Ethylene-Vinyl Halide-Alkyl Vinyl Terpolymer Emulsions

This invention relates to polymeric materials. In another aspect, this invention relates to novel stable emulsions formed with terpolymers of ethylene, a vinyl halide monomer and an alkyl vinyl monomer. In still another aspect, this invention relates to novel emulsions of particles of ethylene-vinyl halide-alkyl vinyl terpolymers which impart improved characteristics when blended in conventional polish formulations.

Polymeric emulsions are conventionally used in coatings, lacquers, paints and polishes. Polyethylene emulsions which are conventionally used in coatings, lacquers, paints and polishes can be produced by emulsion polymerization techniques such as set forth in U.S. Pat. Nos. 3,226,352 and 3,244,652. Generally, polyethylene emulsions will dry at room temperature to form films which have poor gloss, flexibility and crack resistance and can be easily removed from a substrate to which they are applied by mechanical force. Therefore, such polyethylene latexes are admixed with other materials including resins, leveling agents, plasticizers and fluxes when used in polishes and the like. However, many conventional polyethylene emulsions have not been utilized in as wide a variety of applications as desired because of incompatibility problems which exist when they are admixed with certain standard formulations of paints, polishes and the like causing precipitation of the solids and other instability problems. Therefore, there is a continuing need for polymeric emulsions comprising ethylene which are extremely stable and compatible with various types of latexes and other formulations which are utilized in coating compositions such as paints and polishes.

According to the invention, novel stable emulsions of ethylene containing terpolymers are provided. The terpolymer particles in the novel emulsions are formed by the copolymerization of ethylene, a vinyl halide monomer, and an alkyl vinyl monomer. These improved emulsions are produced by copolymerizing the monomers in an aqueous medium in the presence of a water soluble persulfate initiator, and an anionic and/or nonionic emulsifier. The resulting emulsions containing the terpolymer have excellent compatibility with conventional polish formulations and will provide film coatings of improved flexibility and toughness as compared to conventional polyethylene emulsions.

The novel emulsions can be produced in accordance with the subject invention either under batch or continuous process conditions by contacting pressurized ethylene, a vinyl halide monomer, and an alkyl vinyl monomer in an aqueous medium which contains a water soluble persulfate initiator and an emulsifier. Contact of the monomers with the aqueous medium is made under greater than atmospheric pressure and at an elevated temperature. Generally, the polymerization temperature can range from about 60.degree. C to about 150.degree. C and the pressure can generally range from about 1400 psi to about 20,000 psi depending upon the type of emulsifier that is used in the system.

The vinyl halide monomers which can be used in the scope of the subject invention are the aliphatic vinyl compounds which contain up to about 2 halogen atoms attached to a carbon in the molecule. The halogen atoms can be attached directly to a carbon in the vinyl group, or can be attached to a carbon which is not in the vinyl group. Specific examples of the former include vinyl chloride, vinyl fluoride, vinylidene chloride, and vinylidene fluoride. Examples of compounds containing the halogen atoms attached to a carbon atom which is not in the vinyl group include the haloalkyl esters of aliphatic vinyl acids having from 4 to about 20 carbon atoms. Specific examples of such compounds include 2-chloroethyl acrylate, 2-chlorobutyl acrylate, 2-bromoethyl acrylate, 2-chloroethyl methacrylate, 4-chlorobutyl methacrylate, and 2-bromoethyl methacrylate. Other suitable such vinyl halide compounds include the dihalo alkyl vinyl phosphonates wherein each alkyl group contains from about 1 to about 4 carbon atoms such as for example Bis-beta chloroethyl vinyl phosphonate. The vinyl halide monomer can be contained in the aqueous medium in amounts ranging from about 0.1 to about 20% by weight of the aqueous reaction medium.

The alkyl vinyl compounds utilizable within the scope of the subject invention include the straight and branched chain alkyl vinyl compounds having from about 3 through about 24 carbon atoms. The normally liquid alkyl vinyl compounds are generally admixed with the vinyl halide monomer and emulsifier in the aqueous reaction medium before contact of the medium with ethylene is carried out. The normally vaporous alkyl vinyl compounds such as propylene can be introduced with the vaporous ethylene feed during the polymerization process. Generally, the alkyl vinyl compounds can be present in an amount in the range of from about 0.1 to about 10% by weight of the aqueous reaction medium. Extremely durable and flexible terpolymers are produced within the scope of the subject invention when utilizing an alkyl vinyl compound having at least about 15 carbon atoms.

