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
  • C08F6/00—Post-polymerisation treatments
  • C08F6/006—Removal of residual monomers by chemical reaction, e.g. scavenging

Definitions

• the invention relates to a method for reducing the residual monomer content of aqueous polymer dispersions by chemical aftertreatment with a special redox initiator system.
• aqueous polymer dispersions After their preparation by radical polymerization or copolymerization, aqueous polymer dispersions contain, in addition to a polymer solids content of 30 to 75% by weight, due to the incomplete polymerization of the monomers used in the radical free-radical polymerization, which usually up to a monomer conversion of 95 and preferably 98- 99% by weight is still carried out, an undesirable proportion of unbound free monomers
• EP-A 379 892 and DE-A 3834734 disclose the use of Rongalit C (Na salt of hydroxymethanesulfinic acid) as a reducing agent.
• Component known in the redox initiator system for such an aftertreatment It is disadvantageous that formaldehyde easily forms during the postpolymerization reaction. If acetone bisulfite is used as a reducing agent therefor, as described in US Pat. No.
• DE-A 4435422 recommends redox initiators with formamidine sulfinic acid as a reduction component for the postpolymerization of polymer dispersions.
• their limited water solubility and the inconsistency of its aqueous solutions in contact with air are disadvantageous, which makes their technical handling more difficult.
• the use of reducing sugars such as glucose, ascorbic acid or isoascorbic acid as a component in the redox initiators can lead to discoloration.
• the object of the present invention is to achieve a reduction in the residual monomer content in aqueous polymer systems without the formation of further volatile constituents or odor carriers.
• the residual monomer content should be reduced without the formation of microcoagulate and should be easy to use technically, e.g. even in concentrated systems.
• R 1 and R 2 are hydrogen, a Ci-C ⁇ alkyl or Cg-C ⁇ 2 _Aryloli and may be the same or different, with the proviso that at least one radical of R 1 and R 2 is hydrogen, and / or
• Suitable ⁇ -hydroxycarboxylic acids are, in particular, aliphatic hydroxycarboxylic acids with preferably 2 to 8 carbon atoms, such as glycolic acid (hydroxyacetic acid), glyoxylic acid hydrate (dihydroxyacetic acid), lactic acid (2-hydroxypropionic acid), glyceric acid (2, 3-dihydroxypropionic acid) ), Malic acid (2-hydroxy succinic acid) or tartronic acid (2-hydroxymalon acid). The use of tartaric acid is preferred.
• the chemical deodorization system according to the invention is characterized in that when it is added under suitable reaction conditions, the olefinically unsaturated compounds (residual monomers) are reduced without further volatile compounds being formed as a by-product or coagulate being formed as a result of an electrolyte additive.
• the oxidizing agent of the redox initiator system should be able to form radicals.
• the combination of oxidizing agent and reducing agent can also be replaced in whole or in part by a peracid.
• Hydrogen peroxide is preferably used as the oxidizing agent in the redox system, furthermore potassium peroxide, sodium peroxide, sodium perborate and other precursors which form hydrogen peroxide in water.
• Suitable oxidizing agents are also tert-butyl hydroperoxide, cumene hydroperoxide, ammonium, potassium or sodium persulfate, peroxydisulfuric acid and its salts, ammonium, potassium or sodium perphosphate or diperphosphate, potassium permanganate and other salts of peracids.
• the combination of tartaric acid and hydrogen peroxide with iron (II) sulfate as catalyst has proven to be particularly effective as an initiator system.
• the amount of redox initiator system added is preferably in the range from 0.01 to 10, in particular 0.01 to 5,% by weight, based on the monomers used.
• the redox initiator system used for the aftertreatment according to the invention is different from the initiator system used for the main polymerization of the monomers.
• the components of the initiator system used according to the invention are expediently metered in simultaneously or in succession for a period of from 1/2 to 5 hours for the aftertreatment of the polymer dispersion, which may be under pressure, to about 20 to 150 and in particular to 60 to 120 ° C., with stirring , in which case the oxidizing agent is preferably added first.
• the addition of the initiator components can e.g. from above, below or through the side of the reactor.
• Anchor and blade stirrers are preferred as stirrers.
• the dispersed polymers preferably have a particle size of 50 to 400 nm and a monomodal or broad distribution.
• the initiator systems added in the aftertreatment of the polymer dispersions can also contain polyvalent metal ions which can change their valence level. These have a catalytic effect and support electron transfer reactions. Iron, copper, manganese, vanadium, nickel, cerium, chromium, platinum and palladium ions are very suitable for this, of which iron and manganese ions are preferred.
• bases is often expedient in order to adjust the pH of the polymer dispersion to a suitable value. Suitable bases are sodium hydroxide solution, ammonia water and triethanolamine.
• the pH of the polymer dispersion in the aftertreatment according to the invention is preferably less than 8, preferably between 5 and 7.
• the pH can also be in the basic range, but this is associated with disadvantages.
• Hydrogen peroxide is unstable in the basic range, the acid is in salt form and therefore only in the water phase, and the catalyzing metal ions are converted into poorly soluble hydroxides or hydroxo complexes.
• the setting of higher pH values is therefore only under special conditions, e.g. under complex conditions, makes sense.
