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WO1998014405A1 - Dispersions aqueuses - Google Patents

Dispersions aqueuses Download PDF

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Publication number
WO1998014405A1
WO1998014405A1 PCT/US1997/016647 US9716647W WO9814405A1 WO 1998014405 A1 WO1998014405 A1 WO 1998014405A1 US 9716647 W US9716647 W US 9716647W WO 9814405 A1 WO9814405 A1 WO 9814405A1
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WO
WIPO (PCT)
Prior art keywords
polymer
water
soluble
comprised
aqueous dispersion
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US1997/016647
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English (en)
Inventor
Sun-Yi Huang
Louis Rosati
Joseph J. Kozakiewicz
Michael W. Coville
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Cytec Technology Corp
Original Assignee
Cytec Technology Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US08/725,521 external-priority patent/US5919854A/en
Priority claimed from US08/725,865 external-priority patent/US5792366A/en
Priority claimed from US08/724,970 external-priority patent/US5843320A/en
Priority claimed from US08/720,840 external-priority patent/US6664326B1/en
Priority claimed from US08/723,656 external-priority patent/US5696228A/en
Priority claimed from US08/720,851 external-priority patent/US6608124B1/en
Priority claimed from US08/727,693 external-priority patent/US6702946B1/en
Priority to CA002264803A priority Critical patent/CA2264803A1/fr
Priority to JP51659298A priority patent/JP2001506674A/ja
Application filed by Cytec Technology Corp filed Critical Cytec Technology Corp
Priority to IL12919697A priority patent/IL129196A0/xx
Priority to EP97942590A priority patent/EP0952964A1/fr
Priority to AU44259/97A priority patent/AU732835B2/en
Publication of WO1998014405A1 publication Critical patent/WO1998014405A1/fr
Priority to MX9902862A priority patent/MX206802B/es
Priority to NO991540A priority patent/NO991540L/no
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F220/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride ester, amide, imide or nitrile thereof
    • C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
    • C08F220/10—Esters
    • C08F220/34—Esters containing nitrogen, e.g. N,N-dimethylaminoethyl (meth)acrylate
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2/00—Processes of polymerisation
    • C08F2/44—Polymerisation in the presence of compounding ingredients, e.g. plasticisers, dyestuffs, fillers
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F220/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride ester, amide, imide or nitrile thereof
    • C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
    • C08F220/10—Esters
    • C08F220/34—Esters containing nitrogen, e.g. N,N-dimethylaminoethyl (meth)acrylate
    • C08F220/36—Esters containing nitrogen, e.g. N,N-dimethylaminoethyl (meth)acrylate containing oxygen in addition to the carboxy oxygen, e.g. 2-N-morpholinoethyl (meth)acrylate or 2-isocyanatoethyl (meth)acrylate
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F220/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride ester, amide, imide or nitrile thereof
    • C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
    • C08F220/52—Amides or imides
    • C08F220/54—Amides, e.g. N,N-dimethylacrylamide or N-isopropylacrylamide
    • C08F220/60—Amides, e.g. N,N-dimethylacrylamide or N-isopropylacrylamide containing nitrogen in addition to the carbonamido nitrogen
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F220/00—Copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and only one being terminated by only one carboxyl radical or a salt, anhydride ester, amide, imide or nitrile thereof
    • C08F220/02—Monocarboxylic acids having less than ten carbon atoms; Derivatives thereof
    • C08F220/52—Amides or imides
    • C08F220/54—Amides, e.g. N,N-dimethylacrylamide or N-isopropylacrylamide
    • C08F220/60—Amides, e.g. N,N-dimethylacrylamide or N-isopropylacrylamide containing nitrogen in addition to the carbonamido nitrogen
    • C08F220/603—Amides, e.g. N,N-dimethylacrylamide or N-isopropylacrylamide containing nitrogen in addition to the carbonamido nitrogen and containing oxygen in addition to the carbonamido oxygen and nitrogen
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F291/00—Macromolecular compounds obtained by polymerising monomers on to macromolecular compounds according to more than one of the groups C08F251/00 - C08F289/00

Definitions

  • This invention relates to aqueous dispersions comprised of water-soluble polymers, processes for making said dispersions, and methods of using said dispersions in water treating, dewatering, water clarification, papermaking, oil field, soil conditioning, food processing, mineral processing, and biotechnological applications.
  • U.S. Patent No. 4,380,600 discloses a process for producing an aqueous dispersion of water-soluble polymers.
  • the aqueous dispersion may contain inorganic salt.
  • the aqueous dispersions exemplified therein have disadvantageously high bulk viscosities.
  • U.S. Patent No. 4,673,704 and EP 0 170 394 A2 disclose products comprised of particles above 20 microns in size of a high molecular weight polymer gel interconnected by a continuous phase that is an aqueous solution of an equilibrating agent that holds the water content of the particles in equilibrium with the water content of the aqueous phase and that prevents substantial agglomeration of the particles in the fluid product.
  • these references are entitled “Aqueous Polymer Dispersions”
  • the products disclosed therein are distinguished from the aqueous dispersions of U.S. Patent No. 4,380,600 and from the aqueous dispersions of the instant invention in that the particles of U.S.
  • 4,673,704 and EP 0 170 394 A2 are not generally held suspended in a continuous matrix of the aqueous phase but instead generally rest substantially in contact with one another but slide over one another.
  • a process for dispersing the polymer gel into an aqueous solution of an equilibrating agent and working the polymer while in that medium is disclosed in U.S. Patent No. 4,778,836 and EP 0 169 674 B1.
  • U.S. Patent No. 4,522,968 discloses a process for dispersing certain powdered water-soluble homopolymers or copolymers in an aqueous solution containing a polymer of ethylene oxide and/or propylene oxide.
  • U.S. Patent Nos. 4,929,655 and 5,006,590 disclose processes for preparing aqueous dispersions of water-soluble polymers by polymerizing benzyl-containing monomers in the presence of an organic high molecular multivalent cation and a multivalent anionic salt.
  • the benzyl group-containing monomer may be replaced by a hydrophobic alkyl group-containing monomer as in EP 0 525 751. Numerous references concern these and similar polymers, e.g. U.S.
  • aqueous dispersions in these references have relatively low bulk viscosities
  • the need to include special monomers containing aromatic or hydrophobic alkyl groups in order to render the polymer insoluble in salt solution may be disadvantageous because the special monomers may be expensive and dilutive of the polymer effect in a specific application.
  • Kosmotropic salts generally decrease the solubility of substances in water.
  • the Hofmeister ranking apparently guided the choice of salts for precipitating cationic water soluble polymers, containing hydrophobic groups, in U. S. Patent Nos. 4, 929,655 and 5,006,590, as well as EP 0 630 909 A1 , EP 0 525 751 A1 , and EP 0 657 478 A2, as evidenced by their use of strongly kosmotropic salts containing sulfate and phosphate anions.
  • chaotropic salts generally increase the solubility of substances in water.
  • salts which contain anions such as sulfate, fluoride, phosphate, acetate, citrate, tartrate and hydrogenphosphate are kosmotropic.
  • Representative salts which contain anions such as thiocyanate, perchlorate, chlorate, bromate, iodide, nitrate and bromide are chaotropic.
  • the chloride anion is generally considered to be at about the middle of the Hofmeister ranking, being either weakly chaotropic or weakly kosmotropic, depending on the particular system.
  • inorganic salts which contain the chloride anion tend to be kosmotropic.
  • ionene polymers Certain novel cationic polyelectrolytes, termed ionene polymers, were reported (D. Casson and A. Rembauim, Macromolecules, Vol. 5, No. 1 , 1972, pp. 75-81) to be insoluble in either 0.4 M potassium iodide or 0.4 M potassium thiocyanate. It has also been reported (W-F. Lee and C-C. Tsai, J. Appl. Polym. Sci., Vol. 52, pp. 1447-1458, 1994) that poly(trimethyl acrylamido propyl ammonium iodide) did not dissolve in 0.5 M Na 2 CI0 4 or 0.5 M NaNO 3 .
  • compositions comprising sulphonated hydrocarbon surfactants and hydrophilic cationic polymers were disclosed in U.S. Patent No. 5,130,358. Mixtures of chaotropic salts, or anionic organic salts, and kosmotropic salts may be used to precipitate cationic polymers as in U.S. Application Serial No. (attorney docket No. 96052), filed even date herewith.
  • Aqueous dispersions of water-soluble polymers are disclosed in U.S. 5,403,883; 5,480,934; 5,541 ,252; EP 0 624 617 A1 ; EP 0 573 793 A1 ; and WO 95/11269.
  • a problem remains in that the aqueous dispersions exemplified in these references still have relatively high bulk viscosities.
  • a process for preparing crosslinked copolymer beads from water-soluble monomers in an aqueous solution containing an inorganic salt and a dispersant is disclosed in U.S. 5,498,678 and EP 0 604 109 A2.
  • an aqueous dispersion of polymers which comprises: (a) a first cationic water- soluble or water-swellable polymer; and (b) at least one second water-soluble polymer different from said first polymer; and (c) a kosmotropic salt; and (d) a chaotropic salt, wherein the amounts of said (b), (c) and (d) are such that a homogeneous composition is obtained in the absence of said (b).
  • an aqueous dispersion of polymers which comprises: (a) a first cationic water-soluble or water-swellable polymer; and (b) at least one second water-soluble polymer different from said first polymer; and (c) a kosmotropic salt; and (d) an anionic organic salt, wherein the amounts of said (b), (c) and (d) are such that a homogeneous composition is obtained in the absence of said
  • an aqueous dispersion of polymers which is comprised of (a) a discontinuous phase containing polymer that is comprised predominately of a first cationic water-soluble or water-swellable polymer having at least one recurring unit of the formula (I), (I)
  • R. is H or CH 3 , A is O or NH, B is an alkylene or branched alkylene or oxyalkylene group having from 1 to 5 carbons, R 2 is a methyl, ethyl, or propyl group, R 3 is a methyl, ethyl, or propyl group, R 4 is a methyl, ethyl or propyl group, X is a counterion, and R 2 , R 3 , and R 4 together contain a total of at least 4 carbon atoms; and (b) at least one second water-soluble polymer different from said first polymer.
  • an aqueous dispersion of polymers which comprises: (a) a first cationic water-soluble or water-swellable polymer having at least one recurring unit of the formula (I), wherein R- is H or CH 3 , A is O or NH, B is an alkylene or branched alkylene or oxyalkylene group having from 1 to 5 carbons, R 2 is a methyl, ethyl, or propyl group, R 3 is a methyl, ethyl, or propyl group, R 4 is an alkyl or substituted alkyl group having from 1 to 10 carbons, or an aryl or substituted aryl group having from 6 to 10 carbons, X is a counterion, and R 2 , R 3 , and R 4 together contain a total of at least 4 carbon atoms; and (b) at least one second water-soluble polymer different from said first polymer, wherein a homogeneous composition is obtained in the absence of said (b).
  • R- is
  • a process for making an aqueous dispersion of polymers comprises polymerizing vinyl-addition monomers to form an aqueous dispersion comprised of a first cationic water-soluble or water-swellable polymer, wherein said polymerizing is carried out in the presence of an aqueous composition comprised of
  • a process for making an aqueous dispersion of polymers comprises polymerizing vinyl-addition monomers to form an aqueous dispersion comprised of a first cationic water-soluble or water-swellable polymer, wherein said polymerizing is carried out in the presence of an aqueous composition comprised of (a) at least one second water-soluble polymer different from said first polymer; (b) a kosmotropic salt; and (c) of an anionic organic salt, wherein the amounts of said (a), (b) and (c) are such that a homogeneous composition is obtained if said polymerizing is carried out in the absence of said (a).
