PROCESS FOR PREPARING A CRYSTALLINE VINYLIDENE CHLORIDE POLYMER POWDER, AND COMPOSITIONS COMPRISING IT

Abstract: A crystalline vinylidene chloride polymer powder which is dispersible in polyols and other non-solvents for vin­ ylidene chloride polymers is prepared by aging a latex of crystallizable vinylidene chloride polymer particles until sub­ stantially all the latex particles are crystallized and then recovering the latex particles from the latex. The resulting powder can be dispersed with moderate shear in a non-­ solvent for vinylidene chloride polymers, such as a polyol used in the preparation of polyurethane materials. A disper­ sion of the powder and a polyol is eminently suitable for use in the preparation of polyurethane foam material to impart enhanced load-bearing properties and flame-retardancy thereto.

Description: CRYSTALLINE VINYLIDENE CHLORIDE POLYMER POWDER AND POLYMERIC MATERIALS CONTAINING SAME The present invention relates to vinylidene chloride polymers and, more particularly, to vinylidene chloride polymers which are dispersible in non-solvents for such polymers. This invention provides vinylidene chloride polymer powders that can be dispersed in a non-solvent organic liquid for vinylidene chloride polymers and thereafter used to prepare polymeric materials having enhanced physical properties. More specifically, the present invention provides a vinylidene chloride polymer powder, high in chlorine content, that can be dispersed in a polyol used to prepare polyurethane foam materials. In one aspect, this invention provides a process for preparing a crystalline vinylidene chloride polymer powder which is dispersible in non-solvent organic liquids which comprises emulsion polymerizing monomers comprising a major proportion of vinylidene chloride to prepare a latex wherein the latex particles have a diameter less than one micron, aging the resulting latex until from 75 to 100 percent of the latex particles are crystallized and then recovering the polymer from the latex. In another aspect, the present invention resides in the resultant crystalline vinylidene chloride polymer powder and a new composition of matter which comprises the resultant vinylidene chloride polymer powder dispersed in a non-solvent for vinylidene chloride polymers such as a polyol used in the preparation of polyurethane materials. Crystallizable vinylidene chloride polymers in accordance with the present invention include the homopolymer and copolymers of vinylidene chloride with at least one copolymerizable ethylenically unsaturated comonomer. Exemplary comonomers which can be utilized in the present invention include nitriles of ethylenically unsaturated carboxylic acids such as acrylonitrile and methacrylonitrile; alkyl esters of acrylic and methacrylic acids such as methyl acrylate and methyl methacrylate; hydroxyalkyl esters of acrylic and methacrylic acids such as hydroxypropyl acrylate, hydroxyethyl acrylate, and hydroxybutyl acrylate; vinyl esters of saturated carboxylic acids such as vinyl acetate; amides of ethylenically unsaturated carboxylic acids such as acrylamide acid; ethylenically unsaturated alcohols such as allyl alcohol; vinyl halides such as vinyl chloride; and other ethylenically unsaturated monomers known to polymerize with vinylidene chloride. Of these, methyl acrylate is the preferred comonomer. In order to obtain a crystallizable particle, the amount of vinylidene chloride in the polymer will vary with the particular monomer used. In general, the tendency for the latex particles to crystallize while still in emulsion will increase with decreasing molecular weight, with increasing particle size, with increasing temperature during aging of the latex, or with increasing vinylidene chloride content. Typically, a sharp crystallization break point at a specific comonomer concentration can be identified for each comonomer used. If the level of comonomer is increased beyond the break point, the crystallization induction time increases exponentially and the tendency for the particles in the latex to crystallize decreases exponentially. For example, at a polymer composition of 92 weight percent vinylidene chloride and 8 weight percent methyl acrylate, the tendency for latey particles having a size of about 1200 and relative viscosity of about 1.5 to crystallize is so low that the latex can be held at the optimum temperature for crystallization (800C) for six hours and subsequently cooled with essentially no crystallization occurring in the particles. On the other hand, similar polymer particles having a composition of 93 weight percent vinylidene chloride and 7 weight percent methyl acrylate will crystallize under the same conditions. However, the polymers of vinylidene chloride and methyl acrylate constitute a very special case inasmuch as the rate of reaction for the two monomers is nearly identical and very little composition drift occurs during polymerization. In contrast, a sharp crystallization break point is not as readily identified for polymerizable mixtures wherein the comonomer enters the polymer at a rate slower or faster than vinylidene chloride. In conventional batch emulsion polymerization, the crystallization break point for a particular polymerization mixture can nevetheless bs identified without extensive experimentation. In o- tinuous feed polymerization, however, the crystallization break point for a monomer mixture in which the