The present invention relates to a method for the continuous production of an aqueous poly(meth)acrylate resin dispersion comprising the steps of: I) prov iding a ( meth )acrylate polymer and/or a ( meth )acrylate copolymer; II) adding a neutralizing agent; III) adding water; and IV) mixing the composition to yield a dispersion.

It is known from a wide number of publications and patents to use dispersions based on ( co )polymerisates of v inylic, radically ( co )polymerizable monomers as binders in water-dilutable coatings. Such dispersions are prepared in the art from copolymers or mixtures of copolymers, for example ( metli (acryl ic esters, and further addition of hydroxyfunctional monomers, acid-functional monomers and optionally other monomers and molecular weight regulators.

The preparation of such copolymers or copolymer mixtures in the art is undertaken by free radical polymerization in, for example, a batch process. Optionally, the batch reactor may already be charged with polymers and/or further reactions may take place in the finished reaction mixture. The reaction may be conducted in substance (in bulk ), meaning in the absence of diluting and radically non-reactive substances, in the presence of solvents or as an emulsion polymerization, meaning directly in water. Copolymers or copolymer mixtures thus obtained (general ly referred to as 'resin') typically hav e an acid group content in mmol per 100 g solid polymer of 0.1 to 200 mmol.

For the production and t he use of such ( meth )acrylate polymers in two-component polyurethane coatings reference is made to EP-A 0 947 557, EP-A 1 510 561 , DE-A 10 2004 054447, EP-A 1 657 270, EP-A 1 702 954, EP-A 1 862 485, EP-A 2 025 690, EP-A 0 358 979, EP-A 0 537 568, EP-A 0 543 228, EP-A 0 758 007, EP-A 0 841 352, EP-A 1 141 065, EP-A 1 024 184 and DE-A 4 439 669.

Furthermore, the resin typically has a number av eraged molecular weight of 500 to 50000 g/mol and is provided in the form of a highly viscous melt or a solution. The viscosity is a function of temperature and shear rate and normal ly is in a range of 1 Pa s and 1000 Pa s at shear rates from 40/s to 100/s.

After the manufacture of the copolymers or copolymer mixtures in substance or in the presence of solvents it is necessary to prepare the desired aqueous dispersion in a separate process step. As it is described in the state of the art (e. g. EP-A 947 557, DE-A 4 439 669 or EP-A 1 024 184), in a stirred vessel (usually the reaction vessel), batch-wise one or more basic compounds such as organic amines, ammonia or inorganic base solutions are added to the resin. This is generally referred to as the neutral ization step. Then water is added to the neutralized resin and mixed with it or sometimes the neutralized resin is added to water and mixed with the water. This is general ly referred to as the emulsifying or dispersing step. A part of the resin may also transfer to the aqueous solution.

The polymer particles wit in the emulsion may solidify during cooling. Particles should have a mean size of less than 300 nm, which may be determined by way of the weight average. Then water-di lutable coatings can be produced with good optical properties such as a high gloss and furthermore good storage stability.

It is known in the art that the mixing of highly viscous fluids with low viscosity fluids in stirring vessels is especially difficult and requires long stirring times and high shear rates. Because of this the neutral izat ion step and the emulsi fying step take several minutes to hours, which negatively impacts the economy of the process. Constantly rising economic requirements put forward to the production of aqueous binders cannot be met by such a process. In particular, an increase of the throughput at a given process plant size without large investments ( raising the space-time yield) cannot be achieved with conventional methods.

The present invention has the object of addressing the afore-mentioned drawbacks in the art. In part icular, the invention has the object of prov iding a method for the efficient production f aqueous dispersions comprising a poly(meth)acryiate resin without t e need for widespread investments in the process plant and with a high space-time y ield.