  • a process for making an aqueous dispersion of polymers comprises polymerizing vinyl-addition monomers comprised of at least one monomer of the formula (II) to form an aqueous dispersion comprised of a first cationic water-soluble or water-swellable polymer,
  • R. is H or CH 3 , A is O or NH, B is an alkylene or branched alkylene or oxyalkylene group having from 1 to 5 carbons, R 2 is a methyl, ethyl, or propyl group, R 3 is a methyl, ethyl, or propyl group, R 4 is a methyl, ethyl or propyl group, X is a counterion, and R 2 , R 3 , and R 4 together contain a total of at least 4 carbon atoms; and wherein said polymerizing is carried out in the presence of an aqueous composition comprised of at least one second water-soluble polymer different from said first polymer.
  • a process for making an aqueous dispersion of polymers comprises polymerizing vinyl-addition monomers comprised of at least one monomer of the formula (II) to form an aqueous dispersion comprised of a first water- soluble or water-swellable cationic polymer, wherein R.
  • A is O or NH
  • B is an alkylene or branched alkylene or oxyalkylene group having from 1 to 5 carbons
  • R 2 is a methyl, ethyl, or propyl group
  • R 3 is a methyl, ethyl, or propyl group
  • R 4 is an alkyl or substituted alkyl group having from 1 to 10 carbons, or an aryl or substituted aryl group having from 6 to 10 carbons
  • X is a counterion
  • R 2 , R 3 , and R 4 together contain a total of at least 4 carbon atoms; and wherein said polymerizing is carried out in the presence of an aqueous composition comprised of an amount of at least one second water-soluble polymer different from said first polymer; and wherein said amount of said second polymer is such that a homogeneous composition is obtained if said polymerizing is carried out in the absence of said second polymer.
  • a process for blending two or more aqueous dispersions comprising intermixing (a) a first aqueous dispersion of a water-soluble or water-swellable polymer with (b) a second aqueous dispersion of a water-soluble or water- swellable polymer, wherein said (a) is different from said (b), to form a third aqueous dispersion.
  • a method of dewatering a suspension of dispersed solids which (a) intermixing an aqueous dispersion of polymers, or aqueous admixture thereof, in an amount effective for dewatering, with a suspension of dispersed solids, and (b) dewatering said suspension of dispersed solids, said aqueous dispersion being comprised of (i) a first cationic water-soluble or water-swellable polymer; and (ii) at least one second water-soluble polymer different from said first polymer; and (iii) a kosmotropic salt; and (iv) a chaotropic salt, wherein the amounts of said (ii), (iii) and (iv) are such that a homogeneous composition is obtained in the absence of said (ii).
  • a method of dewatering a suspension of dispersed solids comprises (a) intermixing an aqueous dispersion of polymers, or aqueous admixture thereof, in an amount effective for dewatering, with a suspension of dispersed solids, and (b) dewatering said suspension of dispersed solids, said aqueous dispersion being comprised of (i) a first cationic water-soluble or water-swellable polymer; and (ii) at least one second water-soluble polymer different from said first polymer; and (iii) a kosmotropic salt; and (iv) an anionic organic salt, wherein the amounts of said (ii), (iii) and
  • a method of dewatering a suspension of dispersed solids which comprises (a) intermixing an aqueous dispersion of polymers, or aqueous admixture thereof, in an amount effective for dewatering, with a suspension of dispersed solids, and (b) dewatering said suspension of dispersed solids, said aqueous dispersion being comprised of (i) a discontinuous phase containing polymer that is comprised predominately of a first cationic water-soluble or water-swellable polymer having at least one recurring unit of the formula (I), wherein R ⁇ is H or CH 3 , A is O or NH, B is an alkylene or branched alkylene or oxyalkylene group having from 1 to 5 carbons, R 2 is a methyl, ethyl, or propyl group, R 3 is a methyl, ethyl, or propyl group, R 4 is a methyl, ethyl or propyl
  • X is a counterion, and R 2 , R 3 , and R 4 together contain a total of at least 4 carbon atoms; and (ii) at least one second water-soluble polymer different from said first polymer.
  • a method of dewatering a suspension of dispersed solids which comprises (a) intermixing an aqueous dispersion of polymers, or aqueous admixture thereof, in an amount effective for dewatering, with a suspension of dispersed solids, and (b) dewatering said suspension of dispersed solids, said aqueous dispersion being comprised of (i) a first cationic water-soluble or water-swellable polymer having at least one recurring unit of the formula (I), wherein R ⁇ is H or CH 3 , A is O or NH, B is an alkylene or branched alkylene or oxyalkylene group having from 1 to 5 carbons, R 2 is a methyl, ethyl, or propyl group, R 3 is a methyl, ethyl, or propyl group, R 4 is an alkyl or substituted alkyl group having from 1 to 10 carbons, or an aryl or substituted aryl group having
  • a process for producing substantially dry water-soluble or water-swellable vinyl-addition polymer particles comprises (a) spray-drying a vinyl-addition polymer-containing aqueous dispersion into a gas stream with a residence time of about 8 to about 120 seconds and at an outlet temperature of about 70° C to about 150° C and (b) collecting resultant polymer particles.
  • substantially dry water-soluble or water-swellable polymer particles are provided which are comprised of (a) a first cationic water-soluble or water- swellable polymer; and (b) at least one second water-soluble polymer different from said first polymer; and (c) a kosmotropic salt; and (d) a chaotropic salt, wherein about 90% or more of said polymer particles each individually contains both said (a) and said (b), said particles having a bulk density of about 0.4 grams per cubic centimeter to about 1.0 grams per cubic centimeter.
  • a method comprising (a) intermixing a composition comprising substantially dry water-soluble or water-swellable polymer particles comprised of (i) a first cationic water-soluble or water-swellable polymer; and (ii) at least one second water-soluble polymer different from said first polymer; and (iii) a kosmotropic salt; and (iv) a chaotropic salt, wherein about 90% or more of said polymer particles each individually contains both said (i) and said (ii), said particles having a bulk density of about 0.4 grams per cubic centimeter to about 1.0 grams per cubic centimeter, with water to form an aqueous polymer admixture, (b) intermixing said aqueous polymer admixture, in an amount effective for dewatering, with a suspension of dispersed solids, and (c) dewatering said suspension of dispersed solids.
  • a method comprising (a) intermixing a composition comprising substantially dry water-soluble or water-swellable polymer particles comprised of (i) a first cationic water-soluble or water-swellable polymer; and (ii) at least one second water-soluble polymer different from said first polymer; and (iii) a kosmotropic salt; and (iv) an anionic organic salt, wherein about 90% or more of said polymer particles each individually contains both said (i) and said (ii), said particles having a bulk density of about 0.4 grams per cubic centimeter to about 1.0 grams per cubic centimeter, with water to form an aqueous polymer admixture, (b) intermixing said aqueous polymer admixture, in an amount effective for dewatering, with a suspension of dispersed solids, and (c) dewatering said suspension of dispersed solids.
  • a method comprising (a) intermixing a composition comprising substantially dry water-soluble or water-swellable polymer particles comprised of (i) a first cationic water-soluble or water-swellable polymer having at least one recurring unit of the formula (I), wherein R.
  • R 2 , R 3 , and R 4 together contain a total of at least 4 carbon atoms; and (ii) at least one second water-soluble polymer different from said first polymer, wherein about 90% or more of said polymer particles each individually contains both said (i) and said (ii), said particles having a bulk density of about 0.4 grams per cubic centimeter to about 1.0 grams per cubic centimeter, with water to form an aqueous polymer admixture, (b) intermixing
  • the aqueous dispersions of the instant invention contain a first cationic water- soluble or water-swellable polymer, preferably a vinyl-addition polymer.
  • the cationic charge of said first cationic polymer may vary over a broad range by containing from about 1% to about 100% cationic recurring units, preferably about 5% or greater, more preferably about 10% or greater, even more preferably about 20% or greater, most preferably about 30% or greater, preferably about 90% or less, more preferably about 80% or less, most preferably about 70% or less, by mole based on total moles of recurring units in said first cationic polymer.
  • Cationic recurring units may be formed by post-reaction of polymer, but are preferably formed by polymerization of cationic monomers.
  • Cationic monomers may include any cationic monomer, including diallyldialkylammonium halide, cationic (meth)acrylates, and cationic (meth)acrylamides commonly used in preparing water-soluble polymers, preferably diallyldimethylammonium halide, as well as acid and quaternary salts of dialkylaminoalkyl(alk)acrylate and dialkylaminoalkyl(alk)acrylamide.
  • Cationic recurring units may be formed by the polymerization of quatemizable monomers such as dialkylaminoalkyl(alk)acrylate or dialkylaminoalkyl(alk)acrylamide, followed by acidification or quaternization.
  • the first cationic polymer contains cationic recurring units of the formula (I), preferably formed by polymerization of the corresponding monomers of the formula (II):
  • ⁇ is H or CH 3 , A is O or NH, B is alkylene or branched alkylene or oxyalkylene having from 1 to 5 carbons, R 2 and R 3 are each individually methyl, ethyl, or propyl, R 4 is an alkyl or substituted alkyl group having from 1 to 10 carbon atoms, or an aryl or substituted aryl group having from 6 to 10 carbon atoms, X is a counterion, and R 2 , R 3 and R 4 together contain at least a total of 4 carbon atoms, preferably at least 5 carbon atoms. In certain preferred embodiments, R 4 is a methyl, ethyl or propyl group.
  • R 4 is an alkyl or substituted alkyl group having from 4 to 10 carbon atoms. In other preferred embodiments, R 4 is benzyl.
  • X is chloride, bromide, iodide, methylsulfate, or ethylsulfate.
  • the first cationic water-soluble or water-swellable polymer may be a copolymer and may contain other cationic recurring units or nonionic recurring units.
  • Nonionic recurring units may be formed from water-soluble monomers such as N-vinylpyridine, N- vinylpyrrolidone, hydroxyalkyl(meth)acrylates, etc., preferably (meth)acrylamide, or may be formed from hydrophobic monomers having low water-solubility, so long as the inclusion of the poorly water-soluble, e.g. hydrophobic, recurring units does not render the resulting polymer water-insoluble or water-nonswellable.
  • the first cationic polymer may contain amounts of recurring units of water-soluble non-ionic monomers ranging from 0% to about 99%, preferably about 10% or greater, more preferably about 20% or greater, most preferably about 30% or greater; preferably about 90% or less, more preferably about 80% or less, most preferably about 70% or less, by mole based on total moles of recurring units in said polymer.
  • the hydrophobic monomers may be hydrocarbon monomers e.g.
  • styrene butadiene, 1-alkene, vinyl cyclohexane, etc.
  • vinyl monomers such as vinyl halide, other primarily aliphatic or aromatic compounds with polymerizable double bonds, or monomers with only moderate water-solubility such as acrylonitrile.