comonome- > has a faster reaction rate than vinylidene chloride will be harder to determine and will vary with the composition drift occurring both in the seed latex reaction, if used, and in the ultimate polymer particle reaction. Preferably, polymerizable mixtures which produce latex particles that crystallize within an aging period of seven days at 250 to 300C are within the scope of the present invention The crystallizable vinylidene chloride polymers of the present invention are prepared by polymerization in an aqueous emulsion according to processe-s well known in the art. Preferably, the polymerization is carried out by essentially continuous, carefully controlled addition of the reguisite polymerization constituents (including polymerization initiator systems if desired) to the aqueous medium. Generally, it is preferred to start the polymerization by adding a small amount of the monomeric material to the aqueous medium and then adding the desired polymerization initiator to form a polymeric seed latex to aid in the control of particle size. The aqueous medium in which the seed latex is formed will contain the necessary surfactants to form the emulsion and will generally be adjusted to the desired pH value, as is well known in the art. Following the formation of the seed latex, the remaining amount of monomeric material is continuously added under carefully controlled conditions to the aqueous medium. In view of the fact that amine catalysts are typically used in the preparation of polyurethane foam materials 0 control the rate of urea and urethane reactions and that the urethane reactions are significantly exothermic, the vinylidene chloride polymers of the present invention could have a tendency to degrade and produce hydrogen chloride when used in such applications. The accele=ated evolution of hydrogen chloride caused by such degradation could not only result in discoloration of the vinylidene chloride polymer and the resultant polyurethane foam material, but could also alter the kinetics ci the urethane reaction. It has been found that a moderate decrease in the propensity of the vinylidene chloride polymer to discolor when exposed to the conditions of the polyurethane foam reaction and similar deleterious environments can be achieved by sequentially polymerizing such polymers with a monomer mixture comprising an ethylenically unsaturated non-vinylidene chloride monomer. It is believed that the sequential polymerization provides a thin cap on the vinylidene chloride polymer particles which protects them from the amine catalyst, thereby reducing The rate of decomposition. The sequential polymerization can be carried out in a conventional manner by adding an effective degradation reducing amount up to 20 percent by weight of the vinylidene chloride polymer, preferably from 5 to 10 percent by weight, of the desired monomer mixture (including emulsifiers and initiators as needed) to the vinylidene chloride polymer latex and subjecting the monomer mixture to polymerization conditions. In a preferred mode, the desired monomer mixture for sequential polymerization is not added to the latex until it'is certain that essentially all of the residual vinylidene chloride monomer has been depleted. Depletion of residual vinylidene chloride monomer can be accomplished, for example, by adding an additional amount of initiator or a minor amount of methyl acrylate to the polymerization vessel subsequent to the apparent completion of the vinylidene chloride polymer reaction, but prior to the addition of the sequentially polymerizable monomer mixture. In this manner, the possibility of including vinylidene chloride in the resultant non-vinylidene chloride polymer "cap" - will be reduced. In order to provide adequate dispersibility for purposes of this invention, the non-vinylidene chloride polymer 11cap" should either be uncrosslinked and have a second order transition temperature greater than 600C, preferably greater than 650C, or it should be crosslinked. If the cap11 is crosslinked, i.e., by copolymerizing a minor amount of a crosslinking polyfunctional comonomer with the desired ethylenically unsaturated non-vinylidene chloride monomer or monomers, the second order transition temperature requirement is not as critical, though values within the aforementioned range are preferred. Exemplary ethylenically unsaturated non-vinylidene chloride monomers which can be used in the sequential polymerization reaction to prepare the "cap" polymer include the alkyl esters of methacrylic acid such as methyl methacrylate; the vinyl aromatic monomers such as styrene and vinyl toluene; and other sequentially polymerizable monomers, i.e., those which are capable of producing a "cap" satisfying the aforementioned criteria. Exemplary copolymerizable crosslinking polyfunctional monomers which can be polymerized with the ethylenically unsaturated non-vinylidene chloride monomers include 1,3-butylene glycol acrylate 1,4-butane diol diacrylate, allyl acrylate, vinyl acrylate, 1,3-butylene glycol dimethacrylate, 1,4-butane diol dimethacrylate; allyl methacrylate, and vinyl methacrylate. The amount of crosslir±king monomer required for dispersibility will depend upon the efficiency of the particular crosslinking monomer chosen, as well as the ethylenically unsaturated monomer or monomers with which it is polymerized. Generally the amount of crosslinking monomer used, if any, will be