This invention relates to a process of cleaning a surface soiled with a staining agent. The method includes the steps of applying to the soiled surface a highly cross-linked macroporous hydrophobic copolymer which contains a chemical entrapped therein which is a solvent for the staining agent present on the soiled surface, dissolving the staining agent with the solvent, absorbing the staining agent into the solvent entrapped copolymer, and removing the copolymer containing the solvent and the dissolved staining agent from the surface.
This technology was expanded and the precipitant was variously described in the patent literature as a diluent, porogen, active ingredient, solvent, functional material, and volatile agent. For example, in U.S. Pat. No. Re. 27,026, issued Jan. 12, 1971, porous beads of a diameter less than ten microns are disclosed. Among the monomers used to produce the beads are ethyl methacrylate, divinyl benzene, and ethylene glycol dimethacrylate. In U.S. Pat. No. 3,418,262, issued Dec. 24, 1968, there is described a bead characterized as having a rigid sponge structure, and wherein the porogenic agent employed is an acid such as stearic acid. Intermediates in bead form were produced in U.S. Pat. No. 3,509,078, issued Apr. 28, 1970, using polymeric materials such as polyethylene glycols as the precipitant material during the in situ suspension polymerization process. The macroporous character of such bead construction is graphically portrayed and illustrated in FIG. 1 of U.S. Pat. No. 3,627,708, issued Dec. 14, 1971. Beads termed "pearls" are produced, and containing active ingredients therein such as water or various alcohol ethers. The pearls are crosslinked to the extent of about twenty percent. In U.S. Pat. No. 3,637,535, issued Jan. 25, 1972, beads with a sponge structure are said to be capable of being compressed to an imperceptible powder. These beads are capable of being loaded with as much as 200-300% of active ingredients such as white spirit, and benzin. A rigid porous bead of a trifunctional methacrylate is taught in U.S. Pat. No. 3,767,600, issued Oct. 23, 1973. Such beads have a size of 10-900 microns, and various other monomers which can be employed include diacetone acrylamide, and ethylhexyl, hydroxyethyl, and hydroxypropyl methacrylates. Paraffin wax in an amount of 5-100% is used to form the microscopic network of channels in U.S. Pat. No. 3,989,649, issued Nov. 2, 1976. The wax may be removed from the bead structure by solvent extraction.
While many of the foregoing U.S. patents relate to ion exchange technology, a bead similar to those previously described is employed as a carrier for enzymes in U.S. Pat. No. 4,208,309, issued June 17, 1980. Such beads are of the size of about 0.1 mm. U.S. Pat. No. 4,661,327, issued Apr. 28, 1987, describes a macroreticular bead containing a magnetic core. The use of hard crosslinked porous polymeric beads in cosmetics as carriers is taught in U.S. Pat. No. 4,724,240, issued Feb. 9, 1988, wherein various emollients and moisturizers are entrapped therein. These beads are said to be capable of entrapping materials such as 2-ethylhexyl oxystearate, arachidyl propionate, petroleum jelly, mineral oil, lanolin, and various siloxanes. The size of the beads ranges from 1-3,000 microns. Typical monomers include ethylene glycol dimethacrylate, lauryl methacrylate, trimethylol propane trimethacrylate, and dipentaerythritol dimethacrylate. "In situ" hydrophobic powders and "in situ" beads may be produced in accordance with the teaching of this patent. Beads having a rigid sponge structure are also described in U.S. Pat. No. 4,690,825, issued Sept. 1, 1987, and wherein the beads function as a delivery vehicle for a host of materials including pigments, vitamins, fragrances, drugs, repellants, detergents, and sunscreens. The beads have a size of 10-100 microns and are preferably of a monomer system of styrene-divinyl benzene. Crosslinking is said to range from 10-40 percent. U.S. Pat. No. 4,806,360, issued Feb. 21, 1989, describes a post adsorbent bead which contains a melanin pigment for use as a sunscreen.
The foreign patent literature includes West German Offenlegungsschrift No. P-2608533.6, published Sept. 30, 1976, and wherein porous polymeric beads produced by "in situ" suspension polymerization are provided, and which are adapted to release perfumes. A controlled release of the fragrance is disclosed, providing utility for such beads in the home, automobiles, airplanes, railway cars, hospitals, classrooms, conference centers, and gymnasiums. Canadian Patent No. 1,168,157, issued May 29, 1984, describes hard, discrete, free flowing, bead constructions in which the beads entrap a series of functional materials which can be incorporated into toilet soap, body powder, and antiperspirant sticks. The Canadian Patent, it is noted, is the equivalent of European Patent No. 61,701, issued on July 16, 1986, both of which are foreign equivalents of the parent case of the '240 patent. In European International Publication No. 0252463A2, published Jan. 13, 1988, there is disclosed a bead having a hydrophobic polymer lattice, and which entraps numerous non-cosmetic materials such as pesticides, pharmaceuticals, pheromones, and various categories of chemicals. Steroids are entrapped, for example, in the porous beads of PCT International Publication No. WO-88/01164, published on Feb. 25, 1988. The steroids are adrenocortical steroids or various anti-inflammatory type steroids. It should therefore be apparent that what began as a simple ion exchange bead concept has rapidly grown into a technology of widely varied application.