This object is achieved in the present invention by a method for the production of an aqueous poly( meth )acry late resin dispersion, comprising the steps of: I) prov iding a ( meth )acry late polymer and/or a (meth)acrylate copolymer with an acid group content of > 0.1 mmol to < 200 mmol per 100 g of polymer at a temperature of > 50 °C to < 170 °C;

II) adding a neutralizing agent to the ( meth lacry late polymer and/or ( meth )acrylate copolymer to yield an at least partially neutralized (meth)acrylate polymer and/or ( meth lacry late copolymer; III) adding water to the at least partial ly neutralized ( meth lacry late polymer and/or ( meth )acry late copolymer to yield a composition comprising the at least partially neutralized ( meth lacry late polymer and/or (meth)acryiate copolymer and water;

IV) mixing the composition of step III) to yield a dispersion of particles of the at least partially neutralized ( meth lacry late polymer and/or ( meth lacry late copolymer in water. The method is characterized in that at least step III) is conducted as a continuous step. In the method according to the invention aqueous polymer dispersions may be obtained with a solids content of, for example, 25 weight-% to 65 weight-%. The degree f neutralization, defined as the molar ratio of added basic neutralizing agent to the acid groups present in the resin, may be in a range of 30% to 130%. Continuous steps or processes in the sense f the invention are in particular those in which an incoming stream enters an element f a reaction apparatus (such as a reactor or mixer) to be converted or to be processed and exits as an outgoing stream simultaneously but at separate locations. This is opposed to the case of discontinuous processes where the process steps of feeding the components, carrying out process steps and discharging the products take place in temporal succession. Preferably, in a continuous process the run-time of the process and the time in which the products are in the process plant are in a ratio of at least 50: 1.

Suitable monomers which may be employed in the synthesis f the ( meth (acrylate polymers and/or copolymers include aromatic monomers such as styrene, a-methyl styrene or vinyl toluene: aliphatic esters of acrylic and/or methacrylic acid with 1 to 18 C-atoms such as methyl acrlylatc, et hyl acryiate, n -butyl acrylate. iso-butyl acrylate, n-hexyl acrylate, 2-et hylhexyI acrylate, methyl methacrylate, ethyl methacrylate, n-butyl methacrylate, stearyl methacrylate; cycloaliphatic esters of acrylic and/or methacrylic acid with 1 to 12 C-atoms in the alcohol component such as cyclohexyl methacrylate. isobornyi acrylate, isobornyl methacrylate; reaction products of hydroxyalkyl esters f acrylic and. or methacrylic acid with 2 to 4 C-atoms in the hydroxyalkyl rest with ε-capro lactone; α,β-monoolefmically unsaturated mono- or dicarboxylic acids with 3 t 7 C- atoms such as acrylic and/or methacrylic acid, and or at least one hemiester of maleic or fu marie acid with 1 to 14 C-atoms in the alcohol rest such as maleic acid monoethyl ester, aleic acid monobutyl ester: further monomers such as acrylonitri le, methacry lonitrile, maleic acid anhydride, vinyl esters of aliphatic, optionally branched monocarboxylic acids with 1 to 10 C-atoms in the alcohol rest. This exemplary listing is not to be understood as limiting. It is also possible to use further unsaturated monomers as comonomers, cooligomers and even polymers with unsaturated groups. The terms '(meth)acrylate' and '(meth) acrylic' ean the possibility of both acrylate and methacrylate derivatives. It is preferred, but not limited to, to use ( meth (acrylate copolymers with hydroxy I -group containing comonomers, these comonomers including hydroxyalkyl esters f acrylic and/or methacrylic acid with 2 to 4 C-atoms in the hydroxyalkyl rest such as hydroxyethyl acrylate, hydroxypropyl. acryiate, hydroxybutyl acrylate, hydroxyethyl methacrylate and hydroxypropyl methacrylate. The preparation of the ( meth )acrylatc polymers and copolymers is known to a person skilled in the art and may be via radical polymerization in substance (in bulk), in solution or in suspension, continuously or batch-wise.