Generally, the emulsions produced in accordance with the subject invention comprises a mixture of ethylene homopolymer and the terpolymer of ethylene, the vinyl halide compound and the alkyl vinyl compound. These polymers have a molecular weight in the range of from about 2000 to about 20,000. The particle size of the resulting polymers generally ranges from about 100 to about 1000 angstrom units.

Only a minor catalytic amount of a water soluble persulfate initiator need be present in the aqueous reaction medium. Examples of suitable water soluble persulfates include alkali metal persulfates such as potassium and sodium persulfate and any other water soluble persulfate such as ammonium persulfate and the like. The amount of the water soluble persulfate initiator can vary depending upon the particular emulsifier system which is utilized.

Suitable anionic emulsifiers which can be used in the scope of the subject invention include the saturated fatty acid salts, such as the alkali metal salts and particularly the sodium and potassium salts of saturated fatty acids having from about 12 to about 18 carbon atoms. Examples of suitable such emulsifiers include the alkali metal salts of myristic acid, lauric acid, stearic acid and the like.

Other suitable anionic emulsifiers which can be used in the scope of the subject invention include the alkali metal salts and particularly the sodium and potassium salts of alkyl aryl sulfonic acids and preferably the alkali metal alkyl benzene sulfonates wherein the alkyl group is a straight or branched chain group which contains from about 6 to about 18 carbon atoms. Examples of suitable such materials include sodium and potassium salts of dodecyl benzene sulfonic acid, nonyl benzene sulfonic acid, undecyl benzene sulfonic acid, tetradecyl benzene sulfonic acid, hexadecyl benzene sulfonic acid, mixtures thereof and the like.

Further anionic emulsifiers which can be used in the scope of this invention include the salts and particularly the alkali metal salts of sulfates of fatty alcohols having from about 12 to about 18 carbon atoms or mixtures thereof and salts and particularly alkali metal salts of sulfates of ethoxylated fatty alcohols having from between about 12 to about 18 carbon atoms and an average number of ethoxy groups between about 1 and 5. Examples of such materials include sodium sulfates of C.sub.12 alcohols, sodium tridecyl alcohol sulfate, and the sodium salt of ethoxylated lauryl sulfate with an average of about 1.5 ethoxy groups.

When utilizing the anionic emulsifiers and particularly the acid salts, the pH of the reaction should be maintained within the range of from about 8.5 to about 14 by the use of basic materials such as sodium hydroxide or potassium hydroxide.

In addition, especially when using the acid salts particularly the saturated fatty acids having about 12 to 18 carbon atoms, a pH adjuster can be present in the aqueous phase to prevent displacement, by stronger acids, of the weak component of the emulsifier, e.g., fatty acid soaps. The pH adjusters employed in this instance are those which in nature and amount used will result in a pH at least about 8.5 in the product removed from the reactor. Since acid is formed during the polymerization, the pH at the time polymerization is initiated is preferably somewhat higher, suitably about 10.5. Alkaline substances having a pH of about 10.5 for example, are potassium phosphates such as tripotassium phosphate and potassium carbonate, which substances are also buffers. To give the desired pH values sodium hydroxide, for example, is added to the aqueous medium in amounts between about 0.25 and about 0.7% by weight thereof. To maintain the pH, alkalies such as potassium hydroxide or sodium hydroxide can be added to the aqueous medium during the course of the reaction. Furthermore, if the alkyl sulfonate type emulsifiers are utilized, the pH adjuster can be omitted, if desired, since these materials are acid stable to a pH of about 4.

Nonionic emulsifiers which can be used in the scope of this invention are the nonionic alkylphenoxy polyoxyethylene ethanols and preferably the alkylphenoxy polyoxyethylene ethanol emulsifiers having the general formula: ##STR1##

Wherein R' is an alkyl chain having 8 or 9 carbon atoms advisably branched such as a polypropylene or polybutylene chain and n represents and average of 7 to about 15. Some examples of suitable such emulsifiers are as follows: ##STR2##

Likewise, when utilizing the above-described salts of saturated fatty acids or salts of sulfates of fatty alcohols or salts of sulfates of ethoxylated fatty alcohols as emulsifiers, it is generally desirable to conduct the process with a polymerization initiator content in the range of from about 0.06 to about 0.75 percent by weight of the aqueous phase. Furthermore, the emulsifier should be present in an amount in the range of from about 0.09 to about 9 percent by weight of the aqueous phase and even more preferably, an amount in the range of from about 1.2 to about 3.0 percent by weight of the aqueous phase. Furthermore, the emulsion polymerization can be carried out at a temperature within the range of from about 70.degree. to about 150.degree. C and even more preferably at a temperature in the range of from about 85.degree. C to about 100.degree. C. Furthermore, this process can be carried out at a pressure in the range of from about 2000 to about 5000 psi and preferably at a pressure in the range of from about 3000 psi to about 4000 psi.