less than 6 percent of the weight of the sequentially polymerizable monomer mixture. The diameter of the resulting latex particles, which includes those which have been "capped" by sequen- tial polymerization as well as those which have not been "capped" should be less than one micron. Preferably, the mean particle diameter is in the range of 0.05 to 0.5 micron, most preferably in the range of 0.1 to 0.3 micron, with substantially all of the particles having a diameter in that range. The preferred ranges are especially applicable if the powders obtained therefrom are to be used in the preparation of polyurethane foam materials. Larger latex particles will produce less discoloration in polyurethane foam materials, but smaller particles have longer dispersion stability in the polyol starting material and also provide better load-bearing properties in the foam material. Accordingly, the preferred range represents those sizes which will give the best overall balance of properties when used in the preparation of polyurethane foam material. In order to achieve satisfactory dispersions of the vinylidene chloride polymer powders in non-solvents for vinylidene chloride polymers according to the present invention, it is necessary that substantially all of the latex particles are crystallized before they are recovered from the latex. It should be pointed out that the ultimate degree of crystallinity within each latex particle is not as important as the number of particles which are crystallized. Preferably, from 75 to 100 percent of the latex particles will be crystallized prior to recovery; most preferably between 85 and 95 percent of the particles will be crystallized. The percent of particles crystallized is determined by a physical count where the crystalline particles are seen in an electron micrograph as sharp black spheres while amorphous particles are flattened out, are not in focus and are much lighter. It has been found that those latex particles which have been "capped" with an ethylenically unsaturated non-vinylidene chloride monomer that is highly reactive with vinylidene chloride, e.g., methyl methacrylate, have a reduced tendency to crystallize as compared to similar latex particles which have not been "capped" or which have been "capped" with a monomer that is not as highly reactive with vinylidene chloride, e.g., styrene. Accordingly, in those instances where the tendency of the "capped" latex particle to crystallize will be reduced to an undesirable level, it is advantageous to permit the intermediate vinylidene chloride polymer latex particles to crystallize before they are subjected to the sequential polymerization reaction. The crystalline vinylidene chloride polymer powders of the present invention are recovered from the aforementioned latices by conventional tecbziiques, preferably by coagulating the latex and then washing and drying the coagulum or by spray drying the latex to produce a fine powder. The optimum temperature for coagulation will vary depending upon the type and amount of comonomer employed in preparing the vinylidene chloride polymer and particularly upon the second order transition temperature of the resultant polymer. Generally, the coagulation temperature will be in the range of 500 to 95"C, preferably from 50 to 80"C. It is necessary that the vinylidene chloride polymer powders of the present invention be dispersible in non-solvents for vinylidene chloride polymers. For purposes of the present invention, "dispersibility" is measured under the following conditions: 20 weight percent of the desired powder is mixed with a polyol having a room temperature viscosity of 900 to 1000 cps, and the mixture is passed once through a Gifford-Wood colloid mill operating at 10,000 rpm with a gap setting 0.004 inch (0.1 mm) and then twice through a Gaulin homogenizer operating at 5000 psi (350 kg/sq cm). Under such conditions, substantially all of a powder suitable for use in the present invention will break down in the polyol and regenerate the original latex particles. Essentially all of the powder particles which do not break down to the latex particle size, if any, should be of a size less than 100 microns. Preferably at least 40 percent of the powder particles break down to the original latex particle size. As used herein, "non-solvents for vinylidene chloride polymers'1 is intended to be descriptive of liquid organic reactants which are used in the preparation of polymeric materials. In particular, it is intended to include polyols, which are used in the preparation of polyurethane materials; dihydroxy alcohols, which are used in the preparation of polyester resins; and the like. In all cases, the novel crystalline vinylidene chloride polymer powders of the present invention are suitably employed to render the resulting polymeric materials more resistant to ignition and burning while generally retaining and/or improving other beneficial physical properties. Conventional vinylidene chloride polymer powders can, in some instances, be blended directly with a suitable thermoplastic polymer to produce a satisfactory product. However, the crystalline powders of the present invention are advantageously incorporated into a polymer product by dispersing the powder in the desired non-solvent liquid reactant with moderate shear and thereafter carrying out the contemplated polymerization reaction. The latter method is critically employed in the