weight of polymer solids in the latex. The only limit on the upper amount of free radical generator is economics. One upper limit of free radical generator is about 0.20 parts by weight per 100 parts by weight of polymer in the latex. The free radical generator may be used in amounts from about 0.01 to about 0.15 parts by weight per 100 parts by weight of polymer in the latex. A suitable weight range for the free radical generator is from about 0.04 to about 0.08 parts by weight per 100 parts by weight of polymer solids. The process of the present invention is not intended to relate to the initial polymerization of the monomer system. The process is generally applicable in a steam stripper subsequent to devolatilization of the latex. The process of the present invention may also be applied to the latex, prior to devolatilization, in the reactor after about 80 per cent of the monomer has been converted to polymer. Example (see the accompanying drawing, i.e. Fig. 1) The following example is intended to illustrate the invention. Four 4 litre samples of a styrene-butadiene latex which was produced in the plant and which had been devolatilized were treated in accordance with different aspects of the present invention or the prior art. The sample was placed in a 12 litre flask immersed in a constant temperature bath. The flask was connected to a vacuum to control the vapour pressure above the sample. In this manner, it was possible to subject the sample to conditions ranging from no-boiling, boiling, reflux and steam injection. A free radical generator comprising t-butylhydroperoxide and sodium metabisulphite was added to the system. In one experiment, the free radical generator was added in "one shot" in an amount of about 0.05 parts per 100 parts of monomer. The "one shot" addition was tested under reflux and under steam injection. The free radical generator was added incrementally in an amount of about 0.5 parts per hour under boiling, reflux and steam injection. Samples of the latex were tested periodically for residual styrene. A graph was then plotted of percentage residual styrene (on a logarithmic scale) against time in hours (linear scales). The plot of these data is given in Fig. 1, in which the theoretical steam usage has also been plotted. These graphs show that the process of the present invention is about twice as efficient as conventional steam stripping in the absence of a free radical generator. This improvement reduces energy consumption and significantly reduces the time required for the stripping of a latex. An increase in yield is also obtained. It will be noted that the present invention enables residual monomer to be removed from a polymeric emulsion by subjecting it to pressure and temperature conditions so that the ambient vapour pressure is less than the vapour pressure in the emulsion, and concurrently and continuously during the treatment comprising adding a free radical initiator.

Claims: A process of treating an emulsion of one or more monomers, in which : (a) at least about 80 weight per cent of said one or more monomers having been polymerized, said one or more monomers being selected from: C₈₋₁₂ vinyl aromatic monomers which may be substituted or substituted by a C₁₋₄ alkyl or hydroxyalkyl radical or a chlorine or bromine atom; C₄₋₈ conjugated diolefins; C₃₋₉ ethylenically unsaturated carboxylic acids; C₃₋₉ ethylenically unsaturated aldehydes; amide derivatives of C₃₋₉ ethylenically unsaturated carboxylic acids which may be unsubstituted or further substituted at the nitrogen atom by a C₁₋₄ alkyl, alkanol, or alkylol radical; C₁₋₈ alkyl or alkanol esters of C₃₋₉ ethylenically unsaturated carboxylic acids in which the alkyl or alkanol radical may be branched or straight chained; and C₂₋₈ ethylenically unsubstituted nitriles; (b) subjecting said emulsion to temperature and pressure conditions at which the vapour pressure of water in the ambient environment is less than the vapour pressure of water in the emulsion without significantly degrading or destalilising the emulsion; characterised by (c) incremently introducing into the emulsion, without the introduction of additional monomer, at least about 0.01 parts by weight of a free radical generator per 100 parts by weight of polymer in the emulsion per hour of treatment until the residual monomer content is not more than about 0.05 per cent by weight based on the emulsion. A process as claimed in claim 1, characterised by said temperature conditions are in the range about 50 to about 100°C; and said pressure conditions are in the range about 92 to about 760 mm of Hg. A process as claimed in claim 1 or 2, characterised by said temperature and pressure conditions are maintained in a reflux condenser. A process as claimed in claim 1 or 2, characterised by said temperature and prssure conditions are maintained in a steam stripping apparatus. A process as claimed in any one of claims 1 to 4, characterised by said free radical generator is added in an amount in the range about 0.01 to about 0.2 parts by weight per 100 parts by weight of polymer in the emulsion per hour of treatment. A process as claimed in any one of claims 1 to 5, characterised by said free radical generator comprises hydrogen peroxide or an azo or diazo compound containing up to about 12 carbon atoms. A process as claimed in any one of claims 1 to 5, characterised by said free radical generator is a redox system wherein the oxidizing agent is selected from organic perioxides and organic hydroperoxides containing up to about 12 carbon atoms; and the reducing agent is selected from reducing sugars, acid derivatives of reducing sugars, reducing sulphur compounds, and transition metal compounds. A process as claimed in claim 7, characterised by said oxidizing agent is selected from organic perioxides and organic hydroperoxides containing up to about 12 carbon atoms; and said reducing agent is selected from reducing sulphur compounds. A process as claimed in claim 8, characterised by said oxidizing agent comprises a C₁₋₄ alkyl peroxide or a C₁₋₄ alkyl hydroperoxide; and said reducing agent comprises sodium metabisulphite.

Inventors: TAYLOR, MICHAEL ALLAN
Applicants: BASF AKTIENGESELLSCHAFT, POLYSAR LIMITED
Application year: 1985
Main classification: C08F6
IPC codes: C08F6