When utilizing the above described alkyl aryl sulfonate salts as emulsifiers, the polymerization is preferably carried out in the presence of a water soluble persulfate initiator in an amount in the range of from about 0.1 to 0.75% by weight of the initiator based upon the liquid reaction medium. Furthermore, the emulsifier should be present in an amount in the range of from about 1 to 7% by weight of the aqueous reaction medium and more preferably from about 3 to about 5% by weight of the aqueous reaction medium. The reaction can occur at a pressure in the range of from about 1400 to about 5000 psi and preferably in the range from about 1550 to about 3000 psi. The process can be carried out at a temperature in the range of from about 60.degree. C to 150.degree. C and preferably from about 90.degree. C to 100.degree. C.

When utilizing the above-described nonionic emulsifiers the reaction is preferably carried out in the presence of the free-radical initiator in an amount in the range of from about 0.08 to about 0.7 percent by weight of the aqueous medium. The emulsifier can be present in the range of from about 1.0 to about 5.0 percent by weight of the aqueous medium and more preferably in an amount in the range of from about 2.0 to about 4.0 percent by weight of the aqueous medium. The polymerization can be carried out at a temperature within the range of from about 60.degree. C to about 150.degree. C and more preferably at a temperature in the range of from about 90.degree. C to about 110.degree. C. Furthermore, the pressure can be in the range of from about 2000 psi to about 20,000 psi and is preferably within the range of from about 2500 to about 4500 psi.

When using a mixture of the anionic and nonionic emulsifiers, it is preferable that the mixture comprise from about 5 to about 75% by weight of nonionic emulsifier. In such instance, the emulsifier mixture can be present in the range of from about 1 to about 9 percent by weight of the aqueous medium. Furthermore, the initiator can be present in an amount in the range from about 0.06 to about 0.75 weight percent of the aqueous emulsion and the reaction can be carried out at a temperature within the range of from about 80.degree. C to about 100.degree. C and a pressure in the range of about 1500 to about 3000 psi.

Although the polymerization can be readily effected in the presence of water as the sole liquid medium, an alcohol such as t-butanol can be included within the aqueous medium. The presence of such an alcohol is especially preferred when the sole emulsifier is a nonionic emulsifier. Such aqueous alcoholic medium can contain any amount of alcohol of the type that favorably influences the polymerization and the resultant emulsion. Generally up to about 35 percent by weight based on the combined weight of alcohol and water of an alcohol such at t-butanol can be acceptably included in the polymerization medium.

The reaction can be carried out in either a batch or continuous operation. In carrying out the polymerization process in accordance with the present invention, water, the emulsifier, the initiator, the pH adjuster (if necessary), and nonvaporous monomer(s) (alkyl vinyl monomer and/or vinyl halide monomer) are combined in any order in the amounts or proportions which are recited above. The components are mixed in a suitable pressure reactor, or a premixed aqueous phase is introduced into the reactor. The reactor is equipped with a stirring mechanism in which fairly vigorous agitation of the contents is possible either by motion of the reactor or by agitating means of the reactor. The reactor is suitably made of a corrosion resistant material such as stainless steel or is equipped with a corrosion resistant lining such as glass or stainless steel. The reactor is then flushed with polymerization grade (99.8+% pure) ethylene to remove gaseous oxygen from the system. Preferably the polymerization grade ethylene contains less than 10-25 ppm of oxygen.

In some instances, it is desirable to initially add all ingredients but the initiator to the reactor and then heat the reactor to the operating temperature as set forth above, and then the initiator is introduced into the reactor, conveniently dissolved in a portion of the water component of the aqueous medium. In this instance, the initiator is conveniently added to the reaction zone in a sufficient quantity to produce a polymerization rate of about 5% per hour.

High pressure polymerization grade ethylene (and, is desired, a vaporous alkyl vinyl monomer and/or a vaporous vinyl halide monomer) is introduced into the reactor. The pressure of the ethylene can be dependent upon the emulsifier as stated above. The reaction proceeds at the temperatures and pressures set forth above with constant vigorous agitation of the liquid contents of the reactor. As the polymerization proceeds, additional ethylene is continuously fed into the reactor to maintain the pressure. The polymerization is permitted until the emulsion reaches the desired solids content. This can be done by periodically withdrawing samples from the reactor and plotting the solids content as a function of time. A leveling off of the plotted solids content indicates that the reaction is slowing down and that the initiator is becoming depleted by thermal decomposition. When this happens, additional initiator can be added in small increments to maintain the polymerization rate of about 5% per hour. The emulsion produced will generally have a solids content of between about 15 and 25 weight percent.