In accordance with the present invention, copolymer powders are employed in novel processes not believed to be taught in the prior art, as exemplified by the foregoing patents. Those patents, in general, relate to suspension polymerization processes for the production of porous polymeric and copolymeric spheres and beads in which the precipitant is present during polymerization. These are defined as an "in situ" process.
Thus, according to the prior art, crosslinked porous copolymers in particle form can be produced by at least three distinct processes. One process produces beads by "in situ" suspension polymerization. Another process produces beads by suspension polymerization but the beads are "post adsorbed" with an active ingredient after the volatile porogen is removed. In a third process, powders are produced by "in situ" precipitation polymerization.
What has been accomplished in accordance with the present invention, however, is a unique concept differing from all of the foregoing methods, and wherein post adsorbent powders and beads are produced and used in a novel fashion.
SUMMARY OF THE INVENTION
This invention relates to a process of cleaning a surface soiled with a staining agent. The method includes the steps of applying to the soiled surface a highly cross-linked macroporous hydrophobic copolymer which contains a chemical entrapped therein which is a solvent for the staining agent present on the soiled surface, dissolving the staining agent with the solvent, absorbing the staining agent into the solvent entrapped copolymer, and removing the copolymer containing the solvent and the dissolved staining agent from the surface.
In certain of the more specific embodiments of the present invention, one monomer of the copolymer is a monounsaturated monomer and the monounsaturated monomer is lauryl methacrylate. One monomer of the copolymer can also be a polyunsaturated monomer and the polyunsaturated monomer is selected from the group consisting of ethylene glycol dimethacrylate and tetraethylene glycol dimethacrylate.
The copolymer is in the form of a powder and the powder is a combined system of particles, the system of particles including unit particles of less than about one micron in average diameter, agglomerates of fused unit particles of sizes in the range of about twenty to eighty microns in average diameter, and aggregates of clusters of fused agglomerates of sizes in the range of about two-hundred to about twelve-hundred microns in average diameter. The soiled surface can be a textile in which case the copolymer containing the solvent is pressed and rubbed into the textile surface after being applied to the surface. The solvent is evaporated from the copolymer following removal of the copolymer containing the solvent and the staining agent from the surface, and the solvent free copolymer containing the staining agent is discarded.
The copolymer containing the solvent and the staining agent can be removed from the surface by brushing the surface, followed by the application of pressurized air to the brushed surface. The staining agent may be butter, grass, and motor oil and the soiled surface treated in accordance with the present invention could be wool, paper, cotton, silk, rayon, linen, and polyester. The solvent is preferably heptane, methylene chloride, and ethyl alcohol, although other appropriate solvents may be employed.
The invention is also directed to a more simplified process in which no solvent is employed. In this case, the steps are related to a process of cleaning a surface soiled with a staining agent by applying to the soiled surface a highly cross-linked macroporous hydrophobic copolymer, rubbing and mixing the copolymer into the staining agent on the soiled surface, absorbing the staining agent into the copolymer, and removing the copolymer containing the staining agent from the surface. The staining agent is, for example, grease, lipid deposits, and plaque, while the soiled surface may be glass, spectacle lenses, and dentures. The copolymer containing the staining agent is removed from the surface by flushing the surface with water.
A precipitation polymerization process is used for producing the macroporous cross-linked copolymer. In the process, there is copolymerized at least one monounsaturated monomer and at least one polyunsaturated monomer in the presence of an organic liquid which is a solvent for and dissolves the monomers but not the copolymer. The copolymerization of the monomers is initiated by means of a free radical generating catalytic compound, precipitating a copolymer in the solvent in the form of a powder. A dry powder is formed by removing the solvent from the precipitated copolymeric powder.
The solvent is preferably isopropyl alcohol, although ethanol, toluene, heptane, xylene, hexane, ethyl alcohol, and cyclohexane, may also be employed. The monounsaturated monomer and the polyunsaturated monomer can be present in mol ratios of, for example, 20:80, 30:70, 40:60, or 50:50. The process includes the step of stirring the monomers, solvent, and the free radical generating catalytic compound, during copolymerization. Preferably, the dry powder is formed by filtering excess solvent from the precipitated powder, and the filtered powder is vacuum dried. The powder may then be "post adsorbed" with various functional materials.