  • the hydrophobic monomers are alkyl (alk)acrylates or aryl (alk)acrylates in which the alkyl or aryl groups contain about 1 -12 carbon atoms, such as methyl (meth)acrylate, ethyl (meth)acrylate, propyl (meth)acrylate, butyl (meth)ac ylate, hexyl (meth)acrylate, ethylhexyl (meth)acrylate, isoalkyl (meth)acrylate, cyclohexyl (meth)acrylate, or aromatic (meth)acrylate, or alkyl or aryl (alk)acrylamides in which the alkyl or aryl groups contain about 1 -12 carbon atoms, such as methyl (meth)acrylamide, ethyl (meth)acrylamide, t-butyl
  • the first cationic water-soluble or water-swellable polymer may contain amounts of hydrophobic non-ionic recurring units ranging from 0% to about 15%, preferably about 2% to about 10%, by mole based on total moles of recurring units in said polymer.
  • hydrophobic recurring units may be dilutive of the polymer effect in certain applications, inclusion in controlled amounts may advantageously affect a particular characteristic of the aqueous dispersion, e.g. solubility rate, bulk viscosity, cost, ease of processing, performance, etc.
  • a particular characteristic of the aqueous dispersion e.g. solubility rate, bulk viscosity, cost, ease of processing, performance, etc.
  • the amount of the first cationic water-soluble or water-swellable polymer in the aqueous dispersion is as high as practicable, taking into account the effect of high solids on bulk viscosity, preferably about 5% or greater, more preferably about 10% or greater, most preferably about 20% or greater, by weight based on the total weight of the aqueous dispersion. Generally, the solids are not increased above an amount which increases the bulk viscosity to an impractical level. Practically, the amount of first cationic polymer in the aqueous dispersion is about 75% or less, preferably about 60% or less, more preferably about 50% or less, by weight based on total weight.
  • the weight average molecular weight of the first cationic polymer in the aqueous dispersion is not critical and depends on the application, but is generally higher than about 1 ,000,000, preferably greater than about 2,000,000, more preferably greater than about 5,000,000, and most preferably greater than about 10,000,000.
  • Molecular weights of polymers are weight average and may be determined by means known to those skilled in the art, preferably by light scattering.
  • the aqueous dispersions of the instant invention are generally comprised of a discontinuous phase of small aqueous droplets, containing polymer that is comprised predominately of the first cationic water-soluble or water-swellable polymer, that are dispersed in the aqueous continuous phase, although of course minor amounts of said first polymer may be found in the continuous phase.
  • the first cationic water-soluble or water-swellable polymer generally constitutes more than 50%, preferably more than 75%, of the polymer in a typical small aqueous droplet.
  • the amount of first cationic polymer in the discontinuous and continuous phases may be determined by known analytical techniques e.g. Raman microscopy.
  • aqueous dispersions of the instant invention are preferred because it is generally more desirable for the first cationic polymer to be in the form of small droplets which are generally held suspended in a continuous matrix of the aqueous phase and do not generally rest substantially in contact with one another.
  • aqueous dispersions prepared by polymerization of monomers as herein described may sometimes have an average droplet size of about 30 microns or more, the average droplet size is generally less than about 30 microns, preferably less than 20 microns, more preferably about 15 microns or less.
  • Droplet size of a non-spherical droplet is the length along a major axis. Droplet size and shape tend to be a function of reactor conditions such as stirring rate, reactor configuration, type of stirrer, etc.
  • the size of the droplets is chosen by carrying out the polymerization in the presence of one or more insoluble polymeric seeds, said polymeric seeds being insoluble in an aqueous solution having the same inorganic salt concentration as said aqueous dispersion.
  • the aqueous dispersions of the instant invention contain a second water-soluble polymer, preferably a vinyl-addition polymer, that is different from and, preferably, incompatible with, said first water-soluble or water-swellable cationic polymer.
  • the second polymer is different from the first polymer when it can be distinguished from the first polymer on the basis of a particular physical characteristic e.g. chemical composition, charge, molecular weight, molecular weight distribution, distribution of recurring units along the polymer chain, etc., by known characterization methods e.g. spectroscopy, chromatography, etc.
  • the second polymer is incompatible with the first polymer when solutions of the two polymers, at the concentrations present in the aqueous dispersion, do not form a homogenous mixture when blended, or do not form a homogenous mixture when one polymer is formed by polymerization of monomers in the presence of the other polymer.
  • the second, preferably cationic, water-soluble polymer in the aqueous dispersion of the instant invention is generally dissolved in the aqueous continuous phase, although of course minor amounts may be found in the discontinuous phase.
  • the amount of second polymer in the discontinuous and continuous phases may be determined by known analytical techniques e.g. Raman microscopy.
  • the second polymer may be any nonionic water-soluble polymer, preferably a polyalkyleneoxide, a polyvinylalcohol, polyvinylpyridine, polyvinylpyrollidone, polyhydroxylalkyl(alk)acrylate, etc., most preferably poly(meth)acrylamide. Even more preferably, the second water-soluble polymer is cationic.
  • the second polymer may be any cationic polymer, and the charge may vary over a broad range by containing about 1 % to about 100% cationic recurring units, preferably about 10% or greater, more preferably about 20% or greater, even more preferably about 30% or greater, by mole based on total moles of recurring units in the polymer.
  • the second cationic polymer may contain about 70% or less, or even about 50% or less, of cationic recurring units, preferably the second polymer is predominately cationic i.e. contains more than 50% cationic recurring units, by mole based on total moles of recurring units in the polymer; most preferably about 80% or greater of recurring cationic units, same basis.
  • Cationic recurring units may be formed by polymerization of cationic monomers or by post-reaction of polymer as above, and may be a copolymer and may contain other cationic recurring units or nonionic recurring units as above.
  • Preferred second cationic water-soluble polymers contain recurring units of diallyldialkylammonium halide, methyl chloride quaternary salt of dialkylaminoalkyl(alk)acrylate, dimethyl sulfate quaternary salt of d i al ky lam i noal ky l (al k) ac rylate , m ethy l ch l o ride quaternary salt of dialkylaminoalkyl(alk)acrylamide, or dimethyl sulfate quaternary salt of dialkylaminoalkyl(alk)acrylamide.
  • second cationic water-soluble polymers contain recurring units of diallyldimethylammonium chloride, methyl chloride quaternary salt of dimethylaminoethyl(meth)acrylate, or dimethyl sulfate quaternary salt of dimethylaminoethyl(meth)acrylate.
  • One or more second cationic polymers may be used.
  • the second polymer may be cationic in order to maximize the cationic charge density of the aqueous dispersion. Also, for embodiments which contain salt, it may be preferable for the second polymer to be cationic because cationic polymers are often more soluble in salt solution than nonionic polymers.
  • the amount of the second, preferably cationic, water-soluble polymer in the aqueous dispersion is generally chosen to control aqueous dispersion properties e.g. performance, bulk viscosity, charge, molecular weight, solubility rate, physical stability, e.g. settling, etc.
  • the amount of said second polymer is about 5% or greater, preferably about 10% or greater, more preferably about 20% or greater, most preferably about 30% or greater, by weight based on the amount of first cationic water-soluble polymer.
  • the amount of second water-soluble polymer in the aqueous dispersion is 100% or less, preferably about 80% or less, more preferably about 50% or less, by weight based on the amount of first cationic water-soluble polymer.
  • the amounts of the first and second polymers are effective to form an aqueous dispersion.
  • an aqueous dispersion is not formed in the absence of the second polymer, and a homogeneous composition is obtained instead.
  • the amount of first and second polymer may be found by routine experimentation, and different amounts will ordinarily be used depending on the identity of the first and second polymers, the total polymer solids level, the bulk viscosity, cost, ease of production, product performance, etc.
  • the weight average molecular weight of the second water-soluble polymer in the aqueous dispersion is also generally chosen to provide the most advantageous effect, e.g. bulk viscosity, performance, cost, etc., but is generally higher than about 10,000, preferably greater than about 50,000, more preferably greater than about 500,000, and most preferably greater than about 1 ,000,000. Molecular weights of polymers are weight average and may be determined by means known to those skilled in the art, preferably by light scattering.
  • the second water-soluble polymer is primarily in the continuous phase of the aqueous dispersion, although of course minor amounts may be contained in the dispersed droplets.
  • the aqueous dispersions of the instant invention are heterogeneous compositions in which more than 50%, preferably about 75% or more, of the first cationic water-soluble or water-swellable polymer is in the form of a discontinuous phase of aqueous droplets that are dispersed in an aqueous solution that is comprised of more than 50%, preferably about 75% or more, of the second, preferably cationic, water-soluble polymer.
  • the aqueous dispersions of the instant invention may contain a third water-soluble or water-swellable polymer that is different from the first or second polymers.
  • the third polymer may also be contained in droplets dispersed in the aqueous solution, in which case it may be described as discussed above for the first cationic polymer.
  • the third polymer may also be dissolved in the aqueous solution along with the second polymer, in which case it may be described as discussed above for the second polymer.
  • the third polymer is cationic.
  • a third aqueous dispersion, containing three or more polymers, may be formed by blending first and second aqueous dispersions of the instant invention, wherein the first and second aqueous dispersions are different from each other. Blending is generally carried out by intermixing the aqueous dispersions, typically with stirring. Blending may be advantageous to achieve a balance of properties exhibited by the individual aqueous dispersions, e.g. performance, charge, total polymer solids, cost, molecular weight, etc. Surprisingly, in many cases the blends are stable, e.g. remain in the form of aqueous dispersions having low bulk viscosity e.g.
  • the bulk viscosity of the blend is often lower than the bulk viscosity of any of the individual aqueous dispersions.
  • the molecular weight of the aqueous dispersion is simply the weight average molecular weight of the polymers contained therein, obtained by subjecting the entire dispersion to a suitable molecular weight characterization technique e.g. light scattering. Since the aqueous dispersion contains two or more different polymers, each of which may have a molecular weight and molecular weight distribution different from the other(s), the molecular weight distribution of the aqueous dispersion may be multimodal.
  • the molecular weight of the aqueous dispersion is generally about 1 ,000,000 or greater, preferably greater than 2,000,000, more preferably about 3,000,000 or greater, most preferably about 5,000,000 or greater.
  • standard viscosity is determined by: diluting an aqueous dispersion with water to form an aqueous admixture (in the case of water-swellable polymers) or solution (in the case of water-soluble polymers) having a polymer concentration of about 0.2%; mixing together 8.0 g of this aqueous admixture or solution with 8.6 g of 2M NaCl; and then measuring the viscosity of the resultant mixture at 25°C on a rotating cylinder viscometer e.g. Brookfield Viscometer equipped with a UL adapter at 60 rpm.
  • a rotating cylinder viscometer e.g. Brookfield Viscometer equipped with a UL adapter at 60 rpm.
  • the standard viscosities of the aqueous dispersions of the instant invention are generally about 1.5 centipoise or greater, preferably about 1.8 centipoise or greater, more preferably about 2.0 centipoise or greater, most preferably about 2.5 centipoise or greater, depending on the application.
  • aqueous dispersions of the instant invention may also be intermixed with water-in-oil emulsions or microemuisions of water-soluble polymers to form compositions which, though they contain oil, contain proportionately less oil than the water-in-oil emulsions or microemuisions from which they are derived. Consequently, these compositions may advantageously produce less secondary pollution, have lower flammability, etc.
  • the salt may be any inorganic salt, preferably a kosmotropic salt e.g. a chloride, sulfate, phosphate, or hydrogenphosphate salt, more preferably ammonium sulfate, sodium chloride, and sodium sulfate, most preferably sodium sulfate and ammonium sulfate.
  • the counterion may be any counterion, e.g. Group IA and Group II metal ions, ammonium, etc., preferably ammonium, sodium, potassium and magnesium.