Following the polymerization any solvent present such as t-butanol can be stripped from the latex and the latex concentrated by distillation under reduced pressure until the solids content is up to about 45 weight percent without adverse effect on the stability of the emulsion.

The resulting stable emulsions produced by the subject invention are very compatible with conventional polish and paint formulations and contribute to improved properties of these compositions as compared to such compositions containing stable polyethylene emulsions.

More specifically, the novel terpolymer emulsions produced in accordance with the subject invention can be incorporated into conventional latex paint formulations. Typical such latex paint formulations include both the gloss and semi-gloss latexes and acrylic polymers, copolymers, esters and polyvinylacetate and styrene-butadiene copolymers, for example. The typical latex paint formulation will contain a dispersing agent for pigments such as tetrasodium pyrophosphate, soya lecithin and the like; protective colloids and thickeners such as sodium polyacrylates, carboxymethylcellulose, colloidal clays, gum arabic, and the like; defoamers such as tri-n-butylphosphate, n-alkylalcohol, and other higher alcohols and the like; coalescing agents which include hexylene glycol and ethylene glycol, monobutyl ether acetate and the like; freeze-thaw additives such as, e.g., ethylene glycol; mildewcides and preservatives such as mercurial copper and phenolic compounds; and pH controllers such as ammonium hydroxide. The terpolymer emulsions produced in accordance with the subject invention can be incorporated into typical conventional formulas in amounts equaling from about 1 to about 20 weight percent thereof.

The novel terpolymer emulsions of the subject invention can also be incorporated into conventional polishes such as floor polishes which basically comprise aqueous emulsions. Liquid aqueous emulsion polishes generally comprise a waxy component and a resin component, including alkali soluble and alkali insoluble components, and leveling and plasticizing agents and fluxes. Depending on the characteristics desired in the final polish, the dispersed waxy and resinous component can be employed in proportions that constitute between about 5 and about 95% by weight of the total solids dispersed. Polyethylene emulsions have been utilized as the total or a part of the total of the waxy component. The conventional waxy components include natural and synthetic waxes.

A wide variety of alkali soluble and alkali insoluble natural and synthetic resins are known in the polish formulating art, including rosin, shellac, manilla, loba, terpene resins, terpene phenolic resins, polyvinylacetate, polyvinylchloride, polystyrene, polyvinylidene chloride, copolymers of vinyl chloride, and vinyl acetate, copolymers of vinylidene chloride and acrylonitrile, vinyl acetate and crotonic acid copolymers, butadiene-styrene copolymers, condensation products of maleic anhydride or fumaric acid with rosin and mixed polyhydroxy alcohols, condensation products of maleic anhydride and pentaerythritol, condensation products of maleic anhydride and high molecular weight glycols, and polymers and copolymers of alkyl acrylates and methacrylates. These resins can also be polymers of allyl acrylate, methallylacrylate, allyl methacrylate, crothyl acrylate, crothylmethacrylate, allyl methacrylate, allyl cinnamate, methallylmethacrylate, methallylacrylate, diallyl phthalate, dimethallyl phthalate, diallylmaleate, divinylbenzene, and the like.

Suitable leveling agents, plasticizers or fluxers known to the art for use in wax polish formulations include phthalate plasticizers such as dibutylphthalate, alkylphosphate plasticizers such as tributylphosphate or tributyloxyethylphosphate, n-octanol and fluoroalkyl leveling agents taught in U.S. Pat. No. 2,937,098. The ethylene polymer emulsions of the subject invention are more compatible than conventional polyethylene emulsions with the above described polish formulations and also exhibit increased scuff and scratch resistance, slip resistance, gloss, black heel mark resistance, durability and stability without effecting detergent resistance and removability.