The powders of the present invention may be used as carriers or adsorbents for materials such as water, aqueous systems, emollients, moisturizers, fragrances, dyes, pigments, flavors, drugs such as ibuprofen, phosphoric acid, insect repellents, vitamins, sunscreens, detergents, cosmetics, pesticides, pheromones, herbicides, steroids, sweeteners, pharmaceuticals, and antimicrobial agents. Finely divided solids such as analgesic materials can be adsorbed by dissolving the finely divided analgesic in a solvent, mixing the analgesic and solvent with the powder, and removing the solvent. Other post adsorbable materials include alkanes, alcohols, acid esters, silicones, glycols, organic acids, waxes, and alcohol ethers.
These and other objects, features, and advantages, of the present invention will become apparent when considered in light of the following detailed description, including the accompanying drawings.
IN THE DRAWINGS
FIG. 1 is a photomicrograph of the various components of the complex structure of the powder produced in Example I, and including unit particles, agglomeratures, and aggregates.
FIGS. 2 and 3 are photomicrographs of the agglomerates and aggregates of FIG. 1, respectively, shown on a larger scale.
FIG. 4 is a photomicrograph of a polymer bead produced by suspension polymerization.
FIG. 5 is a photomicrograph of the bead of FIG. 4 with a portion of the shell removed to reveal the interior structure of the bead.
FIG. 6 is a photomicrograph of a copolymeric powder material. The powder is shown in magnification as it appears when the agitation rate employed in the process for producing the powder is zero rpm.
FIGS. 7-10 are additional photomicrographs of copolymeric powder materials. The powder is shown in magnification as it appears when the agitation rate employed in the process for producing the powder varies from seventy-five rpm up to eight hundred rpm.
In the above figures in the drawing, the magnification is indicated in each instance. For example, the magnification in FIGS. 6-9 is 1000.times., and 2000.times.in FIG. 10. FIGS. 6-10 also include an insert identifying a length approximating ten microns for comparative purposes.
It should be pointed out, that in viewing the various figures, one will note that as the rate of stirring is increased from zero rpm up to eight hundred rpm, that the size of the unit particles increase. This is in direct opposition to what has been traditionally observed in suspension polymerization systems, wherein increases in stirring rates decrease particle size. Because of the increased size of the unit particles shown in FIG. 10 and the resulting decrease in surface area, the adsorptive capacity of these large particles is less than the adsorptive capacity of the smaller sized particles shown in FIGS. 6-9.
The most effective unit particles can be produced if the rate of stirring is maintained below about three hundred rpm, although particles produced at rates beyond three hundred rpm are useful and adsorptive, but to a lesser extent.
DETAILED DESCRIPTION OF THE INVENTION
The material of the present invention, can be broadly and generally described as a crosslinked copolymer capable of entrapping solids, liquids, and gases. The copolymer is in particulate form and constitutes free flowing discrete solid particles even when loaded with an active material. When loaded, it may contain a predetermined quantity of the active material. One copolymer of the invention has the structural formula: ##STR1## where the ratio of x to y is 80:20, R' is --CH.sub.2 CH.sub.2 --, and R" is --(CH.sub.2).sub.11 CH.sub.3.
The copolymer is highly crosslinked as evidenced by the foregoing structural formula, and is more particularly a highly crosslinked polymethacrylate copolymer. This material is manufactured by the Dow Corning Corporation, Midland, Mich., U.S.A., and sold under the trademark POLYTRAP.RTM.. It is a low density, highly porous, free-flowing white particulate, and the particles are capable of adsorbing high levels of lipophilic liquids and some hydrophilic liquids, while at the same time maintaining a free-flowing particulate character.
In the powder form, the structure of the particulate is complex, and consists of unit particles less than one micron in average diameter. The unit particles are fused into agglomerates of twenty to eighty microns in average diameter. These agglomerates are loosely clustered into macro-particles termed aggregates of about 200 to about 1200 microns in average diameter.
Adsorption of actives to form post adsorbent powder, can be accomplished using a stainless steel mixing bowl and a spoon, wherein the active ingredient is added to the empty dry powder, and the spoon is used to gently fold the active into the powder. Low viscosity fluids may be adsorbed by addition of the fluids to a sealable vessel containing the powder and tumbling the materials until a consistency is achieved. More elaborate blending equipment such as ribbon or twin cone blenders can also be employed.
The following example illustrates the method for making a post adsorbent powder, of the type illustrated in FIGS. 1-3 and 6-10.