preparation of many foamed polymeric products, particularly ïn the preparation of foamed polyurethane materials. The use of the crystalline vinylidene chloride polymer powders in the preparation of polymeric materials having enhanced physical properties will now be described by way of example with respect to the preparation of polyurethane materials--which may or may not be foamed. Polyurethane materials are prepared according to the methods well known in the art by reacting a polyfunctional isocyanate with a polyfunctional chemical compound having an active hydrogen in its structure such as a polyester, polyesteramide or -polyether or mixture of two or more of such materials. The latter component is generally referred to as the "active hydrogen-containing material" and is typically sufficiently liquid to permit mixing and reaction with the polyfunctional isocyanate in producing the polyurethane. The active hydrogen-containing materials conventionally used contain hydroxyl groups as the radicals having the active hydrogen and thus are generally termed "polyols1,. In addition, other hydroxyl-capped polymers useful as the polyol in preparing polyurethane resins include polyformals; the hydroxyl-terminated lactone polyesters; and alkylene oxide adducts of the alkyl alcohol-styrene polymers. For reasons of commercial availability and cost, it is conventional to use polyethers having hydroxyl-terminated chains in the preparation of polyurethane foams and either such polyethers or hydroxyl-terminated polyesters in preparing vulcanizable gum, adhesive, films, etc. The polyurethane end products may occasionally be crosslinked to some extent by including with the polyol (which is generally di- or polyfunctional) a smali amount of polyfunctional crosslinking agent. The active hydrogen-containing materials suitable for use in the preparation of polyurethane materials of the present invention are any of those known in the art and (1) which form stable and uniform dispersions with the crystalline vinylidene chloride polymer powders, which dispersions are preferably dilutable without the formation of undesirable precipitates with other components used to form the polyurethane; (2) which are liquids, at least at the temperatures used for preparing the dispersions and for the reaction with the polyisocyanate; and (3) which have at least two radicals reactive with the isocyanato radicals of the polyisocyanate so as to form a polymeric reaction product. The preferred active hydrogen-containing materials are the polyols having the aforementioned properties. The polyols employed can have hydroxyl numbers which vary over a wide range. The exact polyol employed depends, among other things, upon the end use of the poly urethane product to be produced. For example, in the case of foamed reaction products, the molecular weight of the hydroxyl number is selected to result in flexible, semiflexible, or rigid foams. In such applications, the polyols preferably possess a hydroxyl number of from 200 to 1000 when employed in rigid foam formulations, from 50 to 150 for semiflexible foams, and from 20 to 70 or more when employed in flexible foam formations. The crystalline vinylidene chloride polymer powders are preferably incorporated into polyurethanes by first forming a dispersion of the powder in the desired polyol. Generally, the resulting dispersions should have a viscosity low enough to permit ready mixing with additional quantities of polyol used, if any, and with the other components of the polyurethane reaction Furthermore, the resulting dispersions should be at least sufficiently stable to prevent sedimentation during the period required to carry out the polyurethane reaction. If the dispersions are to be prepared and then stored prior to use, they should be stable for a much longer period of time, e.g., usually at least three months. Generally, the dispersions of the present invention demonstrate such long-term stability requirements, particularly those dispersions containing the smaller vinylidene chloride polymer powder particles. The polymer powder/polyol dispersions of the present invention may be used in place of the polyols of the prior art in any of the processes used in preparing polyurethanes. Thus, the dispersions may be used in the prepolymer process, the quasi-prepolymer process or the one-shot process. The polyurethanes may be further reacted with epoxy resins, cured with sulfur, peroxides or other coring agents, or otherwise reacted or modified as known to those skilled in the art. Referring now to the use of the present crystalline vinylidene chloride polymer powders in the preparation of polymeric products in general, the amount of powder which will be incorporated into a desired polymeric material will depend upon the particular vinylidene chloride polymer powder used and upon the degree to which it is desired to enhance flame-retardancy and/or other beneficial physical properties in the resulting polymeric materials, as well as other technical and economic considerations. The resulting polymeric materials will generally contain an amount of the polymer powder which effectively enhances the physical properties thereof. This amount generally ranges from 2 tq 50 weight percent of crystalline vinylidene chloride polymer powder, preferably from 3 to 30 percent. Accordingly, the amount of powder dispersed in the non-solvent will be adjusted to produce such