The hydroxyl group content, expressed as mmol OH groups per 100 g of resin, may be calculated fr m the amount of OH group-containing monomers. Analytic methods include 'H-NM spectroscopy or I R spectroscopy. Titrati n to determine the OH number according to DI I SO 4269 is also possible. Preferred OH group contents are > 5 mmol to < 600 mmol per 100 g of polymer, more preferred > 30 mmol to < 400 mmol per 100 g of polymer, most preferred > 50 mmol to < 350 mmol per 100 g of polymer. The acid group content may preferably be calculated using the acid number determined according to D I EN ISO 2 1 14. I t is further possible to determine the acid number spectroscopically, such as via ^] H-NM R spectroscopy or I R spectroscopy. Preferred acid group contents are > 0. 1 mmol to <

100 mmol per 100 g of polymer, more preferred > 10 mmol to < 50 mmol per 100 g of polymer.

The mean particle size in the dispersions obtained by the method according to the invention and determined by ultracentrifugation may have a d50 value of > 10 urn to < 300 nm and preferably >

1 nm to < 250 nm. The d50 value is the value at which 50 weight-% of all particles are above this value and 50 weight-% of all particles are below. Ultracentrifugation methods are described in: W. Scholtan, H. Lange, Kolloid-Z. u. Z. Polymere 250 (1972) 782 and in K G. Muller, Colloid Polym Sci 267 (1989) 1113. Final ly, the polymers employed may have a number averaged molecular weight M _n ( determined at 23°C by Size Excluding Chromatography using polystyrene standard for calibration and tetrahydrofurane as eliient ) of 500 to 50000 g/moi, preferably 1000 to 40000 g/mol and more preferred 2000 to 30000 g/mol.

Polymers provided in the initial step f the method according to the invention may be dissolved in solvents such as, but not l imited to, butyl glycol, solvent naphtha and/or propylene glycol-n-buty l ether. The temperature range of > 50 °C to < 170 °C prov ides for a melting, dissolution and adequately processible viscosity of the polymer. Preferred are temperatures of > 80 °C to < 120 °C.

The neutralization step may be conducted using mixing units such as extruders, stat ic mixers, spike mixers, nozzle jet dispersers, rotors and stators or under the influence of ultrasound. Residence time in the mixing units ma be, f r example, from > 10 seconds to < 20 minutes, preferably from > 30 seconds to < 12 minutes and more preferred from > 60 seconds to < 3 minutes. The ratio of length to diameter in the static mixer during this step may be in a range of > 1 :5 to < 1 : 100, preferably > 1 : 10 to < 1 :50 and more preferred 1 : 15 to < 1 :30. Neutralizing agents may be bases such as, for example, amines.

The continuous emulsifying or dispersion may also be performed using mixing units such as extruders, static mixers, spike mixers, nozzle jet dispersers, rotors and stators or under the influence of ultrasound. Residence time in the mixing units may be, for example, from > 10 seconds to < 20 minutes, preferably from > 30 seconds to < 1 2 minutes and more preferred from > 60 seconds to < 3 minutes. The ratio of length to diameter in the static mixer during this step may be in a range of > 1 :5 to < 1 : 100, preferably > 1 : 10 to < 1 :50 and more preferred > 1 : 1 5 to < 1 :30.

Further preferred embodiments and other aspects of the present invent ion are described below. They can be combined freely unless the context clearly indicates otherwise.

Of course, al l the other steps may be continuous steps. In one embodiment of the method according to the invention steps I), II), III) and IV) arc conducted as continuous steps. in another embodiment of the method according to the invention in step II) the ( meth (acry late polymer and/or ( meth (aery late copolymer are neutralized to a degree of > 30% to < 130%. As already outlined, the degree of neutral ization is to be understood as the molar ratio of added basic neutral izing agent to the acid groups present in the resin. For example, a degree of neutral ization of 1 10%) would correspond to a ratio of 1 . 1 molar equivalents of basic component such as amines to 1 mo I of acid groups. A preferred degree of neutral ization is > 50%> to < 120%.