EXAMPLE I
A hydrophobic porous copolymer was produced by the precipitation polymerization technique by mixing in a five hundred milliliter polymerization reactor equipped with a paddle type stirrer, 13.63 grams of ethylene glycol dimethacrylate monomer, or eighty mole percent, and 4.37 grams of lauryl methacrylate monomer, or twenty mole percent. Isopropyl alcohol was added to the reactor as the solvent in the amount of 282 grams. The monomers were soluble in the solvent, but not the precipitated copolymer. The process can be conducted with only polyunsaturated monomers if desired. The mixture including monomers, solvent, and 0.36 grams of catalytic initiator benzoyl peroxide, was purged with nitrogen. The system was heated by a water bath to about sixty degrees Centigrade until copolymerization was initiated, at which time, the temperature was increased to about 70-75 degrees Centigrade for six hours, in order to complete the copolymerization. During this time, the copolymer precipitated from the solution. The copolymerization produced unit particles of a diameter less than about one micron. Some of the unit particles adhered together providing agglomerates of the order of magnitude of about twenty to eighty microns in diameter. Some of the agglomerates adhered further and were fused and welded one to another, forming aggregates of loosely held assemblies of agglomerates of the order of magnitude of about two to eight hundred microns in diameter. The mixture was filtered to remove excess solvent, and a wet powder cake was tray dried in a vacuum oven. A dry hydrophobic copolymeric powder consisting of unit particles, agglomerates, and aggregates was isolated.
The adsorptive capacity of the hydrophobic particulates produced in Example I, as a function of the stirring rate, was determined. The stirring rate during the reaction in Example I significantly influenced the adsorption properties of the particulate materials. The adsorptivity of the particulate materials decreases with an increase in stirring rate, and the density of the particulates increases. These results are set forth in Tables I-III.
TABLE I
__________________________________________________________________________
Average
Average Average
Agitation
Bulk Density
Aggregate
Agglomerate
Unit
Rate Size Size Size Particle
Adsorption
(RPM)
(g/cc) (.mu.)
(.mu.) Size (.mu.)
Capacity*
__________________________________________________________________________
0 0.067 182.5 33.9 1.0 83.0
75 0.077 140.6 36.6 0.5 84.8
150 0.071 149.8 39.8 0.8 83.0
300 0.293 47.0 34.0 1.5-2.0
58.3
800 0.440 -- 10.0 3.0-5.0
37.7
__________________________________________________________________________
* = Percent Silicone Oil
TABLE II
______________________________________
Stirring Adsorption Capacity %
Speed Mineral Organic
RPM Water Oil Glycerine
Ester*
______________________________________
0 0 80 75 80
75 0 83.9 75 81.5
150 0 80 75 80
300 0 54.5 58.3 54.5
______________________________________
* = 2ethylhexyl-oxystearate
TABLE III
______________________________________
Adsorption Capacity %
Mineral 2-ethylhexyl
Silicone Density (g/cm.sup.3)
RPM Oil oxystearate
Oil Bulk Tapped
______________________________________
0 82.5 82.5 86.5 0.0368
0.0580
75 82.3 82.2 86.5 0.0462
0.0667
150 82.3 82.3 86.3 0.0527
0.0737
200 81.5 81.5 85.7 0.0554
0.0752
250 79.2 80.0 84.8 0.0636
0.0859
300 68.8 68.8 75.0 0.1300
0.1768
450 58.3 58.3 61.5 0.1736
0.2392
600 54.5 54.5 60 0.1933
0.2792
700 42.2 42.5 45.7 0.2778
0.4142
800 33.3 28.6 33.3 0.3862
0.5322
1000 32.8 28.5 32.9 0.3808
0.5261
______________________________________
In the foregoing tables, it can be seen that adsorption and density, as a function of stirring rate, was determined for several fluids including a silicone oil, water, mineral oil, glycerine, and an organic ester. From zero rpm up to about 250 rpm, the adsorptivity of the porous copolymeric powder particulates of Example I remained essentially consistent. However, at about three hundred rpm, there was a substantial decrease in adsorptivity, which decrease became more apparent as the stirring rate was increased up to about one thousand rpm. A similar pattern is evidenced by the data which are reflective of the density.
This phenomenon is more apparent in the photomicrographic figures of the drawing. Thus, it can be seen from FIG. 6, that the particle size of the unit particles increases as the stirring rate is increased, as evidenced by FIG. 10. A progression in this phenomenon can be observed in FIGS. 7-9.
While the procedure of Example I is a precipitation polymerization process and not a suspension polymerization system, the prior art dealing with suspension polymerization processes, teaches that an increase in stirring rate causes a decrease in particle size. This is documented, for example, in U.S. Pat. No. 4,224,415, issued Sept. 23, 1980, and in the PCT International Publication. The PCT International Publication employs stirring rates upwards of nine hundred to twelve hundred rpm. In Example I of the present invention, however, increases in stirring rates not only did not decrease the particle size, but in fact had exactly the opposite effect, causing the unit particle size to increase. As the rate of stirring increased from zero rpm up to one thousand, the density of the particles increased and the adsorptive capacity decreased.