results. The resulting polymeric materials may be prepared so as to contain further modifying ingredients such as heat and light stabilizers, pigments, conventional flame-retardant synergists, and so forth, as necessary or desired for particular applications. With respect to polyurethane foam materials, in particular, surfactants or emulsifiers are frequently use to provide the necessary cell formation and growth for opti mum processability. However, polyurethane foam materials prepared from polyols containing crystalline vinylidene chloride polymer powders in accordance with the present invention do not generally require the use of such surfactants or emulsifiers. Nevertheless, such surfactants or emulsifiers may be advantageously employed especially when using powders prepared from the larger-sized crystalline vinylidene chloride polymer particles inasmuch as such particles have a reduced tendency to improve cell size in the polyurethane foam material. A user can, with only minimal experimentation, determine when such a surfactant or emulsifier will provide improved results. The crystalline vinylidene chloride polymer powders of the present invention can be moderately stabilized in an environment of high temperature and/or basic compounds, e.g., that environment encountered in preparing polyurethane foam materials, by sequential polymerization with non-vinylidene chloride monomers. Alternatively, or in addition thereto, conventional stabilizers for vinylidene chloride polymers, such as the hindered phenolic antioxidants and the like, may also be employed. Marginal improvement in the color of a polyurethane foam material is achieved by using epoxy stabilizers. Accordingly, it may be necessary for a user to determine by simple preliminary experimentation those stabilizers which will be suitably employed with the crystalline vinylidene chloride polymer powders. Suitable stabilizers are preferably used by adding them to the aqueous medium prior to or during the emulsion polymerization of the vinylidene chloride polymer. The following specific examples further illustrate the invention. Parts and percentages are by weight unless otherwise indicated. Example 1 The following recipe and technique were used to prepare a crystalline vinylidene chloride polymer powder which is dispersible in polyols and other non -solvents for vinylidene chloride polymers: Initial Water Phase 2000 g distilled water 16.56 g dihexyl sodium sulfosuccinate emulsifier (80% active) 10.6 g sodium persulfate Emulsifier Feed Stream 176.66 g C1 H H C12H7O(SO Na) emulsifier (45% active) in 1000 g aqueous solution Used 500 g in 12 hours (feed rate = 42 g/hr) Seed Latex Monomer 25 g methyl acrylate (MA) 475 g vinylidene chloride (VDC) Used 150 g in seed latex reaction Mixed Monomers 200 g MA 3800 g VDC Used 2500 g in 12 hours (feed rate = 208 g/hr) The initial water phase was introduced into a 2-gallon (7.6 liter) reactor and placed under a vacuum of about 25 inches (63.5 cm) Hg for 10 minutes while being heated to 520C. While agitating the contents of the rrac tor at 100 rpm, the vacuum was then shut off and 150 g ±' seed latex monomer was introduced. After the seed latex reaction had proceeded to approximately a 2 psi (0.141 kg/sq cm) pressure drop from the maximum pressure achie± introduction of the mixed monomers at 208 g/hr was begun and continued for 12 hours while concurrently adding the emulsifier stream at a rate of 42 g/hr. At the end of that period, the mixed monomer and emulsifier streams were shut off and a 2 percent solution of sodium bisulfite was added at a rate of 40 g/hr for 1.5 hours to complete the reaction. The resultant latex, containing a polymer comprising about 95 percent VDC and 5 percent MA, was aged for five days (85 percent of the latex particles were crystalline) at room temperature and then recovered by the following technique: 30 ml of 32 percent calcium chloride was added to 800 ml of water and heated to 50" with vigorous stirring. The latex was then added slowly while continuing the vigorous agitation. As soon as some growth of coagulated particles was observed, the mixture was cooled as rapidly as possible and the coagulum col- lected in a centrifuge. The coagulum was washed 10 minutes with a water spray and then allowed to dry in a tray at room temperature. 200 Grams of the resulting dried powder was mixed with 800 g polyether polyol having a MW of 4700, hydroxyl number 31.7-36.3 and triol functionality using a spatula. Thereafter, the mixture was continuously recycled through a Gifford-Wood colloid mill, operating at a speed of 10,000 rpm with a clearance of 0.004 inch (0.1 mm), for five minutes. The so-formed dispersion was examined by microscopy and many of the original latex particles having a size of 0.2 micron were observed. None of the examined particles had a size greater than about 100 microns. Example 2 The following alternate recipe and technique were used to prepare a vinylidene chloride polymer powder much like that of Example 1: Initial Water Phase 2500 g distilled water 16.56 g dihexyl sodium sulfosuccinate 80 emulsifier (80 percent active) 10.6 g sodium persulfate 19.88 g itaconic acid Seed Latex Monomer 25 g MA 475 g VDC Used 150 g in seed latex reaction Mixed Monomers 200 g MA 3800 g VDC Used 2500 g in 12 hours (feed rate = 208 g/hr) The initial water phase was introduced into a 2-gallon (7.6 liter) reactor and placed under a vacuum of about 25 