The following examples are set forth to better facilitate the understanding of this invention and are not intended to limit the scope thereof:

A high pressure stainless steel batch reactor equipped with an internal agitator was charged with an aqueous solution of emulsifier, initiator, and octadecene-1. Thereafter vinyl chloride gas was pumped into the interior of the reactor above the solution. This total initial charge to the reactor consisted of 95.3% by weight deionized water, 3.2% by weight of dodecyl benzene sulfonic acid, 0.4% by weight of potassium persulfate, 0.5% by weight of octadecene-1, 0.1% by weight of vinyl chloride, and 0.5% by weight of sodium hydroxide. The reactor was next heated to 90.degree. C and polymerization grade ethylene was pumped into the interior of the reactor to maintain a pressure therein at 1700 psi. The pressure was maintained at 1700 psi by an automatically operated pressure valve supplying ethylene from the compressor. The temperature was automatically maintained at 90.degree. C by means of a thermostat and internal cooling coils. The reaction began immediately and reaction samples were removed from the reactor at 30 minute intervals after the initiation began. The solids content of the samples was determined by means of a moisture balance. When the samples reached 17.5% by weight solids, the polymerization was terminated by shutting off the ethylene supply, cooling the reactor, stopping the motion of the agitator and discharging the contents into a receiving vessel at atmospheric pressure. The total reaction time was 2.5 hours. The product was a fluid, opaque latex with no sediment or visible solid particles present.

An aqueous feed solution, and vinyl chloride gas were continuously fed to a stainless steel continuous reactor. These liquid and vaporous feed streams consisted of 95.3% by weight deionized water, 3.2% by weight of dodecyl benzene sulfonic acid, 0.4% by weight of potassium persulfate, 0.5% by weight of octadecene-1, 0.1% by weight of vinyl chloride, and 0.5% by weight of sodium hydroxide. The continuous reactor was maintained at a temperature of 90.degree. C and a pressure of 1700 psi by pressurized ethylene which was constantly supplied thereto. The reaction product from the continuous reactor was constantly withdrawn at a rate to maintain a residence time of 2.5 hours and a solids level in the product of 17.5 weight percent. The physical properties of the resulting product were the same as the properties of the product described in the batch process of Example I.

A high pressure stainless steel batch reactor equipped with an internal agitator was charged with an aqueous solution of emulsifier, initiator, and octadecene-1 as vinyl monomer. Thereafter vinyl chloride was pumped into the interior of the reactor above the solution. The total charge to the reactor consisted of 93.1% by weight deionized water, 3.2% by weight of nonyl phenol polyethylene oxide (9-40 moles ethylene oxide), 0.4% by weight of potassium persulfate, 0.5% by weight of octadecene-1, 0.1% by weight of vinyl chloride, 2.5% by weight of t-butanol, and 0.2% by weight of potassium hydroxide. The reactor was next heated to 95.degree. C and polymerization grade ethylene was pumped into the interior of the reactor to maintain a pressure therein at 2500 psi. The pressure was maintained at 2500 psi by an automatically operated pressure valve supplying ethylene from the compressor. The temperature was automatically maintained at 95.degree. C by means of a thermostat and internal cooling coils. The reaction began immediately and reaction samples were removed from the reactor at 30 minute intervals after the initiation began. The solids content of the samples was determined by means of a moisture balance. When the samples reached 17.5% by weight solids, the polymerization was terminated by shutting off the ethylene supply, cooling the reactor, stopping the motion of the agitator and discharging the contents into a receiving vessel at atmospheric pressure. The total reaction time was 2.5 hours. The product was a fluid, opaque latex with no sediment or visible solid particles present.

An aqueous feed solution, and vinyl chloride gas was continuously fed to a stainless steel continuous reactor. These liquid and vaporous feed streams consisted of 93.1% by weight deionized water, 3.2% by weight nonyl phenol polyethylene oxide (9-40 moles ethylene oxide), 0.4% by weight of potassium persulfate, 0.5% by weight of octadecene-1, 0.1% by weight of vinyl chloride, 2.5% by weight t-butanol, and 0.2% by weight of potassium hydroxide. The continuous reactor was maintained at a temperature of 95.degree. C and a pressure of 2500 psi by pressurized ethylene which was constantly supplied thereto. The reaction product from the continuous reactor was constantly withdrawn at a rate to maintain a residence time of 2.5 hours and a solids level in the product of 17.5 weight percent. The physical properties of the resulting product were the same as the properties of the product described in the batch process of Example III.

All of the emulsions produced by the process as set forth in Example I through Example IV were blended with conventional polish formulations. The emulsions imparted improved flexibility and toughness over that of polyethylene emulsions alone and displayed improved compatibility with the polish formulations as compared with the polyethylene emulsions alone.

While this invention has been described in relation to its preferred embodiment, it is to be understood that various modifications thereof will now be apparent to one skilled in the art upon reading the specification and it is intended to cover such modifications as fall within the scope of the appended claims.