In accordance with the above, it is possible to tailor porous adsorbent powders of a particular particle size and adsorptivity by means of stirring rate. Thus, with large unit particles in FIG. 10, the adsorptive capacity is less than the adsorptive capacity of smaller sized unit particles in FIGS. 6-9. While the most effective particles are produced when the rate of stirring is maintained below about three hundred rpm, particles produced at rates beyond three hundred rpm are useful.
It is important to understand that the method of Example I for the production of porous copolymer particulate powder materials is characterized as a precipitation polymerization technique. In accordance with the technique, monomers are dissolved in a compatible volatile solvent in which both monomers are soluble. Polymer in the form of a powder is precipitated and the polymer is insoluble in the solvent. No surfactant or dispersing aid is required. The materials produced are powders and not spheres or beads. The powder particulates include unit particles, agglomerates, and aggregates. The volatile solvent is subsequently removed resulting in a dry powder, which can be post adsorbed with a variety of functional active ingredients. The suspension polymerization process on the other hand, provides that polymerization be carried out in water, and in some cases chloroform or chlorinated solvents. The monomers, the active, and the catalyst, form beads or droplets in water, and polymerization occurs within each bead. A surfactant or stabilizer, such as polyvinyl pyrrolidone, is required in order to prevent the individually formed beads and droplets from coalescing. The resulting beads, with the active material entrapped therein, include a substantially spherical outer crust or shell, the interior of which contains a macroporous structure of fused unit particles, agglomerates, and aggregates. The bead is about ten microns in average diameter to about one hundred-fifty microns, depending upon the rate of agitation employed during the process. Such beads are shown in FIGS. 4 and 5, and the process is set forth in Example III.
Some unique features of the powders of Example I and FIGS. 1-3 and 6-10 are their ability to adsorb from sixty to eighty percent of a liquid and yet remain free flowing. The materials provide a regulated release of volatile ingredients such as cyclomethicone entrapped therein, and have the capability of functioning as carriers for other non-volatile oils. Loaded powders disappear when rubbed upon a surface. This phenomenon is believed due to the fact that large aggregates of the material scatter light rendering the appearance of a white particulate, however, upon rubbing, these large aggregates decrease in size approaching the range of visible light and hence seem to disappear. The materials find applications in diverse areas such as cosmetics and toiletries, household and industrial products, pesticides, pheromone carriers, and pharmaceuticals. The materials do not swell in common solvents and are capable of physically adsorbing active ingredients by the filling of interstitial voids by capillary action. The active ingredients are subsequently released by capillary action or wicking from the voids within the particulates.
The following example illustrates a precipitation polymerization process in which an organic ester is entrapped "in situ" in the polymer powder.
EXAMPLE II
7 grams of 2-ethylhexyl oxystearate was mixed with 1.5 grams of ethylene glycol dimethacrylate and 1.5 grams of lauryl methacrylate in a glass test tube. The solution was deaerated for five (5) minutes and 0.1 ml of t-butyl peroctoate was added and mixed while heating to 80 degrees Centigrade in an oil bath. After 20 minutes, the contents solidified; and the mixture was maintained at about 80 degrees Centigrade for an additional hour to assure full polymerization. A semi-soft, heterogeneous white opaque polymer mass resulted containing the entrapped ester.
The powder of Example II differs from the powder of Example I in that the solvent in Example I is removed resulting in a dry empty powder which is post adsorbed with other functional materials. The powder of Example II is otherwise similar to the material shown in FIGS. 1-3.
Example III illustrates a process for the production of beads as shown in FIGS. 4 and 5. The process is suspension polymerization and an organic ester is entrapped "in situ".
EXAMPLE III
1.20 grams of polyvinyl pyrrolidone was dissolved in 1500 ml of water in a 2000 ml three necked resin flask equipped with a stirrer, thermometer and nitrogen purge. A solution of 335 grams of 2-ethylhexyl oxystearate, 132 grams ethylene glycol dimethacrylate, 33 grams 2-ethylhexyl methacrylate, and 5 ml t-butyl peroctoate, was bubbled with nitrogen for 5 minutes. The resultant mix was slowly added to the stirred aqueous solution of polyvinyl pyrrolidone at 22 degrees Centigrade under nitrogen. The temperature was raised to 80 degrees Centigrade with constant agitation and held until polymerization started in approximately 15 minutes, and maintained at 80 degrees Centigrade for an additional 2 hours to complete the reaction. Semi-soft, white opaque beads were collected by filtering off the supernatant liquid and dried to remove any excess water. The beads weighed 450 g for a yield of 90%, and were 0.25 to 0.5 mm in diameter. Other protective colloids such as starch, polyvinyl alcohol, carboxymethyl cellulose, methyl cellulose, or inorganic systems such as divalent alkali metal hydroxides, for example MgOH, may be used in place of the polyvinyl pyrrolidone suspending medium.