inches (63.5 cm) Hg for 10 minutes while being heated to 450C with agitation at 120 rpm. When the reactor contents had reached a temperature of 45"C, the vacuum was shut off and 150 g seed latex monomer was added. After the seed latex reaction had proceeded to a 2 psi (0.141 kg/sq cm) pressure drop from maximum pres- sVre achieved, the mixed monomer stream was introduced at 208 g/hr and continued for 12 hours. At the end of that period, the mixed monomer stream was shut off and a 2 percent solution of sodium bisulfite was added at 40 g/hr for two hours to complete the reaction. The resulting latex, containing a polymer comprising about 95 percent VDC and 5 percent MA, was aged for about four days (80 percent of the latex particles crystallized) to permit the latex particles to crystallize and then coagulated by slowly adding 300 ml of latex to a vigorously agitated solution of 35 ml of calcium chloride in 960 ml water maintained at a temperature of 50 C. As soon as coagulum was observed, the mixture was quickly quenched in ice. The coagulum was then collected in a centrifuge, washed with water for 10 minutes, and then tray dried at room temperature. 200 Grams of the dried vinylidene chloride polymer was mixed with 800 g of the polyether polyol employed in Example 1 and then continuously recycled through a Gifford-Wood colloid mill, operating at 10,000 rpm with a clearance of 0.004 inch (0.1 mm) for five minutes. The resulting dispersion was uniform, stable, and contained particles of a size much like those of Example 1. Example 3 Three similar sequentially polymerized vinylidene chloride polymer powders, which differed only in the amount of non-vinylidene chloride monomer used in the sequential stage, were prepared according to the following recipe and technique: The polymerization described in Example 2 was repeated, but the sodium bisulfite was not added after the mixed monomer stream was shut off. Instead, the polymerization was permitted to continue until the pressure in the reactor leveled off and then the reactor was evacuated to reduce the concentration of residual vinylidene chloride monomer. Thereafter, the desired amount of the non-vinylidene chloride monomer feed, consisting of 96 percent methyl methacrylate (MMA) and 4 percent 1,3 -butylene glycol dimethacrylate (BGDM) crosslinking monomer, was added continuously over a 45 minute period. The reaction was then permitted to continue for three hours after which the reactor was again evacuated to reduce residual monomer. The so-formed latices, wherein the polymers respectively contained, 5 percent, 10 percent, and 20 percent non-vinylidene chloride polymer based on the weight of the VDC/MA polymer prepared in the first stage, were aged for seven days (85 percent of latex particles crystallized) and then recovered by the procedure described in Example 2. Example 4 Various polymer/polyol dispersions in accordance with the present invention were prepared by admixing in an Eppenbach shear homogenizer a suitable amount of polyol with each of the vinylidene chloride polymer powders obtained in Examples 2 and 3. Each dispersion contained 20 percent of the respective polymer powder. Each of the dispersions was then passed twice through a water -cooled Gifford-Wood colloid mill having a 2 inch (5 cm) diameter rotor operating at 10,000 rpm. In the first pass a gap setting of 0.020 inch (0.5 mm) was used and in the second pass a gap setting of 0.004 inch (0.1 mm) was used. It was noted that the dispersions containing the polymers of Example 3 had considerably greater viscosity than the dispersion containing the polymer of Example 2, and that viscosity increased with the ambunt of non-vinylidene chloride polymer used. The dispersions were then stored for one month and then examined for dispersion stability. The dispersion containing the polymer of Example 2 showed no signs of sedimentation and the dispersions containing the polymers of Example 3 showed visible, but minimal, sediment. This may have been due to the inherently larger size of the latex particles obtained in Example 3. Nevertheless, all of the dispersions appeared to be suitable for use in the preparation of polyurethane materials. Example 5 Polyurethane foam samples were prepared with two of the polymer/polyol dispersions of Example 4 according to the following recipe: Amount Ingredient (Grams) Polyol 490.0 Polymer/polyol dispersion 210.0 Non-hydrolyzable silicone 14.0 surfactant Solution of 33% triethylene 2.1 di amine in dipropylene glycol Solution of 70% bis(N,N-dimethyl- 0.7 aminoethyl)ether in dipropylene glycol Solution of 26% 1,4-dimethylpipera- 1.75 zine and 75% bis(2-morpholine- ethyl)ether Dibutyl tin dilaurate 0.049 Isophorone diamine 4.2 Water 17.5 A mold, having dimensions of 15.5 x 15.5 x 4.5 inches (39 x 39 x 11.4 cm), and cover therefore were first preheated to 880C. After applying a mold release agent to the interior surfaces of the mold and cover, they were allowed to cool to about 540 to 600C. The above-identified ingredients were then mixed in a high-speed blender operating at about 1800 to 2400 rpm for about 20 seconds. Thereafter, 231 g of a 90/10 mixture of toluene diisocyanate/polymethylene polyphenylisocyanate was added and the mixture was further blended for about 3 to 3.5 seconds. The resulting mixture was poured into the mold, the cover was secured, and the mold was placed in a 121 C oven for eight minutes. After eight