In another embodiment of the method according to the invention the neutralizing agent in step II) comprises an organic amine. Preferred are trialky amines and most preferred are triethanolamine, dimethylethanolamine and combinations thereof.

In another embodiment of the method according to the invention a ( meth )acrylate copolymer is used which is a copolymer obtainable from at least one a Iky I met hacry late, at least one hydroxyalkyl ( meth (acrylate, at least one a Iky I acrylate, and at least one ( meth (acryl ic acid, and optionally styrene. Part icularly preferred is a combination of at least two comonomers selected from methyl methacrylate, hydroxyethyl methacrylate, butyl ( meth (acrylate, isobornyl ( meth (acrylate, cyclohexyl (meth)acrylate, styrene and ( meth (acryl ic acid.

In another embodiment of the method according to the invention in step I) the acid group content of the ( meth (acrylate copolymer is > 0.1 mmol to < 10 mmol per 100 g of polymer and the ( meth)acrylate copolymer is produced using v iny ic comonomers comprising substituents with polyoxyalkylene units ( ^~ -CH2 ^~ -CH(R ¹ ) ^~ -0-) _m , R ¹ denoting H or alkyl and m hav ing a value of > 4 to < 60. The aforementioned alkyl can preferably contain 1 -30 carbon atoms in the alkyl part and can be unsubstituted or substituted with optional ly 1 , 2, 3, 4, 5, 6, 7, 8 or 9 substituents selected independently of one another from the group consisting of F, Ci, Br, I,— CN,— NO; ,— OH,— NH _\ SH,— 0(Ci _-5 -alkyl),— S(Ci _-5 -alkyl), NH(CY<-alkyl ),— N(Ci _-5 -alkyl) (G-s-alkyl), OCF ₃ , C ₃ -8-cycloalkyl and— SCF ₃ .

Preferred are alkyl groups selected from the group consisting f methyl, ethyl, n-propyl. isopropyl, n-buty , sec-butyl, isobutyl, tert-butyl, n-pentyl, sec-pentyl, neopentyl and n-hexyl, which can optionally be substituted with I , 2, 3, 4, 5, 6, 7, 8 or 9 substituents selected independent ly of one another from the group consisting of F, CI, Br, I. CN, NO:, OH. NH _: , SH, OCl h, O— C ₂ H ₅ , SCH„ S C;H — OCF ₃ , SCF?,— NH— CH3,— N(CH ₃ ) ₂ , - ^™ N(C ₂ H ₅ )2 and— N(CH3)(C2H5). More preferred are unsubstituted alkyl groups selected from the group consisting f methyl, ethyl, n-propyl, isopropyl, n-butyi, sec-butyl, isobutyl, tert-butyl, n-pentyl, sec-pentyl, neopentyl and n-hexyl. Such a low acid group content may, under certain circumstances, not be sufficient to ensure the emulsification of the resin in water. Therefore it is advantageous to incorporate these

polyoxyalkylene units into the resin. Preferably, R ¹ denotes H or methyl.

In another embodiment of the method according to the invention in step I) the acid group content of the ( meth )acrylate copolymer is > 0.1 mm l to < 10 mmol per 100 g f polymer and t he ( meth)acrylate copolymer is produced using vinylic comonomet s comprising substituents with amino groups NR R \ wherein R ² and R ³ denote, independently of each other, H, Ci to C30 alkyl r C7 to C37 alkylaryi. These groups may be converted to ammonium groups by reaction with acids in order to improve the emulsification of the resin in water.