In Example III macroporous polymers submicron in size are produced with two or more monomers, at least one monomer of which contains more than a single double bond. The polymerization is conducted in the presence of an active ingredient which does not dissolve or swell the resulting polymer. The monomers and the active ingredient are mutually soluble, but are insoluble in the aqueous suspending medium in which droplets are formed. Polymerization occurs within suspended droplets, and beads or spheres are produced. The active ingredient which is polymerized "in situ" is entrapped and contained within the beads, but the active ingredient is capable of being released. It is also possible to use a volatile liquid during polymerization, and to subsequently thermally drive off the volatile liquid, leaving behind a porous polymer bead product into which a variety of active materials can be subsequently adsorbed.
Examples of polyunsaturated monomers suitable for use in accordance with the present invention are ethylene glycol dimethacrylate, triethylene glycol dimethacrylate, tetraethylene glycol dimethacrylate, trimethylol propane ethoxylated triacrylate, ditrimethylol propane dimethacrylate; propylene, dipropylene and higher propylene glycols, 1,3 butylene glycol dimethacrylate, 1,4 butanediol dimethacrylate, 1,6 hexanediol dimethacrylate, neopentyl glycol dimethacrylate, pentaerythritol dimethacrylate, dipentaerythritol dimethacrylate, bisphenol A dimethacrylate, divinyl and trivinyl benzene, divinyl and trivinyl toluene triallyl maleate, triallyl phosphate, diallyl maleate, diallyl itaconate, and allyl methacrylate. The monounsaturated monomers include allyl methacrylates and acrylates having straight or branched chain alkyl groups with 1 to 30 carbon atoms, preferably 5 to 18 carbon atoms. Preferred monomers include lauryl methacrylate, 2-ethylhexyl methacrylate, isodecylmethacrylate, stearyl methacrylate, hydroxy ethyl methacrylate, hydroxy propyl methacrylate, diacetone acrylamide, phenoxy ethyl methacrylate, tetrahydrofurfuryl methacrylate and methoxy ethyl methacrylate.
As noted previously, the copolymer can be formed by copolymerizing one monounsaturated monomer with one polyunsaturated monomer, or with only polyunsaturated monomers.
EXAMPLE IV
Example I was repeated for each of a series of monomer systems shown in Tables IV-XVII. In each instance, submicron sized copolymeric powders were produced employing a stirring speed of about seventy-five RPM. The catalyst was benzoyl peroxide. Adsorption capacities of the various copolymeric powders for fluids were determined and are shown in the Tables, along with the mole ratios of monomers and the solvent. The abbreviations used in Tables IV-XVII are identified as follows:
______________________________________
DAA Diacetone acrylamide
EGDM Ethylene glycol dimethacrylate
TEGDM Tetraethylene glycol dimethacrylate
ST Styrene
DVB Divinylbenzene
VP Vinyl pyrrolidone
IBOMA Isobornyl methacrylate
PEMA Phenoxyethyl methacrylate
IDMA Isodecyl methacrylate
STMA Stearyl methacrylate
HPMA Hydroxypropyl methacrylate
CYMA Cyclohexyl methacrylate
DMAEMA Dimethylaminoethyl methacrylate
TBAEMA t-butyl aminoethyl methacrylate
AMPS 2-acrylamido propane sulfonic acid
BMA Butyl methacrylate
EHMA 2-ethylhexyl methacrylate
MMA Methyl methacrylate
HEMA 2-hydroxyethyl methacrylate
EHO 2-ethylhexyl oxystearate
GG Glucose glutamate
IPA Isopropyl alcohol
PEG Polyethylene glycol 200
______________________________________
TABLE IV
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