minutes, the resulting foam pad was removed from the mold, crushed, and Then cured at 1210C for 30 minutes. After aging the foams for seven days at room temperature they were tested for physical properties according to ASTM-D-1564 and ASTM-D-2406. The results of these tests are shown in Table I, wherein Samples 5A and 5B identify foams prepared from the' polymer/polyol dispersions containing, respectively, the powder prepared in Example 2 and the powder prepared in Example 3 having a 10 weight percent "cap". Both foams passed the Department of Transportation Motor Vehicle Safety Standard No. 302, indicating the flame-retardancy of such materials. Sample 5B had slightly reduced lpad- -bearing properties but less discoloration than Sample 5A. Accordingly, these effects can be balanced to obtain the particular results desired by a user. TABLE I Physical Property 5A 5B Density - lb/cubic ft (g/l) 2.82 (45.17) 2.79 (44.69) Tensile - psi (kg/sq cm) 22.3 (1.56) 19.4 (1.36) Elongation (%) 164 134 Tear - inch (cm) 2.37 (6.02) 2.20 (5.59) Compression Set 75% CN 9.6 8.7 75% CT 7.3 6.7 Humid Age 50% CLD 29.4 27.3 50% SET 15.9 13.3 ILD - lb/50 sq in (g/sq cm) 25% 37.5 (52.88) 44.9 (63.31) 65% 99.1 (139.73) 97.7 (137.76) Return 25% 31.2 36.9 % Hystersis return 83 82 Modulus 2.65 2.18 Example 6 In accordance with the present invention, a "capped!' crystalline polymer powder, which is suitably incorporated into a polymer/polyol dispersion for use in the preparation of polyurethane foam materials, was prepared according to the following recipe and technique: : Initial Water Phase 3200 g distilled water 18.2 g dihexyl sodium sulfosuccinate 80 emulsifier 10.6 g sodium persulfate 19.88 g itaconic acid Seed Latex Monomer 500 g VDC 2.5 g IRGANOX 1076 stabilizer Used 150 g in seed latex reaction Monomers Stage I 4000 g VDC 20 g IRGANOX 1076 stabilizer Used 2500 g in 12 hours (feed rate = 208 g/hr) Stage II 500 g MA Used 132.8 g in 2 hours (feed rate = 66.4 g/hr) Stage III 600 g MMA 24 g BGDM Used 256 g in 4 hours (feed rate = 66.4 g/hr) Emulsifier Feed Stream 88.2 g C12H25C12H7O(SO Na) emulsifier (45% active) in 750 9 us solution Used 500 g in 12 hours (feed rate = 42 g/hr) The initial water phase was introduced into a 2-gallon (7.6 liter) reactor and placed under a vacuum of about 25 inches (63.5 cm) Hg for 10 minutes while being heated to 520C. While agitating the contents of the reactor at 100 rpm, the vacuum was then shut off and 150 y of the seed latex monomer was introduced. After the seed latex reaction had proceeded to approximately a 2 psi (0.141 kg/sq cm) pressure drop from the maximum pressure achieved, introduction of the Stage I monomer at 208 g/hr was begun and continued for 12 hours while concurrently adding the emulsifier stream at a rate of 42 g/hr.-- At the end of that period, the Stage I monomer and emulsifier stream were shut off. 15 Minutes after the end of the Stage I monomer and emulsifier stream addition, introduction of the Stage II monomer at 66.4 g/hr was begun and continued for two hours. At the end of that period, the Stage II monomer stream was shut off and the Stage III monomer was introduced at 64 g/hr for four hours. The resultant latex was aged for four days at room temperature (84 percent of latex particles crystallized) and then recovered by the following technique: 30 ml of 32 percent calcium chloride was added to 800 ml of water and heated to 500C with vigorous stirring. The latex was then added slowly while continuing the vigorous agitation. As soon as some growth of coagulated particles was observed, the mixture was cooled as rapidly as possible and the coagulum collected in a centrifuge. The coagulum was washed 10 minutes with a water spray and then allowed to dry in a tray at room temperature. Example 7 Vinylidene chloride polymer latexes at two particle sizes 4ere prepared from a 95/5 VDCA mixture in a manner similar to that of Example 1. The latex particle size was controlled by varying the amount of emulsifier. The number of particles (percent) which crystallized as a function of latex age was determined by transmission electron microscopy. The results, as shown in Table II, demonstrate that at a given composition the rate of development of crystalline particles varies with latex particle size. TABLE II Latex Age ¯ ¯ Percent Crystalline Particles (days) 1300 A Particles 2130 A Particles 0 38 38 1 58 86 2 72 '92 4 88 95 8 94 100 12 98 100 After various aging periods, samples of the latex containing the 2130 particles were coagulated at 500C and dried in the same manner as in Example 1. 20 Weight percent of each of the resulting powders were mixed with a polyol having a room temperature viscosity of 900 to 1000 cps and the mixture was passed once through a Gifford-Wood colloid mill operating at 10,000 rpm with a gap setting of 0.004 inch (0.1 mm) and then twice through a Gaulin homogenizer operating at 5000 psi (350 kg/sq cm). Table III summarizes The microscopy evaluation of the dispersions as a function of latex age and relative number of crystalline particles. It is noted that the particles in the latex containing 38 percent crystalline particles underwent extensive irreversible coalescence during coagulation and that the coagulated particles did not redisperse in the polyol. As the number of crystalline particles increased above 50 percent, however, the extent of irreversible coalescence upon chemical coagu- lation decreased and