  • salts may be used, and the amount of salt may be chosen to achieve a desirable bulk viscosity or any other desirable effect. Since the salt may have a dilutive effect, in certain preferred embodiments the salt is only added in amounts so as to achieve a homogeneous composition in the absence of the second water- soluble polymer. In these embodiments, the aqueous dispersion is not formed by the action of the salt, but by the interaction of the first and second polymers. Effective or viscosity- reducing amounts of salt may be found through routine experimentation and are generally chosen to reduce the bulk viscosity without causing precipitation of the polymer.
  • the salt is only added in amounts so as to achieve a homogeneous composition in the absence of the first cationic polymer.
  • salt levels may range upwards from 0%, preferably about 3% or greater, most preferably about 5% or greater, by weight based on total weight, depending on the upper limit to solubility, because solubility of the salt in the aqueous dispersion is preferred.
  • salt levels are chosen to favorably influence product attributes such as cost, bulk viscosity, etc.
  • salt levels may be determined by routine experimentation, e.g. balancing the tendency for positive product attributes e.g. lower bulk viscosities resulting from higher salt levels, against the negative aspects of salt use e.g. cost and dilutive effect.
  • chaotropic salts with kosmotropic salts, or anionic organic salts with kosmotropic salts, have a tendency to reduce the bulk viscosity of the aqueous dispersion.
  • the salt mixture is more effective than either salt alone, on a weight basis.
  • Useful chaotropic salts include thiocyanates, perchlorates, chlorates, nitrates, bromides, iodides, and mixtures thereof, preferably sodium thiocyanate and sodium iodide.
  • anionic organic salts include anionic surfactants and anionic hydrotropic salts, preferably aryl and substituted aryl sulfonates having from 6 to 22 carbons, preferably 6 to 18 carbons, and alkyl and substituted alkyl sulfonates having from 2 to 22 carbons, preferably 4 to 18 carbons, and mixtures thereof.
  • Especially preferred anionic organic salts are dialkylsulfosuccinates, diarylsulfosuccinates, benzenesulfonates, benzenedisulfonates, naphthalensulfonates, naphthalenedisulfonates, and mixtures thereof; 1 ,3-benzendisulfonates are most preferred.
  • Counterions to the chaotropic and anionic organic salts may be any typical counterion, e.g. Group IA metal ions, ammonium, etc., preferably ammonium, sodium, and potassium. Effective or viscosity-reducing amounts of chaotropic and anionic organic salts may be found through routine experimentation and are generally chosen to reduce the bulk viscosity without causing precipitation of the polymer.
  • the amounts of chaotropic salt, or anionic organic salt, and kosmotropic salt are chosen such that a homogeneous composition is obtained in the absence of the second cationic polymer; i.e. the concentration of the salts is such that the first cationic polymer is not precipitated in the absence of the second cationic polymer.
  • amounts of chaotropic, or anionic organic, salts are about 10% or less, preferably about 5% or less, and generally 0.5% or more, preferably 1 % or more, by weight based on total weight. At very low chaotropic or anionic organic salt levels, the viscosity-reducing effect of the salt is negligible, whereas the salt may cause undesirable precipitation or layering at high levels of incorporation.
  • amounts of kosmotropic salts used with the chaotropic, or anionic organic salt are generally less than when the kosmotropic salt is used alone, but still within the ranges given above for the use of inorganic or kosmotropic salts alone.
  • the aqueous dispersions of the instant invention generally have lower bulk viscosities than comparable aqueous dispersions.
  • a comparable aqueous dispersion is generally one which is substantially identical in many functional aspects, but lacks a particular element of the instant invention.
  • the aqueous dispersions of the instant invention have lower bulk viscosities than comparable aqueous dispersions which have substantially the same polymer solids, cationic charge level and weight average molecular weight, but which lack an important feature of the instant invention e.g.
  • a comparable aqueous dispersion may be one which contains the same amount of each component, except the R 2 , R 3 and R 4 in the corresponding recurring formula (I) unit of the comparable aqueous dispersion together contain a total of 3 carbon atoms, instead of the 4 or more carbons in the corresponding recurring unit of formula (I) in the claimed aqueous dispersion.
  • aqueous dispersions having formula (I) recurring units in which R 2 , R 3 and R 4 contain four or, preferably, five carbons generally have bulk viscosities which are dramatically lower than the bulk viscosities of aqueous dispersions that are substantially identical except that R 2 , R 3 and R 4 contain only three carbons.
  • the bulk viscosity of aqueous dispersions is typically influenced by e.g. total polymer solids, salt level, polymer type, ratio of first cationic polymer to second cationic polymer, etc. as disclosed herein.
  • aqueous dispersions having bulk viscosities of about 20,000 centipoise (cps) or more, or even about 200,000 cps or more may be suitable in certain circumstances, much lower bulk viscosities are generally preferred for ease of handling.
  • Aqueous dispersions having bulk viscosities of about 20,000 centipoise (cps) or less, preferably about 10,000 cps or less, more preferably about 8,000 cps or less, even more preferably about 5,000 cps or less, most preferably about 2,500 cps or less, may be obtained by the practice of the instant invention.
  • Bulk viscosity may be measured by any convenient method known to those skilled in the art, preferably a rotating cylinder viscometer as described in the Examples below.
  • Aqueous dispersions are preferred which have as many of the following advantageous attributes as possible: relatively high cationic polymer solids, preferably 20% or greater, more preferably 25% or greater, by weight based on total; high molecular weight, preferably 2,000,000 or greater, more preferably 5,000,000 or greater; reduced environmental impact (low VOC, substantially free of organic solvents and aromatic groups, e.g.
  • aromatic- or benzyl-containing oils or recurring units aromatic- or benzyl-containing oils or recurring units); minimal levels of diluents (preferably, 20% or less of salt, by weight based on total, and polymer devoid or substantially free of hydrophobic recurring units); bulk viscosity about 2,000 cps or less; for recurring units based on formula (I), R 2 , R 3 and R 4 together containing a total of 5 carbons; and superior or equivalent performance. Products having all of these attributes may be obtained by the practice of the present invention.
  • Aqueous dispersions of water-soluble polymers are preferably formed by polymerization of the corresponding monomers to form the first cationic water-soluble polymer, in the presence of at least one second cationic water-soluble polymer and, in certain embodiments, an inorganic salt.
  • Polymerization may be effected by any initiating means, including redox, thermal or irradiating types.
  • Examples of preferred initiators are 2,2'-azobis(2-amidino-propane)dihydrochloride (V-50), 2,2'-azobis(isobutyronitrile), sodium bromate/sulfur dioxide, potassium persulfate/sodium sulfite, and ammonium persulfate/sodium sulfite, as well as peroxy redox initiators e.g. those disclosed in U.S.
  • Initiator levels are chosen in a known manner so as to create polymers of the desired molecular weight.
  • Amounts of chain transfer agents, e.g. isopropanol, lactic acid, mercaptoethanol, etc. and branching or crosslinking agents, e.g. methylenebisacrylamide may be added in a known manner to further adjust the properties of the first cationic water- soluble polymer.
  • branching or crosslinking agents e.g. methylenebisacrylamide
  • water-swellable or branched, water-soluble polymers may be formed.
  • branching or crosslinking agent increases the tendency for the product to be water-swellable instead of water-soluble, and increased amounts of chain transfer agent tend to reduce molecular weight.
  • chain transfer agent and branching agent are used together, water-swellable products are more likely to be obtained at high branching agent and low chain transfer agent levels, whereas branched, water-soluble polymers may be obtained at high chain transfer and low branching agent levels.
  • Components may be added at any time; e.g. all of the monomers may be present from the onset of the polymerization, or monomers may be added during the course of the polymerization.
  • salt may be present from the onset of the polymerization, or salt may be added during the course of the polymerization or after polymerization is complete.
  • polymerization parameters e.g. temperature and time may be chosen in a known manner, and may be varied during the course of the polymerization.
  • Polymerization is generally effected in the presence of an inert gas, e.g. nitrogen.
  • Conventional processing aids e.g. chelating agents, sequestrants, pH adjusters, etc. may be added as required.
  • aqueous dispersions of the present invention have advantageous aspects in that they are preferably substantially free of dilutive substances such as surfactant, oil, hydrocarbon liquids, organic solvents, etc.
  • viscosity-reducing additives e.g. glycerin, glycerol, alcohol, glycol, etc. may be present in the aqueous dispersions, amounts should be 2% or less, more preferably 1% or less, most preferably 0.1% or less, in order to maintain the advantageous properties of the invention.
  • aqueous dispersions of the instant invention may be homogenous in the absence of a particular component e.g., said second water-soluble polymer.
  • Homogenous compositions are generally characterized as being clear or translucent, and are not aqueous dispersions because they do not contain dispersed droplets as described above.
  • said first cationic water-soluble polymer or said second cationic water-soluble polymer is dispersion-creating in that aqueous dispersions are not obtained in the absence of an effective or dispersion-creating amount of the particular component.
  • Waters used in the present invention may be from any source, e.g. process water, river water, distilled water, tap water, etc.
  • polymerizations are conducted in aqueous solutions that do not contain substantial amounts of materials which detrimentally affect the polymerization.
  • the aqueous dispersions of the present invention tend to dissolve quickly when diluted with water.
  • the aqueous dispersion of the instant invention may be dehydrated to increase the total polymer solids content, or to create substantially dry products. Any means known in the art e.g. stripping, spray drying, solvent precipitation, etc. may be used to reduce the water content. Surprisingly, partial dehydration may reduce the bulk viscosity of an aqueous dispersion, in spite of the tendency for dehydration to increase polymer solids.
  • Dehydration may be performed by heating, preferably under reduced pressure, although of course excessive heating may be detrimental to polymer properties.
  • a substantially dry mass of polymer may be obtained by removal of water, and the mass may be comminuted to create a powdery, particulate, or granular product.
  • substantially dry polymer products may be obtained by spray-drying the aqueous dispersions of the instant invention.
  • oil-containing polymer emulsions and dispersions have been spray-dried, see e.g. U.S. Patent Application Serial No. 08/668,288 and references therein, spray-drying of aqueous dispersions, which are generally free of oil and surfactants, has not previously been reported.
  • vinyl-addition polymer-containing aqueous dispersions may be sprayed-dried by a suitable means into a large chamber through which a hot gas is blown, thereby removing most or all of the volatiles and enabling the recovery of the dried polymer.
  • the means for spraying the aqueous dispersion into the gas stream are not particularly critical and are not limited to pressure nozzles having specified orifice sizes; in fact, any known spray-drying apparatus may be used.
  • means that are well known in the art such rotary atomizers, pressure nozzles, pneumatic nozzles, sonic nozzles, etc. can all be used to spray- dry the aqueous dispersion into the gas stream.
  • the feed rate, feed viscosity, desired particle size of the spray-dried product, droplet size of the aqueous dispersion, etc. are factors which are typically considered when selecting the spraying means.
  • the size and shape of the chamber, the number and type of spraying means, and other typical operational parameters may be selected to accommodate dryer conditions using common knowledge of those skilled in the art.
  • Gas flow may be cocurrent, countercurrent or mixed flow, cocurrent flow being preferred.
  • the hot gas, or inlet gas may be any gas that does not react or form explosive mixtures with the feed and/or spray-dried polymer.
  • gases used as the inlet gas are gases known to those skilled in the art, including air, nitrogen, and other gases which will not cause undesirable polymer degradation or contamination, preferably gases containing about 20% or less oxygen, more preferably about 15% or less oxygen. Most preferably, inert gases such as nitrogen, helium, etc. that contain about 5% or less of oxygen should be used.