GG Water
__________________________________________________________________________
DAA/EGDM 20/80
Xylene
75 82 83 78
DAA/EGDM 30/70
Xylene
77 80 83 78
DAA/EGDM 40/60
Xylene
75 75 83 77
DAA/EGDM 50/50
Xylene
50 57 67 0
DAA/EGDM 60/40
Xylene
40 40 50 0
DAA/TEGDM
20/80
Xylene
40 50 62 58
DAA/TEGDM
30/70
Xylene
29 40 50 55
DAA/TEGDM
40/60
Xylene
25 28 40 43
DAA/TEGDM
50/50
Xylene
25 30 40 43
DAA/TEGDM
60/40
Xylene
22 29 40 40
__________________________________________________________________________
TABLE V
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
PEG
Water
__________________________________________________________________________
ST/TEGDM 20/80
IPA 58 69 69 67
ST/TEGDM 30/70
IPA 58 64 67 69
ST/TEGDM 40/60
IPA 62 71 71 61
ST/TEGDM 50/50
IPA 67 62 54 58
ST/TEGDM 60/40
IPA 50 58 58 54
ST/TEGDM 70/30
IPA 50 58 50 54
ST/TEGDM 80/20
IPA 44 54 50 50
ST/DVB 20/80
IPA 80 75 75 0
ST/DVB 30/70
IPA 75 67 75 0
ST/DVB 40/60
IPA 69 67 67 0
ST/DVB 50/50
IPA 64 72 67 0
ST/DVB 60/40
IPA 67 71 71 0
ST/DVB 70/30
IPA 71 75 76 0
ST/DVB 80/20
IPA 50 50 50 0
__________________________________________________________________________
TABLE VI
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
GG Water
__________________________________________________________________________
VP/EGDM 20/80
Xylene
77 80 74 73.6
VP/EGDM 30/70
Xylene
76 79 78.3
70
VP/EGDM 40/60
Xylene
70 67 75.6
75
VP/EGDM 50/50
Xylene
72 76 80 76
VP/EGDM 60/40
Xylene
74 80 76 77
VP/EGDM 70/30
IPA 71 78 74 75
VP/EGDM 80/20
IPA 67 75 73 74
VP/TEGDM 20/80
Xylene
58 68.8 61.5
67.7
VP/TEGDM 30/70
Xylene
70 67 54.5
68.8
VP/TEGDM 40/60
Xylene
54.5
61.5 52.4
64.3
VP/TEGDM 50/50
Xylene
44.4
47.4 52.4
52.4
VP/TEGDM 60/40
Xylene
50 44.4 50 54.4
VP/TEGDM 70/30
Xylene
50 47.4 44.4
50
VP/TEGDM 80/20
Xylene
54.5
52.4 60 58
__________________________________________________________________________
TABLE VII
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
GG Water
__________________________________________________________________________
IBOMA/EGDM
20/80
IPA 62.9
9.1 71.4
0
IBOMA/EGDM
30/70
IPA 64.3
16.6 67.7
0
IBOMA/EGDM
40/60
IPA 68.7
28.6 61.5
0
IBOMA/EGDM
50/50
IPA 67.7
16.7 58.3
0
IBOMA/EGDM
60/40
IPA 50 23.1 50 0
IBOMA/EGDM
70/30
IPA 50 9.1 47.3
0
IBOMA/EGDM
80/20
IPA 52.3
16.6 44.4
0
IBOMA/TEGDM
20/80
IPA 66.6
62.9 61.5
0
IBOMA/TEGDM
30/70
IPA 61.5
61.5 70.6
0
IBOMA/TEGDM
40/60
IPA 64.3
64.3 71.4
0
IBOMA/TEGDM
50/50
IPA 61.5
66.6 67.7
0
IBOMA/TEGDM
60/40
IPA 58.3
54.5 54.5
0
IBOMA/TEGDM
70/30
IPA 47.3
50 41.1
0
IBOMA/TEGDM
80/20
IPA 37.5
41.1 33.3
0
__________________________________________________________________________
TABLE VIII
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
GG Water
__________________________________________________________________________
PEMA/EGDM 20/80
IPA 64.3
68.7 66.6
61.5
PEMA/EGDM 30/70
IPA 54.5
50 54.5
44.4
PEMA/EGDM 40/60
IPA 52.3
47.3 72.2
9
PEMA/EGDM 50/50
IPA 54.5
33.3 62.9
0
PEMA/EGDM 60/40
IPA 67.7
28.5 70.5
0
PEMA/EGDM 70/30
IPA 69.7
44.4 60.7
0
PEMA/EGDM 80/20
IPA 66.6
68.7 66.6
0
PEMA/TEGDM
20/80
IPA 58.3
56.5 66.6
58.3
PEMA/TEGDM
30/70
IPA 64.2
70.5 67.7
62.9
PEMA/TEGDM
40/60
IPA 66.6
67.7 71.4
69.7
PEMA/TEGDM
50/50
IPA 66.6
70.5 73.6
72.2
PEMA/TEGDM
60/40
IPA 58.3
62.9 52.3
61.5
PEMA/TEGDM
70/30
IPA 50 58.3 52.3
54.5
PEMA/TEGDM
80/20
IPA 67.7
73.6 76.1
47.3
__________________________________________________________________________
TABLE IX
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
PEG
Water
__________________________________________________________________________
IDMA/EGDM 20/80
IPA 55 64 70 0