the ability to redisperse the powder in an organic non-solvent increased. For example, at 86 percent crystalline latex particles minimal irreversible coalescence occurred and the powder redispersed such that more than 40 percent of the particles in the dispersion were of the original latex particle size and essentially all of the particles were of a size less than 100 microns. TABLE III Approximate Maximum Percent of Diameter of Percent Original Latex Undispersed Crystalline Sedimentation Particles in Agglomerates Latex Age Particles Time % Settled Dispersion (Microns) Fresh 38 1 day 95 none > 1000 1 day 86 1 month trace 50-75 20 4 days 95 1 month trace 50-75 60 6 days 100 1 month 40 20-30 500 Example 8 It tidal Water Phase 2500 g distilled water 16.56 g dihexyl sodium sulfosuccinate 10.6 g sodium persulfate 19.88 g itaconic acid Seed Latex Monomer 20 g butyl acrylate (four parts) 480 g vinylidene chloride Used 150 g in seed latex reaction Mixed Monomers 3640 g vinylidene chloride 360 g butyl acrylate (nine parts) Used 2500 g in 12 hours (feed rate = 208 g/hr) The initial water phase was introduced into a 2-gallon (7.6 liter) reactor and placed under a vacuum of about 25 inches (63.5 cm) Hg for 10 minutes while being heated to 520C with agitation at 120 rpm. When the reactor contents had reached a temperature of 520C, the vacuum was shut off and 150 grams of seed latex monomer was added. After the seed latex reaction has proceeded to a 2 psi (0.141 kg/sq cm) pressure drop from maximum pressure achieved, the mixed monomer stream was introduced at 208 g/hr and continued for 12 hours. At the end of that period, the mixed monomer stream was shut off and a 2 percent solution of sodium bisulfite was added at 40 g/hr for two hours to complete the reaction. The resulting latex contained a polymer comprising 91 percent VDC and 9 percent butyl acrylate with a seed latex composition of 96 percent VDC and 4 percent butyl acrylate which was 87 percent crystalline within seven days. Example 9 Batch Emulsion Polymerization Initial Reactor Charge 1750 g distilled water 5 g alkyl benzene sulfonate emulsifier 0.13 g sodium formaldehyde sulfoxylate 0.93 g 30 percent hydrogen peroxide 800 g vinylidene chloride 200 g vinyl chloride Aqueous Feed Stream 500 g distilled water 0.7 g sodium formaldehyde sulfoxylate -10 g alkyl benzene sulfonate emulsifier The initial water, emulsifier and reducing agent was introduced into a 3-liter reactor with agitation at 300 rpm. While heating the contents of the reactor to the polymerization temperature of 450C, the reactor was evacuated to 28 inches (71 cm) Hg. When the contents of the reactor reached 450C, the vacuum was shut off and the mixed monomers and initial shot of hydrogen peroxide were introduced into the reactor. Addition of the aqueous stream was started at 43 g/hr two hours after addition of the mixed monomers and peroxide. Approximately seven hours later, the polymerization was completed and at a 15 psi (1.05 kg/sq cm) pressure drop, the aqueous stream was shut off and the reactor was cooled to room temperature. The resulting latex contained a polymer comprising 80 percent VDC and 20 percent vinyl chloride, which was 94 percent crystalline within seven days.

Claims: Claims: 1. A process for preparing a crystalline vinylidene chloride polymer powder which is dispersible in non -solvent organic liquids which comprises emulsion polymeri- zing monomers comprising a major proportion of vinylidene chloride to prepare a latex wherein the latex particles have a diameter less than one micron1 aging the resulting latex until from 75 to 100 percent of the latex particles are crystallized and then recovering the polymer from the latex. 2. Process of Claim 1 which comprises emulsion polymerizing the vinylidene chloride with at least one alkyl or hydroxyalkyl ester of acrylic or methacrylic acid, a vinyl ester of a saturated carboxylic acid, an amide or nitrile of an ethylenically unsaturated carboxylic acid, an ethylenically unsaturated carboxylic acid or alcohol or a vinyl halide. 3. Process of Claim 2 which comprises emulsion polymerizing from 94 to 97 parts by weight of vinylidene chloride with from 6 to 3 parts by weight of methyl acrylate. 4. Process of any one of Claims 1 to 3 wherein up to 20 weight percent of a sequentially polymerizable monomer mixture comprising an ethylenically unsaturated non-vinylidene chloride monomer is added to the latex and the monomer mixture polymerized. 5. Process of Claim 4 wherein the monomer mixture is added after the latex has been aged. 6. Process of Claim 5 wherein the non-vinylidene chloride monomer is methyl methacrylate. 7. Process of Claim 5 or 6 wherein the polymer resulting from the polymerization of the sequentially polymerizable monomer has a second order transition temperature of at least 600C. 8. Composition comprising a crystalline vinyli- dene chloride polymer powder prepared according to the process of any one of Claims 1 to 7. 9. Composition comprising a crystalline vinylidene chloride polymer powder prepared according to the process of any one of Claims 1 to 7 and a non-solvent organic liquid. 10. Composition of Claim 9 wherein the non -solvent organic liquid is a polyol.

Inventors: BENSON, JACK HOWARD, FERNANDEZ, REET T., GIBBS, DALE SABIN
Applicants: THE DOW CHEMICAL COMPANY
Application year: 1979
Main classification: C08F14
IPC codes: C08J9, C08J3, C08F14, C08F214, C08F6, C08F2