  • the dried polymer may be collected by various means such as a simple outlet, classifying cone, bag filter, etc., or the polymer may be subjected to further stages of drying, such as by fluid beds, or agglomeration.
  • the means for collecting the dry polymer product is not critical. There are four interrelated operating parameters in the instant spray-drying process: gas inlet temperature, gas outlet temperature, product volatiles and residence time in the dryer.
  • the outlet temperature generally should be about 150°C or below, preferably about 120°C or below, more preferably less than 100°C, even more preferably about 95°C or below, most preferably about 90°C or below.
  • the outlet temperature is generally about 70°C or higher, preferably about 75°C or higher.
  • outlet temperatures are generally about 70° C to about 150° C, preferably about 70° C to about 120° C, more preferably about 70° C to less than 100°C, even more preferably about 70° C to about 95° C, most preferably about 75°C to about 90°C.
  • Outlet temperatures below about 70°C may be suitable in certain instances, though generally this is less preferred. For instance, at the cost of efficiency, spray drying could be carried out at long residence times, high gas flow rates and low outlet temperatures. Generally, the dryer should be operated at the lowest possible outlet temperature consistent with obtaining a satisfactory product.
  • the inlet temperature, the feed rate, and the composition of the aqueous dispersions may all affect outlet temperatures. These parameters may be varied to provide a desired outlet temperature. Feed rates are not critical, and generally will vary depending on the size of the dryer and the gas flow rate. Inlet gas temperature is less critical than outlet gas temperature, and is generally about 140°C or above, preferably about 160°C or above. The inlet gas temperature is preferably about 200°C or below and more preferably about 180°C or below. Thus, preferred inlet gas temperature ranges from about 140°C to about 200°C, more preferably from about 160°C to about 180°C. Proper inlet gas temperatures tend to avoid product degradation on the high side and to avoid inadequate drying on the low side.
  • Residence time is a nominal value obtained by dividing the volume of the dryer by the volumetric gas flow. Residence time is generally at least about 8 seconds, preferably at least about 10 seconds. Residence time is generally no more than about 120 seconds, preferably no more than about 90 seconds, more preferably no more than about 60 seconds, and most preferably no more than about 30 seconds. Therefore, the general range of residence time is about 8 to about 120 seconds, preferably about 10 to about 90 seconds, more preferably about 10 to about 60 seconds, and most preferably about 10 to about 30 seconds. It is known to those skilled in the art that longer residence times are to be expected when larger dryers are used or when the dryer is run in a less efficient manner. For instance, at the cost of efficiency, longer residence times would be expected at very low inlet temperatures and slow gas flow rates.
  • residence times useful in the present invention may vary from the values described above, depending on the size and type of spray dryer used, the efficiency at which it is operated, and other operational parameters.
  • residence times specified herein may be modified to accommodate dryer conditions using common knowledge of those skilled in the art.
  • polymer particles of the instant invention are generally about 10 microns or greater in diameter, preferably about 40 microns or greater, more preferably about 100 microns or greater, most preferably about 200 microns or greater. It is preferred that the polymer particles be non- dusting. Dusting and flow problems are typically exacerbated when the polymer particles are small, so larger polymer particles are generally desirable. However, very large particles may dissolve more slowly. Therefore, it is generally desirable for the polymer particles to be about 1200 microns or less in diameter, preferably about 800 microns or less in diameter, more preferably about 600 microns or less, most preferably about 400 microns or less.
  • At least about 90% of the polymer particles range in size from about 10 microns to about 1200 microns, preferably at least about 95%, more preferably at least about 98%.
  • the size of the polymer particles can be varied somewhat by altering the operational parameters e.g. spray configuration, aqueous dispersion viscosity, feed rate, etc.
  • Particles may be substantially spherical or non-spherical; "diameter" of a non-spherical particle is the dimension along a major axis.
  • the polymer particles are hollow, porous structures having at least one opening in their walls, it has been discovered that these features are not always necessary in order to obtain particles having desirable properties e.g. fast dissolution times.
  • the spray-drying parameters e.g. nozzle type, nozzle size, outlet temperature, etc. needed to produce particles that are hollow, porous structures having at least one opening in their walls are inconvenient or uneconomical, and it is advantageous to produce particles that lack some or all of these features.
  • the particles formed by the spray-drying processes of the instant invention may be screened to remove an oversize or undersize fraction. Oversize particles may be fragmented by e.g. grinding, whereas undersized particles are generally agglomerated.
  • Sizes may be determined by methods known to those skilled in the art e.g. sieving, screening, light scattering, microscopy, microscopic automated image analysis, etc.
  • the bulk densities of the spray-dried polymer particles of the instant invention are generally greater than the bulk densities of dry polymers prepared by precipitation of e.g. water-in-oil emulsions of the same polymer.
  • Polymer particles having greater density may be advantageous because they occupy a smaller volume, resulting in e.g. lower shipping and storage costs.
  • the bulk densities of the spray-dried polymer particles of the instant invention are generally about 0.35 g/cc or greater, preferably about 0.4 g/cc or greater, more preferably about 0.45 g/cc or greater, most preferably about 0.50 g/cc or greater.
  • the bulk densities of the spray-dried polymer particles of the instant invention are generally about 1.1 g cc or less, preferably about 1.0 g/cc or less, more preferably about 0.95 g/cc or less, most preferably about 0.90 g/cc or less.
  • the bulk densities of the spray-dried polymer particles of the instant invention generally range from about 0.35 to about 1.1 g cc, preferably about 0.4 to about 1.0 g/cc, more preferably about 0.45 to about 0.95 g/cc, most preferably about 0.50 to about 0.90 g/cc.
  • the polymer particles produced by the processes described herein are substantially dry.
  • substantially dry generally means that the polymer contains about 12% or less volatiles, preferably about 10% or less by weight, based on the weight of the spray dried polymer.
  • the polymer generally contains about 2% or more volatiles, preferably about 5% or more, by weight based on total weight, and most preferably contains from about 8% to about 10% volatiles by weight, same basis. The volatiles are measured by determining the weight loss on drying the polymer product at about 105°C for about 30 minutes.
  • agglomeration of the polymer particles of the instant invention may improve the flow properties and dissolution times of the polymers.
  • Agglomeration is a known process for increasing particle size and various methods for agglomerating particles are known to those skilled in the art, e.g. "Successfully Use Agglomeration for Size Enlargement,” by Wolfgang Pietsch, Chemical Engineering Progress, April 1996, pp. 29-45; “Speeding up Continuous Mixing Agglomeration with Fast Agitation and Short Residence Times,” by Peter Koenig, Powder and Bulk Engineering. February 1996, pp. 67-.S4.
  • agglomeration methods such as natural agglomeration, mechanical agglomeration, tumble or growth agglomeration, pressure agglomeration, binderless agglomeration, agglomeration with binders, etc. may be used to agglomerate the polymer particles of the instant invention.
  • Agglomeration may optionally be followed by drying e.g. fluid bed drying, to remove binder e.g. water.
  • Pressure agglomeration is preferred, and mechanical agglomeration using a water binder, followed by fluid bed drying is most preferred.
  • the agglomerates formed by agglomerating the polymer particles of the instant invention tend to have improved flow properties and faster dissolution times when compared to the unagglomerated polymer particles.
  • the agglomerates are non-dusting.
  • about 90% of the agglomerates of the instant invention have an agglomerate size of about 120 microns or greater, preferably about 160 microns or greater, more preferably about 200 microns or greater, most preferably about 300 microns or greater.
  • about 90% of the agglomerates have an agglomerate size of about 1500 microns or less, preferably about 1200 microns or less, more preferably about 1100 microns or less, most preferably about 1000 microns or less.
  • about 90%, preferably 95%, of the agglomerates have a size in the range of about 120 to about 1500 microns, preferably about 160 microns to about 1200 microns, more preferably about 200 microns to about 1100 microns, most preferably about 300 microns to about 1000 microns.
  • at least about 5% of the agglomerates preferably at least about 10%, most preferably at least about 15%, are larger than about 900 microns.
  • the agglomerates formed by agglomerating the spray-dried particles of the instant invention may be screened to remove an oversize or undersize fraction.
  • agglomerates larger than about 1200 microns and smaller than about 175 microns are removed by e.g. screening.
  • Oversize agglomerates are generally fragmented by e.g. grinding, whereas undersized agglomerates are generally recycled into the agglomerator.
  • the bulk density values of the agglomerates of the instant invention tend to be lower than the bulk density values of the spray-dried particles from which they are formed.
  • the bulk densities of the agglomerates of the instant invention are generally about 0.35 g/cc or greater, preferably about 0.4 g/cc or greater, mo.e preferably about 0.45 g/cc or greater, most preferably about 0.50 g/cc or greater.
  • the bulk densities of the agglomerates of the instant invention are generally about 1.0 g/cc or less, preferably about 0.95 g/cc or less, more preferably about 0.90 g/cc or less, most preferably about 0.85 g/cc or less.
  • the bulk densities of the agglomerates of the instant invention generally range from about 0.35 to about 1.0 g/cc, preferably about 0.4 to about 0.95 g/cc, more preferably about 0.45 to about 0.90 g/cc, most preferably about 0.50 to about 0.85 g cc.
  • the polymer particles themselves be of such a size that they are agglomerable. Agglomeration obviously tends to multiply the average particle size, so that it is frequently easier to cause large increases in particle size than it is to cause small increases in particle size. Therefore, to produce agglomerates of a preferred size or size range, it is generally preferred to agglomerate particles that are much smaller than the desired agglomerate size, rather than particles that are only slightly smaller. Agglomerable particles are generally those that may be conveniently agglomerated to produce agglomerates having a preferred size. It is possible, but less preferred, to agglomerate larger particles to produce agglomerates that are larger than desired, then remove the oversize agglomerates as described above.
  • the substantially dry polymer particles and agglomerates of the present invention are generally comprised of the polymer that was contained in the aqueous dispersion that was spray-dried, as discussed hereinabove.
  • Spray-drying of the aqueous dispersions of the instant invention is advantageous because typically 90% or greater, preferably 95% or greater, most preferably substantially all, of the resultant spray-dried polymer particles each individually contains two or more water-soluble or water-swellable vinyl-addition polymers, so that stratification effects may be minimized.
  • Stratification may occur when two different dry polymers having differing particle sizes or particle size distributions are blended together because of the tendency for the larger particles to settle towards the bottom of the container. Stratification on storage may affect blend product performance as the top of the container tends to become enriched in the polymer having the smaller particle size.
  • each polymer in a blend be of similar particle size, see e.g. EP 479 616 A1 and U.S. Patent No. 5,213,693.
  • a dry blend of the two different polymers is likely to exhibit greater stratification than a dry blend obtained by spray-drying the instant aqueous dispersions because the majority of the spray-dried polymer particles of the instant invention each individually contains two or more water-soluble or water- swellable vinyl-addition polymers.
  • the spray-dried aqueous dispersions of the instant invention tend to dissolve faster than polymers obtained by spray-drying conventional water-in-oil emulsions of similar polymers.
  • a suspension of dispersed solids may be dewatered by a method which comprises (a) intermixing an effective amount of an aqueous dispersion of polymers, or aqueous admixture thereof, with a susp3nsion of dispersed SONGS, and (b) dewatering said suspension of dispersed solids.