IDMA/EGDM 30/70
IPA 38 50 44 0
IDMA/EGDM 40/60
IPA 50 67 69 0
IDMA/EGDM 50/50
IPA 58 64 67 0
IDMA/EGDM 60/40
IPA 58 69 69 0
IDMA/TEGDM
20/80
IPA 62 70 70 0
IDMA/TEGDM
30/70
IPA 50 62 62 0
IDMA/TEGDM
40/60
IPA 62 67 67 0
IDMA/TEGDM
50/50
IPA 38 44 50 0
IDMA/TEGDM
60/40
IPA 38 55 50 0
__________________________________________________________________________
TABLE X
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
PEG
Water
__________________________________________________________________________
STMA/EGDM
10/90
IPA 66 64.3 66.7
0
STMA/EGDM
20/80
IPA 69 63 65.5
0
STMA/EGDM
30/70
IPA 73-75
58.3 61.5
0
STMA/EGDM
40/60
IPA 69-71
54.5 58.3
0
STMA/EGDM
50/50
IPA 60-63
52.4 52.4
0
STMA/TEGDM
20/80
IPA 50 47.4 52.4
0
STMA/TEGDM
30/70
IPA 50 64.3 50 0
STMA/TEGDM
40/60
IPA 52.4
61.5 58.3
0
STMA/TEGDM
50/50
IPA 47.4
52.4 56.5
0
__________________________________________________________________________
TABLE XI
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
PEG
Water
__________________________________________________________________________
HPMA/EGDM
20/80
Xylene
64.3
61.5 61.5
9
HPMA/EGDM
30/70
Xylene
54.5
16.7 58.3
0
HPMA/EGDM
40/60
Xylene
54.5
9 58.3
0
HPMA/EGDM
50/50
Xylene
37.5
58.3 50 0
HPMA/EGDM
60/40
Xylene
44.4
61.5 58.3
0
HPMA/EGDM
70/30
Xylene
50 44.4 37.5
0
HPMA/EGDM
80/20
Xylene
61.5
16.7 58.3
0
HPMA/TEGDM
20/80
Xylene
50 58.3 54.5
61.5
HPMA/TEGDM
30/70
Xylene
56.5
54.5 50 60
HPMA/TEGDM
40/60
Xylene
50 58.3 52.4
54.5
HPMA/TEGDM
50/50
Xylene
52.4
61.5 54.5
56.5
HPMA/TEGDM
60/40
Xylene
33.3
47.4 44.4
54.5
HPMA/TEGDM
70/30
Xylene
54.5
44.4 54.5
50
HPMA/TEGDM
80/20
Xylene
50 47.4 41.2
37.5
__________________________________________________________________________
TABLE XII
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
EHO Glycerine
PEG
Water
__________________________________________________________________________
CYMA/EGDM
80/20
IPA 61.5
71.4 66.6
0
CYMA/EGDM
70/30
IPA 60 66 64.2
0
CYMA/EGDM
60/40
IPA 61.5
66 66.6
0
CYMA/EGDM
50/50
IPA 64.2
66 68.7
0
CYMA/EGDM
40/60
IPA 64.2
66 68.7
0
CYMA/EGDM
30/70
IPA 61.5
66 66.6
0
CYMA/EGDM
20/80
IPA 66.6
71.4 75 61.5
CYMA/TEGDM
80/20
IPA 68.7
0 68.7
0
CYMA/TEGDM
70/30
IPA 71.4
0 69.7
0
CYMA/TEGDM
60/40
IPA 66.6
0 62.9
0
CYMA/TEGDM
50/50
IPA 0 0
CYMA/TEGDM
40/60
IPA 60 0 72.9
0
CYMA/TEGDM
30/70
IPA 64.2
0 72.2
0
CYMA/TEGDM
20/80
IPA 61.5
0 66.6
0
__________________________________________________________________________
TABLE XIII
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers Ratio
Solvent
Water
Mineral Oil
Glycerine
EHO
__________________________________________________________________________
DMAEMA/EGDM
20/80
Hexane
0 58.3 66.7 58.3
DMAEMA/EGDM
40/60
Hexane
66.7
61.5 70.6 66.7
DMAEMA/EGDM
60/40
Hexane
77.3
61.5 72.2 76.2
DMAEMA/EGDM
80/20
Hexane
66.7
58.3 68.8 58.3
TBAEMA/EGDM
20/80
Hexane
0 70.6 75 70.6
TBAEMA/EGDM
40/60
Hexane
0 66.7 72.2 66.7
TBAEMA/EGDM
60/40
Hexane
0 61.5 68.75 61.5
TBAEMA/EGDM
80/20
Hexane
0 44.4 54.6 50
TBAEMA/EGDM
80/20
Hexane
54.6
54.6 58.3 50
__________________________________________________________________________
TABLE XIV
__________________________________________________________________________
Mole Adsorption Capacity %
Monomers
Ratio
Solvent
Water
Mineral Oil
Glycerine
EHO
__________________________________________________________________________
AMPS/EGDM
20/80
Xylene
84.3
83.3 85.3 83.3
BMA/EGDM
20/80
Hexane
0 70.6 75 68.8
BMA/EGDM
40/60
Hexane
0 70.6 77.3 70.6
BMA/EGDM
40/60
Ethyl-
0 66.7 73.7 68.8
Alcohol
BMA/EGDM
60/40
Hexane
0 72.2 0 73.7
BMA/EGDM
80/20
Hexane
0 54.5 66.7 58.3
________________ 