• the process according to the invention is particularly suitable for reducing the amount of residual monomers in aqueous dispersions of copolymers of acrylates and methacrylates (esters of acrylic acid or methacrylic acid with C ⁇ -C ⁇ 2 alkanols, in particular Ci-Cg alkanols, methyl, ethyl , n-butyl and 2-ethylhexyl acrylate and methacrylate are particularly preferred), styrene such as styrene-butadiene or styrene (meth) acrylic ester copolymers and vinyl acetate copolymers such as ethylene-vinyl acetate copolymers the main monomers, the monomer mixtures used for the polymerization can also be preferred in smaller amounts in amounts of 0.01 to 10% by weight of the total amount of monomers, polar monomers such as acrylic acid, methacrylic acid, acrylonitrile, maleic acid or their anhydride or hydroxyalkyl (meth
• aqueous polymer dispersions aftertreated according to the invention is known to the person skilled in the art (see, for example, Encyclopedia of Polymer Science and Engineering, Vol. 8, 659 ff. (1957); DC Blackley in High Polymer Latices, Vol. 1, 35 ff (1966 ); F.Hölscher, dispersions of synthetic high polymers, Springer-Verlag Berlin (1969)). It is carried out by emulsion polymerization of the olefinically unsaturated monomers in the presence of a preferably water-soluble polymerization initiator, in particular a redox initiator, and in the presence of emulsifiers and, if appropriate, protective colloids and customary further additives.
• a preferably water-soluble polymerization initiator in particular a redox initiator
• the monomers are added by continuous addition.
• the initiator used is preferably peroxodisulfuric acid and / or its salts in amounts of 0.1 to 2% by weight, based on the total amount of monomers.
• the polymerization temperature is generally 20 to 150 and preferably 60 to 120 ° C. The polymerization may take place under
• anionic emulsifiers alone or in a mixture with nonionic dispersants, are used as emulsifiers in an amount of in particular 0.5 to 6% by weight of the total amount of monomers.
• the aftertreatment of the aqueous polymer dispersion according to the invention to reduce the residual monomer content takes place in particular after at least 95 and preferably at least 98 to 99% by weight of the total amount of monomers in the main polymerization has been converted.
• the ratios in the main polymerization and in the aftertreatment are generally different. While in the main polymerization with a high concentration of monomers and growing and thus always more hydrophobic oligomer radicals the radical entry into the dispersion particles is easy, this becomes very difficult in the aftertreatment due to the low monomer concentration and the lack of increasing and thus always more hydrophobic oligomer radicals.
• oxodisulfate 480 g water.
• the monomer emulsion was fed into the reactor for 3 1/2 hours and then polymerized for one hour at the polymerization temperature of 80.degree.
• a copolymer dispersion with a solids content of 51% and a pH of 3.4 was obtained. It had a residual monomer content of 5726 ppm n-butyl acrylate and 449 ppm styrene.
• the polymer dispersion was mixed with iron (II) sulfate solution (0.01%, based on the total amount of monomers used to prepare the polymer dispersion) and adjusted to a pH of 7 with sodium hydroxide solution. Then the two redox components [a) a 20% strength aqueous hydrogen peroxide solution as oxidizing agent and b) a 30% strength aqueous tartaric acid solution as reducing agent] were metered into the polymer dispersion separately at a feed rate of 10 ml per hour at 85 ° C.
• iron (II) sulfate solution 0.01%, based on the total amount of monomers used to prepare the polymer dispersion
• an aqueous polymer dispersion was prepared from a mixture of the following composition:
• Emulsifier Eml was a 20% solution of an octylphenol ethoxylated with 25 moles of ethylene oxide.
• Emulsifier Em2 was a neutralized sulfated nonylphenol ethoxylated with 25 moles of ethylene oxide.
• the polymer dispersion prepared by 3.5 hours of monomer emulsion feed and one hour after-reaction at the polymerization temperature of 85 ° C. had a solids content of 54% and a residual monomer content of 9609 ppm n-butyl acrylate and 360 ppm acrylonitrile.
• the pH is 7.
• Post-treatment according to the invention In the post-polymerization (chemical deodorization), the two redox components a) a 10% aqueous hydrogen peroxide solution and b) a 22% aqueous tartaric acid solution were separated at a feed rate of 10 ml / hour at a pH of Worth 7 and a temperature of 85 ° C in the 1.8 x 10 ⁇ 4 mol / L iron (II) sulfate-containing polymer dispersion.
• the two redox components [a) a 10% aqueous hydrogen peroxide solution and b) a 22% aqueous tartaric acid solution] with a feed rate of 10 mL / hour each at a pH of 7 and Metered into the 1.8 x 10 " 4 mol / L iron (II) sulfate-containing polymer dispersion at 85 ° C.
• a reduction in the residual monomer styrene was based on 5 ppm (99.7% reduction)
• the residual amount of acrylic acid was below the detection limit ( ⁇ 10 ppm).

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• 1997
  • 1997-09-18 DE DE19741187A patent/DE19741187A1/de not_active Withdrawn
• 1998
  • 1998-09-17 EP EP98948987A patent/EP1023335B1/de not_active Expired - Lifetime
  • 1998-09-17 BR BR9812464-1A patent/BR9812464A/pt not_active IP Right Cessation
  • 1998-09-17 WO PCT/EP1998/005928 patent/WO1999014249A1/de not_active Ceased
  • 1998-09-17 AU AU95411/98A patent/AU9541198A/en not_active Abandoned
  • 1998-09-17 DE DE59809028T patent/DE59809028D1/de not_active Expired - Fee Related
  • 1998-09-17 JP JP2000511796A patent/JP2001516775A/ja active Pending
  • 1998-09-17 US US09/508,104 patent/US6444760B1/en not_active Expired - Fee Related

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