  • a method which comprises (a) intermixing an effective amount of an aqueous dispersion of polymers, or aqueous admixture thereof, with a susp3nsion of dispersed SONGS, and (b) dewatering said suspension of dispersed solids.
  • Substantially dry polymers derived from the aqueous dispersions of the instant invention as described above may also be used to dewater suspended solids.
  • a suspension of dispersed solids may be dewatered by a method which comprises (a) intermixing an effective amount of a substantially dry water- soluble or water-swellable polymer, or aqueous admixture thereof, with a suspension of dispersed solids, and (b) dewatering said suspension of dispersed solids.
  • an aqueous admixture of the dry polymer or aqueous dispersion is prepared by intermixing the dry polymer or aqueous dispersion with water, more preferably by dissolving the dry polymer or aqueous dispersion in water to form a dilute polymer solution. Effective amounts of dry polymer or aqueous dispersion are determined by methods known in the art, preferably by routine laboratory or process experimentation.
  • suspensions of dispersed solids which may be dewatered by means of the instant invention are municipal and industrial waste dewatering, clarification and settling of primary and secondary industrial and municipal waste, potable water clarification, etc.
  • the polymers may be especially well-suited to situations where part or all of the dewatered solids or clarified water is returned to the environment, such as sludge composting, land application of sludge, pelletization for fertilizer application, release or recycling of clarified water, papermaking, etc.
  • aqueous dispersion or dry polymer preferably an aqueous admixture thereof
  • suspensions of dispersed solids which may be dewatered by means of the instant invention are found in the papermaking area, e.g. the aqueous dispersions or dry polymer may be used as retention aids, drainage aids, formation aids, washer/thickener/drainage production aid (DNT deink application), charge control agents, thickeners, or for clarification, deinking, deinking process water clarification, settling, color removal, or sludge dewatering.
  • the polymers of the instant invention may also be used in oil field applications such as petroleum refining, waster clarification, waste dewatering and oil removal.
  • Dewatering and clarification applications for the aqueous dispersions and dry polymers of the instant invention may also be found in the food processing area, including waste dewatering, preferably waste dewatering of poultry beef, pork and potato, as well as sugar decoloring, sugar processing clarification, and sugar beet clarification.
  • Mining and mineral applications for the aqueous dispersions and dry polymers of the instant invention include coal refuse dewatering and thickening, tailings thickening, and Bayer process applications such as red mud settling, red mud washing, Bayer process filtration, hydrate flocculation, and precipitation.
  • Biotechnological applications for the aqueous dispersions and dry polymers of the instant invention include dewatering and clarification of wastes and preferably, dewatering and clarification of fermentation broths.
  • aqueous dispersions of the instant invention may be employed in the above applications alone, in conjunction with, or serially with, other known treatments.
  • SV Viscosity
  • the bulk density of polymer particles and agglomerates was determined by adding the particles or agglomerates to a suitable preweighed measuring container and 'tapping" or slightly agitating the container to cause the particles or agglomerates to settle. The volume of the polymer was then read from the measuring container, the measuring container weighed, and the bulk density calculated in units of grams per cubic centimeter (g/cc).
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, and a nitrogen inlet tube was charged with 17.10 parts deionized water and 9 parts of a 40% aqueous solution of the polymer obtained by polymerizing the methyl chloride quaternary salt of dimethylaminoethylmethacrylate (poly(DMAEM.MeCI)), weight average molecular weight about 200,000.
  • poly(DMAEM.MeCI) dimethylaminoethylmethacrylate
  • ALD acrylamide
  • DEAEA.DMS dimethyl sulfate salt of diethylaminoethylacrylate
  • the bulk viscosity (BV) of the dispersion was 2250 centipoise (cps) showing preferable fluidity as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25° C.
  • the dispersion was dissolved to give a standard viscosity (SV) of 2.56 cps.
  • Example 2 Additional aqueous dispersions were prepared in the same manner as Example 1 , showing the effect of various polymer and ammonium sulfate salt levels on bulk viscosity as shown in Table 1.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and a nitrogen inlet was charged with 72.60 parts of deionized water and 30.8 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 222,600.
  • a 40% aqueous solution of poly(DMAEM.MeCI) weight average molecular weight about 222,600.
  • 24.37 parts of a 53.33% aqueous solution of acrylamide and 45.93 parts of a 79% aqueous solution of DEAEA.DMS were added and mixed.
  • 31.9 parts ammonium sulfate, 2.57 parts citric acid, and 6.9 parts of 1% solution of EDTA were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 4.93 parts of 1 % solution of V-50.
  • the reaction mixture was heated to 40°C for 2 hours and then raised to and held at 50°C for 4 hours. The overall conversion was greater than 99%.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this dispersion was about 1460 cps showing preferable fluidity as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25° C.
  • the dispersion was dissolved to give a SV of 2.40 cps.
  • aqueous dispersions were prepared in the same manner as Example 9 demonstrating the effect of total polymer solids, ratio of first cationic to second cationic polymer, second cationic polymer molecular weight, and ammonium sulfate salt level on the bulk viscosity (BV) of the aqueous dispersion, as shown in Table 2.
  • Table 2
  • This polymerization was carried out in the same manner as Example 9, except that a poly(DMAEM.MeCI) having a weight average molecular weight of about 395,000 was used.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this aqueous dispersion was about 5100 cps showing preferable fluidity as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25° C.
  • the dispersion was dissolved to give a SV of 2.35 cps.
  • Example 36 This polymerization was carried out in the same manner as Example 34, except that 2.46 parts of 10% glycerol solution was added. Polymerization proceeded smoothly. A stable fluid aqueous dispersion was obtained. The bulk viscosity of this dispersion was about 3700 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25°C showing improved fluidity. The bulk viscosity was greatly reduced relative to Example 34, demonstrating the viscosity-reducing effect of the glycerol additive. The dispersion was dissolved to give a SV of 2.35 cps. EXAMPLE 36
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 39.73 parts deionized water and 30.1 parts of 41 % poly(DMAEM.MeCI), weight average molecular weight about 395,000.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this aqueous dispersion was about 1900 cps as measured with a Brookfield Viscometer No. 4 spindle, 30 rpm at 25° C, showing improved fluidity compared to Example 34 and demonstrating the effect of incorporating hydrophobic recurring units of tertiary butyl acrylamide.
  • the aqueous dispersion was dissolved to give a SV of 2.32 cps.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 78.84 parts deionized water and 30.1 parts of 41 % poly(DMAEM.MeCI), weight average molecular weight about 395,000. After completion of dissolution, 20.95 parts of a 53.57% aqueous solution of acrylamide,
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this dispersion was about 3840 cps as measured with a Brookfield Viscometer No. 4 spindle, 30 rpm at 25°C showing preferable fludity.
  • the dispersion was dissolved to give a SV of 2.14 cps.
  • a suitable vessel with an external jacket for heating or cooling was equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube.
  • the vessel was charged with 294.47 parts deionized water and 117.60 parts of 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 210,000.
  • 94.03 parts of a 52.77% aqueous solution of acrylamide and 173.18 parts of an 80% aqueous solution of DEAEA.DMS were added and mixed.
  • 130.20 parts ammonium sulfate, 9.83 parts citric acid, and 13.17 parts of 2% EDTA were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 7.53 parts of 1% V-50.
  • the reaction mixture was heated to 40°C for 2 hours and then raised to and held at
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 63.18 parts deionized water and 30.8 parts of 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 230,600.
  • ALD acrylamide
  • DEAEA.DMS 80% aqueous solution of DEAEA.DMS
  • 16.94 parts of a 80% aqueous solution of the methyl chloride quaternary salt of dimethylaminoethylacrylate (DMAEA.MeCi) were added and mixed.
  • Example 39 Polymerizations were carried out in the same manner as Example 39 except that the bulk viscosity was adjusted by varying the level of ammonium sulfate salt as shown in Table 3. These Examples demonstrate that aqueous dispersions having low bulk viscosities and high polymer solids may be prepared, wherein the first cationic polymer is a DMAEA.MeCi / DEAEA.DMS / AMD terpolymer.
  • a suitable vessel equipped with an external jacket for heating or cooling, a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 260.35 parts deionized water and 117.6 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 210,000. After completion of dissolution, 107.89 parts of a 52.77% aqueous solution of acrylamide, 99.35 parts of a 80% aqueous solution of DEAEA.DMS and 64.68 parts of a 80% aqueous solution of
  • DMAEA.MeCi were added and mixed. To this mixture, 271.92 parts ammonium sulfate, 9.83 parts citric acid, and 13.17 parts of 2% EDTA were added and mixed. The pH of the mixture was about 3.3. The vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 7.53 parts of 2.5% V-50. The reaction mixture was raised to 40°C for 2 hours, and then raised to and held at 50° C for 4 hours. The overall conversion was greater than 99%. A stable fluid aqueous dispersion was obtained. The bulk viscosity of this dispersion was about 1240 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25° C showing good fluidity. The dispersion was dissolved to give a SV of 2.74 cps.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, and nitrogen inlet tube was charged with 18.86 parts deionized water and 9 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 200,000. After completion of dissolution, 4.39 parts of a 53.64% aqueous solution of acrylamide and 15.19 parts of a 79.3% aqueous solution of DEAEA.DMS were added and mixed. To this mixture, 8.4 parts ammonium sulfate, 0.7 parts citric acid, and 2.02 parts of 1% EDTA were added and mixed. The pH of the mixture was about 3.3. The vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 1.44 parts of 1% V-50. The reaction mixture was raised to 40°C for 2 hours and then raised to and held at
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, and nitrogen inlet tube was charged with 92.9 parts deionized water and 30.1 parts of a 41 % aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 395,000.
  • a 41 % aqueous solution of poly(DMAEM.MeCI) weight average molecular weight about 395,000.
  • 15.03 parts of a 53.57% aqueous solution of acrylamide and 51.53 parts of an 80% aqueous solution of DEAEA.DMS were added and mixed.
  • To this mixture 22 parts of sodium sulfate, 2.57 parts citric acid, and 3.45 parts of 2% EDTA were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 2.46 parts of 2% V-50.
  • the reaction mixture was raised to 40°C for 2 hours and then raised to and held at 50° C for 4 hours. The overall conversion was greater than 99%.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this dispersion was about 1100 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25°C.
  • the dispersion was dissolved to give a SV of 2.19 cps. This Example demonstrates the effectiveness of sodium sulfate.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 17.57 parts deionized water and 9 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 200,000. After completion of dissolution, 4.77 parts of a 53.64% aqueous solution of acrylamide, 12 parts of a 79.3% aqueous solution of DEAEA.DMS and 2.91 parts of an
  • 80% aqueous solution of DMAEA.MeCi were added and mixed.
  • 9.6 parts ammonium sulfate, 0.7 parts citric acid, and 2.02 parts of 1 % EDTA were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 1 .44 parts of 1 % V-50.
  • the reaction mixture was raised to 40°C for 2 hours and then raised to and held at 50° C for 4 hours. The overall conversion was greater than 99%.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this dispersion was about 800 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25° C showing good fluidity.
  • the dispersion was dissolved to give a SV of 2.3 cps.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 89 parts deionized water and 20.9 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 190,000.
  • a 40% aqueous solution of poly(DMAEM.MeCI) weight average molecular weight about 190,000.
  • 30.96 parts of a 52.77% aqueous solution of acrylamide and 21.38 parts of a 80% aqueous solution of DEAEA.DMS were added and mixed.
  • 49.5 parts ammonium sulfate, 2.57 parts citric acid, and 2.34 parts of 1% EDTA were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 3.34 parts of 1% V-50.
  • the reaction mixture was raised to 40°C for 2 hours and then raised to and held at 50° C for 4 hours. The combined conversion was greater than 99%.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this dispersion was about 280 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25° C showing good fluidity.
  • the dispersion was dissolved to give a SV of 1.60 cps.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 82 15 parts deionized water and 30 8 parts of a 20% aqueous solution of po!y(d ⁇ allyid ⁇ methylammon ⁇ um chloride) (poly(DADMAC)), weight average molecular weight about 289,000
  • poly(DADMAC) po!y(d ⁇ allyid ⁇ methylammon ⁇ um chloride)
  • the pH of the mixture was about 3.3
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 3.34 parts of 1% V-50.
  • the reaction mixture was raised to 40°C for 2 hours and then raised to and held at 50°C for 4 hours.
  • the combined conversion was greater than 99%.
  • a stable fluid aqueous dispersion was obtained The bulk viscosity of this dispersion was about 960 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25°C showing preferable fluidity.
  • the dispersion was dissolved to give a SV of 3.67 cps.
  • This Example demonstrates aqueous dispersions having poly(DADMAC) as the second cationic polymer.
  • a suitable vessel equipped with an external jacket for heating or cooling, mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 262.6 parts deionized water, 47.4 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 41 ,500, and 92.60 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 205,000.
  • Polymerization was carried out in the same manner as Example 102, except that the two poly(DMAEM MeCl) polymers were replaced with a single poly(DMAEM.MeCI) having a weight average molecular weight of about 1 ,500,000 The bulk viscosity of this dispersion was about 8,000 cps as measured with a Brookfield Viscometer, No 4 spindle,
  • a suitable vessel equipped with an external jacket for heating, mechanical stirrer, reflux condenser, thermocouple and nitrogen inlet tube was charged with 23.8 parts deionized water and 25.3 parts of a 20% aqueous solution of poly(DADMAC), weight average molecular weight about 289,000.
  • DADMAC poly(DADMAC)
  • After completion of dissolution 7.9 parts of a 53.1% aqueous solution of acrylamide and 11.3 parts of a 77.9% aqueous solution of DEAEA.MeCI were added and mixed.
  • 18 parts ammonium sulfate, 1.08 parts citric acid, 0.37 part of 5% EDTA, and 0.9 part glycerol were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 1.3 parts of 1% V-50 at 40°C. This temperature was held for 2 hours and then was raised to 50°C and maintained at this temperature for 8 hours. The residual acrylamide level was about 209 parts per million (ppm).
  • a stable fluid aqueous dispersion was obtained. The bulk viscosity of this dispersion was about 2,950 cps as measured with a Brookfield Viscometer, No. 4 spindle, 30 rpm at 25°C showing preferable fluidity. The dispersion was dissolved to give a SV of 2.47 cps.
  • Example 104 Polymerizations were carried out in the same manner as Example 104, except that part of the poly(DADMAC) was replaced with a poly(DADMAC) polymer having a lower weight average molecular weight.
  • the effect on the aqueous dispersion bulk viscosity of including the third polymer is shown in Table 8.
  • aqueous dispersion containing 12.5% ammonium sulfate and having a polymer solids of 30%, a bulk viscosity of about 7200 cps and a standard viscosity of about 2.34 cps was prepared in the same manner as in Example 2.
  • aqueous dispersion containing 15.5% ammonium sulfate and having a polymer solids level of 28%, a bulk viscosity of about 2640 cps and a standard viscosity of about 2.4 cps was prepared in the same manner as in Example 9.
  • Example 103 8000 1 ,3-BDS 19.6 24.51 1660
  • aqueous dispersion blend had an overall charge of about 40% and a SV of 2 5 cps
  • Example 48 About 18 parts of a high charge aqueous dispersion prepared as in Example 48 and about 18 parts of a low charge aqueous dispersion prepared as in Example 101 were intermixed with stirring
  • the resultant aqueous dispersion blend was stable and very uniform with a bulk viscosity of about 2300 cps, demonstrating that differently charged dispersions may be blended to prepare an aqueous dispersion having an intermediate charge
  • the resultant aqueous dispersion contained four different polymers
  • Example 9 A polymerization was conducted in the same manner as Example 9, except that the DEAEA.DMS was replaced with an equal weight of DMAEA MeCl During the process of polymerization, the contents of the vessel became so viscous that stirring became impossible The product was obtained as a gel without fluidity
  • This Example demonstrates that replacement of DMAEA MeCl with DEAEA DMS results in an aqueous dispersion having a dramatically lower bulk viscosity
  • Example 91 A polymerization was conducted in the same manner as Example 91 , except that the DEAEA.DMS was replaced with an equal weight of DMAEA.MeCi. During the process of polymerization, the contents of the vessel became so viscous that stirring became impossible. The product was obtained as a gel without fluidity.
  • This Example demonstrates that replacement of DMAEA.MeCi with DEAEA.DMS results in an aqueous dispersion having a dramatically lower bulk viscosity.
  • Example 100 A polymerization was conducted in the same manner as Example 100, except that the DEAEA.DMS was replaced with an equal weight of DMAEA.MeCi. During the process of polymerization, the contents of the vessel became so viscous that stirring became impossible. The product was obtained as a gel without fluidity.
  • This Example demonstrates that replacement of DMAEA.MeCi with DEAEA.DMS results in an aqueous dispersion having a dramatically lower bulk viscosity
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, and nitrogen inlet tube was charged with 20 parts deionized water and 10.51 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 210,000.
  • a 40% aqueous solution of poly(DMAEM.MeCI) weight average molecular weight about 210,000.
  • 6.57 parts of a 53.27% aqueous solution of acrylamide, 14.56 parts of an 80% aqueous solution of DMAEA.MeCi and 4.15 parts of a 80% aqueous solution of DMAEA.BzCI were added and mixed.
  • 10.8 parts ammonium sulfate, 0.4 parts citric acid, and 1.51 parts of 1% EDTA were added and mixed.
  • the pH of the mixture was about 3.3.
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by adding 1.08 parts of 1% V-50.
  • the reaction mixture was raised to 40°C for 2 hours by placing the vessel in a water bath and then raised to 50° C for 6 hours. The conversion was greater than 99%.
  • a stable fluid aqueous dispersion was obtained.
  • the bulk viscosity of this dispersion was about 2000 cps showing preferable fluidity as measured with a Brookfield Viscometer No. 4 spindle, 30 rpm at 25°C.
  • the dispersion was dissolved to give a SV of 2.2 cps.
  • Example 140 Polymerizations were carried out in the same manner as Example 140 The effect of the composition of the first polymer (given in terms of % AMD, % DMAEA.MeCi, and DMAEA.BzCI in monomer feed) and molecular weight of the poly(DMAEM.MeCI) on the aqueous dispersion bulk viscosity is shown in Table 10.
  • aqueous dispersion having a bulk viscosity of about 3570 cps was prepared in the same manner as Example 13. The dispersion was concentrated by placing about 135 parts into a suitable vessel and heating to 45°C under flowing nitrogen. A total of 26 parts of water was removed in two stages by this dehydration process. The aqueous dispersion remained stable demonstrating that dehydration is effective for achieving high solids, low bulk viscosity aqueous dispersions as shown in Table 12.
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, and a nitrogen inlet tube was charged with 277 75 parts deionized water and 1 12 0 parts of a 40% aqueous solution of poly(DMAEM MeCl), weight average molecular weight about 200,000
  • Example 154 Duplicate polymerizations ware carried out in a similar manner to Example 154 except that an additional amount of ammonium sulfate (4% on total) was added approximately 3 hours after initiation of polymerization This prevented any substantial increase in bulk viscosity during the polymerization and resulted in a final bulk viscosity that was lower than the bulk viscosity obtained in Example 154 as shown in Table 13
  • Citric acid 0.58 parts Ammonium sulfate 7.78 parts poly(DMAEM.MeCI) (40 wt. %, 200,000 MW) 7.03 parts
  • aqueous viscosity values were obtained by dissolving or dispersing the aqueous dispersions in the same general manner as for the standard viscosity values described above, except that the polymer concentration was 0.135 wt. %.
  • Lactic acid wt. % MBA (ppm on viscosity (#4 Aqueous Viscosity
  • a aqueous dispersion was prepared as in Example 155.
  • the aqueous dispersion had a bulk viscosity of about 240 cps and an aqueous viscosity (obtained as in Examples 157-172) of 3.55 cps.
  • the aqueous dispersion of Example 173 was spray-dried on a commercially available laboratory spray dryer.
  • the chamber of the laboratory spray dryer was 760 millimeters (mm) in diameter with a 860 mm vertical side and a 65 degree conical bottom. Nominal gas flow through the dryer was about 180 cubic meters per hour.
  • the aqueous dispersion feed was fed at the center of the top of the chamber using a variable speed pump, through a two-fluid nozzle using air for atomization.
  • the outlet gas temperature was 86°C and controlled by varying the inlet gas temperature (169° C) and the feed rate (60 milliliters/minute).
  • the spray-dryer was supplied with nitrogen gas from a cryogenic storage tank.
  • the dried polymer product was discharged through the bottom of the dryer cone to a cyclone where the dry product was removed and collected. Residence time in the dryer was about 14 seconds.
  • the resultant spray-dried polymer particles which had a volatiles content of 3.4% and a bulk density of about 0.50 grams per cubic centimeter (g/cc), were readily soluble in water and had a SV a 3.49 cps.
  • the dissolution rate of the spray- ⁇ ed polymer of Example 174 was compared to a dry polymer of similar composition obtained by spray-drying a commercial water-in-oil emulsion. Solutions were prepared in a wide mouth quart jar using a 2.5 inch magnetic stirring bar. The stirring rate was adjusted so that a deep vortex was obtained in the water. The dry polymer was added slowly over a period of 5 minutes at the edge of the vortex to avoid clumping. The spray-dried polymer of Example 174 wet more readily and completely dissolved over a period of 30-40 minutes, giving a clear solution. In contrast, the dry polymer obtained by spray-drying an inverse emulsion did not wet as rapidly and was not completely dissolved after two hours.
  • This Example demonstrates that a dry polymer obtained by spray-drying an aqueous dispersion of the instant invention dissolved faster than a dry polymer obtained by spray-drying a corresponding water-in-oil emulsion.
  • Example 1 The procedure of U.S. Patent No. 5,403,883 Example 1 was followed, except that the 2-trimethlyammoniumethyl acrylate chloride was replaced by an equal weight of DEAEA.MeCI The resulting aqueous dispersion had a bulk viscosity of about 6,900 cps (#4 spindle, 30 rpm), demonstrating improved bulk viscosity as compared to Example 176C
  • a suitable vessel equipped with a mechanical stirrer, reflux condenser, and a nitrogen inlet tube was charged with 22.94 parts deionized water and 10 5 parts of a 40% aqueous solution of poly(DMAEM.MeCI), weight average molecular weight about 245,000
  • 6 47 parts of a 54.20% aqueous solution of acrylamide, and 7.49 parts of the propyl chloride quaternary salt of dimethylaminoethyl acrylate were added and mixed
  • 10.8 parts ammonium sulfate, 0 7 parts citric acid, and 0 76 parts of a 2% solution of EDTA were added and mixed
  • the pH of the mixture was about 3.3
  • the vessel was sealed and sparged with nitrogen for 30 minutes, and then polymerization was started by addition of 0 54g of 2% aqueous solution of V-50
  • the reaction mixture was heated to 40°C for 2 hours and then raised to 50° C and held for an additional 4 hours The conversion was greater than 99% A stable
  • aqueous dispersion was prepared in a similar manner to Example 40 except that the first polymer composition was AMD/DEAEA DMS/DMAEA MeCl (60/30/10 mole)
  • the aqueous dispersion had a bulk viscosity of about 3,600 cps (No 4 spindle, 30 rpm at 25° C) and a SV of 2.64 cps EXAMPLE 180
  • aqueous dispersion was prepared in a similar manner to Example 40 except that the first polymer composition was AMD/DEAEA.DMS/DMAEA.MeCI (60/25/15 mole)
  • the aqueous dispersion had a bulk viscosity of about 1 ,000 cps (No 4 spindle, 30 rpm at 25° C) and a SV of 2.87 cps.
  • aqueous dispersions of the instant invention was determined by measuring free drainage rate and cake solids from dewatered sludge as follows: Two hundred grams of sewage sludge from a municipal waste treatment plant were weighed into each of a series of jars. Solutions of the aqueous dispersions and of W/O, a commercial water-in-oil emulsion control (60/40 mole % AMD/DM AEA. MeCl), were prepared so that the concentration of the polymer was about 0.2%.
  • the performance of the aqueous dispersions of Examples 118 and 121 is determined by measuring free drainage rate and cake solids from dewatered sludge by following the procedure of Examples 181-261. Similar results are obtained.
  • a solution of the spray-dried polymer of Example 174 is prepared so that the concentration of the polymer is about 0.2%.
  • the performance is determined by measuring free drainage rate and cake solids from dewatered sludge by following the procedure of Examples 181 -261. Similar results are obtained.
  • Solutions of the aqueous dispersions and spray-dried polymers of Examples 9, 44, 61 , 67, 102, 103, 118, 121 , 140, 142, 174, 179, and 180 are prepared so that the concentration of the polymer is about 0.2%.
  • the performance is determined by measuring free drainage rate by following the procedure of Examples 181-261 , except that a 1% suspension of paper solids is dewatered instead of sewage sludge. Similar results are obtained
  • Aqueous admixtures are prepared by intermixing the aqueous dispersions of
  • Examples 157-172 with water so that the concentration of the polymer is about 0.2%.
  • the performance is determined by measuring free drainage rate by following the procedure of Examples 181 -261 , except that a 1% suspension of paper solids is dewatered instead of sewage sludge. Similar results are obtained

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Abstract

L'invention porte sur une dispersion aqueuse de polymères comprenant (a) un premier polymère cationique hydrosoluble ou gonflant en présence d'eau; et (b) au moins un deuxième polymère hydrosoluble différent du premier; et (c) un sel cosmotrope; et (d) un sel chaotrope. Les quantités de (b), (c) et (d) sont telles qu'il est possible d'obtenir une composition homogène en l'absence de (b). L'invention porte également sur un procédé de formation d'une dispersion aqueuse, sur une méthode d'égouttage d'une suspension de solides dispersés, et sur une méthode de production d'eau clarifiée à l'aide de ladite dispersion.
PCT/US1997/016647 1996-10-03 1997-09-16 Dispersions aqueuses Ceased WO1998014405A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
AU44259/97A AU732835B2 (en) 1996-10-03 1997-09-16 Aqueous dispersions
EP97942590A EP0952964A1 (fr) 1996-10-03 1997-09-16 Dispersions aqueuses
IL12919697A IL129196A0 (en) 1996-10-03 1997-09-16 Aqueous dispersions
CA002264803A CA2264803A1 (fr) 1996-10-03 1997-09-16 Dispersions aqueuses
JP51659298A JP2001506674A (ja) 1996-10-03 1997-09-16 水性分散体
MX9902862A MX206802B (es) 1996-10-03 1999-03-25 Dispersiones acuosas
NO991540A NO991540L (no) 1996-10-03 1999-03-30 Vandige dispersjoner

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US72532596A 1996-10-03 1996-10-03
US72552296A 1996-10-03 1996-10-03
US72558696A 1996-10-03 1996-10-03
US72498896A 1996-10-03 1996-10-03
US72684596A 1996-10-03 1996-10-03
US08/725,521 US5919854A (en) 1996-10-03 1996-10-03 Process for preparing aqueous dispersions
US08/725,865 1996-10-03
US08/720,851 1996-10-03
US08/727,693 1996-10-03
US08/727,693 US6702946B1 (en) 1996-10-03 1996-10-03 Aqueous dispersions
US08/720,851 US6608124B1 (en) 1996-10-03 1996-10-03 Aqueous dispersions
US08/720,840 1996-10-03
US08/725,325 1996-10-03
US08/724,988 1996-10-03
US08/724,970 1996-10-03
US08/723,656 US5696228A (en) 1996-10-03 1996-10-03 Process for producing substantially dry polymer particles from aqueous dispersions
US08/725,522 1996-10-03
US08/726,845 1996-10-03
US08/720,840 US6664326B1 (en) 1996-10-03 1996-10-03 Aqueous dispersions
US08/724,970 US5843320A (en) 1996-10-03 1996-10-03 Aqueous dispersions
US08/725,521 1996-10-03
US08/725,865 US5792366A (en) 1996-10-03 1996-10-03 Aqueous dispersions
US08/725,586 1996-10-03
USO8/723,656 1996-10-03

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JP (1) JP2001506674A (fr)
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CA (1) CA2264803A1 (fr)
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WO2000020470A3 (fr) * 1998-10-05 2000-07-20 Cytec Tech Corp Dispersions aqueuses
WO2005100416A1 (fr) * 2004-04-16 2005-10-27 Basf Aktiengesellschaft Procede de production de dispersions aqueuses de lactame polyvinylique
WO2005100415A1 (fr) * 2004-04-16 2005-10-27 Basf Aktiengesellschaft Procédé de production d'une dispersion eau dans eau de polyvinyllactame ayant une valeur k $m(g) 120
DE102004023104A1 (de) * 2004-05-11 2005-12-08 Hwt Wassertechnische Anlagen Gmbh Verfahren zum Aufbereiten von Abwasser oder Prozesswasser
DE102005009809A1 (de) * 2005-03-03 2006-09-07 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur Abtrennung suspendierter Feststoffe
US7323510B2 (en) 2000-12-08 2008-01-29 Ashland Licensing And Intellectual Property Llc Method for the production of water-in-water polymer dispersions
RU2371454C2 (ru) * 2004-12-30 2009-10-27 ЭШЛЭНД ЛАЙСЕНСИНГ ЭНД ИНТЕЛЛЕКЧУАЛ ПРОПЕРТИ ЭлЭлСи Катионные полимерные дисперсии, способ их получения и их применение
US8476391B2 (en) 2004-03-18 2013-07-02 Ashland Licensing And Intellectual Property Llc Anionic water-in-water polymer dispersion, method for the production thereof and its use

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PL2470603T3 (pl) * 2009-08-24 2017-04-28 Solenis Technologies Cayman, L.P. Kationowe sieciowane polimery w dyspersjach polimerowych typu woda w wodzie
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KR101535996B1 (ko) * 2013-04-25 2015-07-13 (주)기륭산업 코스모트로픽 염을 이용해 생성된 양이온성 수분산성 폴리아크릴아미드 공중합체 입자를 함유한 w/o형 에멀젼 고분자 응집제 및 그 제조방법
CN108495868B (zh) * 2016-01-25 2021-03-19 巴斯夫欧洲公司 具有至少双峰分子量分布的阳离子聚合物
PL3408301T3 (pl) * 2016-01-25 2020-08-24 Basf Se Sposób otrzymywania polimeru kationowego o co najmniej dwumodalnym rozkładzie masy cząsteczkowej
CN107058297B (zh) * 2017-06-05 2018-01-16 陈礼平 一种离液剂以及使用该离液剂提取基因组dna的方法
CN109385173A (zh) * 2017-08-10 2019-02-26 中国科学院苏州纳米技术与纳米仿生研究所 疏油涂层材料、油水分离功能材料、其制备方法及用途
JP6837403B2 (ja) * 2017-08-28 2021-03-03 水ｉｎｇ株式会社 油分を含む排水の水処理方法及び油分を含む排水の水処理装置

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EP0525751A1 (fr) * 1991-07-30 1993-02-03 Hymo Corporation Procédé de préparation d'une dispersion d'un monomère cationique soluble dans l'eau
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GB1498136A (en) * 1975-04-04 1978-01-18 Hercules Inc Polymerization of unsaturated monomer with radiation in the presence of salt
US4699951A (en) * 1984-11-13 1987-10-13 Nalco Chemical Company Bimodal cationics for water clarification
EP0262945A2 (fr) * 1986-10-01 1988-04-06 Ciba Specialty Chemicals Water Treatments Limited Compositions de polymères solubles dans l'eau
EP0525751A1 (fr) * 1991-07-30 1993-02-03 Hymo Corporation Procédé de préparation d'une dispersion d'un monomère cationique soluble dans l'eau
US5330656A (en) * 1993-03-05 1994-07-19 Calgon Corporation Polysalt compositions and the use thereof for treating an oil and water system
WO1995033697A1 (fr) * 1994-06-08 1995-12-14 Ab Cdm Egouttage de suspensions

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2000020470A3 (fr) * 1998-10-05 2000-07-20 Cytec Tech Corp Dispersions aqueuses
US7323510B2 (en) 2000-12-08 2008-01-29 Ashland Licensing And Intellectual Property Llc Method for the production of water-in-water polymer dispersions
US8476391B2 (en) 2004-03-18 2013-07-02 Ashland Licensing And Intellectual Property Llc Anionic water-in-water polymer dispersion, method for the production thereof and its use
WO2005100416A1 (fr) * 2004-04-16 2005-10-27 Basf Aktiengesellschaft Procede de production de dispersions aqueuses de lactame polyvinylique
WO2005100415A1 (fr) * 2004-04-16 2005-10-27 Basf Aktiengesellschaft Procédé de production d'une dispersion eau dans eau de polyvinyllactame ayant une valeur k $m(g) 120
DE102004023104A1 (de) * 2004-05-11 2005-12-08 Hwt Wassertechnische Anlagen Gmbh Verfahren zum Aufbereiten von Abwasser oder Prozesswasser
RU2371454C2 (ru) * 2004-12-30 2009-10-27 ЭШЛЭНД ЛАЙСЕНСИНГ ЭНД ИНТЕЛЛЕКЧУАЛ ПРОПЕРТИ ЭлЭлСи Катионные полимерные дисперсии, способ их получения и их применение
DE102005009809A1 (de) * 2005-03-03 2006-09-07 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur Abtrennung suspendierter Feststoffe
DE102005009809B4 (de) * 2005-03-03 2007-02-22 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur Abtrennung suspendierter Feststoffe

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NO991540L (no) 1999-05-28
CA2264803A1 (fr) 1998-04-09
CN1231650A (zh) 1999-10-13
RU2183646C2 (ru) 2002-06-20
AU4425997A (en) 1998-04-24
KR20000048832A (ko) 2000-07-25
ID22894A (id) 1999-12-16
EP0952964A1 (fr) 1999-11-03
JP2001506674A (ja) 2001-05-22
MX206802B (es) 2002-02-20
NO991540D0 (no) 1999-03-30
MX9902862A (es) 1999-10-01
AU732835B2 (en) 2001-05-03

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