Aryl, as referred to in the present invent ion, is understood as meaning ring systems with at least one aromatic ring but without heteroatoms even in only one of the rings. These aryl is unsubstituted or subst ituted with 1 , 2, 3, 4 or 5 substituents selected from the group consisting of F, CI, Br, I, ΝΗ;·, SH, OH , SO2, oxo, carboxy, amido, cyano, carbamyl, nitro, phenyl, benzyl, -SO2 H2, Ci-6 alkyl and Ci-6-alkoxy. Preferred examples of aryl include but are not restricted to phenyl, naphthyl, fluoranthcnyl, fluorenyl, tetralinyl or indanyl or anthracenyl radicals, which are unsubstituted or substituted.

Alkylaryi, as defined in the present invention, comprises a linear or branched, unsubstituted or substituted alkyl which is bonded to an aryl group, as defined above. A preferred alkylary i is a benzyl group, wherein the alkyl chain is linear or branched and unsubstituted or substituted with 1 , 2, 3, 4 or 5 substituents selected from the group consisting of F, CI, Br, I, N¾, SH, OH, SO:, CF3, carboxy, amido, cyano, carbamyl, nitro, phenyl, benzyl, -SO2.NH2, Ci-6 alkyl and Ci-6-alkoxy.

In another embodiment of the method according to the invention an emulsifier selected from the group consisting of cationic, anionic and. or nonionic emulsifiers is added in one or more of steps I), II), III) and IV). Suitable emulsi fiers are known to those skil led in the art and are, for example, listed in Surfactants and Polymers in Aqueous Solution, by K. Holmherg, B. Jonsson, B. Kronberg, B. Lindman, 2.nd Edition, J. Wiley, New York, 2002, such as anionic, for example, alkali metal or ammonium salts of long-chain carboxylic acids with 10 to 50 carbon atoms, alkali metal or ammonium alkyl sulfates, alkyl sul fonates, alkylarylsulfonates, sulfosuccinates, cationic, for example long-chain quaternary ammonium ammoniums salts with or without incorporation f ethylene oxide units, non-ionic, for example, polyoxoethylenated long-chain alcohols or

alklyphenols or, for example, zwitterionic with both positive and negative charge on the

hydi opliilic group I t is particularly preferred to add the emulsifier if the acid group content of the ( meth )acrylate copolymer is > 0.1 mmoi to < 10 mm l, as described by the two embodiments above. Anionic and cationic emulsi iers are not compatible with each other, but non-ionic and zwitter-ionic emulsifiers may be used in the mixtures. The typical emulsifier amount based on the resin is within a range of 0.1 weight-% to 5 weight-%. In another embodiment the method according to the invention step IV) is performed using a static mixer. Static mixers are known to those in ski l led in the art and are, for example, described in Arno Signer, Statisches Mischen in der Kunststoffverarbeitung und -herstellung, Plastverarbeiter 11(43), 1992. Particularly preferred are static mixers of the SMX type, which are also known to those skilled in the art and are also mentioned in this publication. The ratio of length to diameter in the static mixer during this step may be in a range of > 1 :5 to < 1 : 100, preferably > 1 : 10 to < 1 :50 and more preferred > 1 : 15 to < 1 :30.

It is known that in a static mixer problems may arise when a low viscosity fluid (liquid, supercritical r gaseous) and a high viscosity fluid are metered separately. In particular with a high volume ratio between a low viscosity fluid and a high viscosity fluid the effect has been observed that bubbles f the low viscosity fluid pass the static mixer with virtually no mixing hav ing occurred. This leads to a reduced efficiency o the static mixer and may lead to a loss of function for the mixer. A special embodiment of the method according to the invention addresses this problem by performing step III) in a continuous manner using a nozzle with an, in radial direct ion, inner channel through which the water flows and a lural ity f, in radial direct ion, outer channels through which the at least partially neutralized ( metli)acrylate polymer and/or ( meth )acrylate copolymer flows.

It is preferred that the nozzle is constructed in such a way that to every partial stream of the high viscosity fluid (the at least partial ly neutralized ( meth )acrylate polymer and/or ( meth )acrylatc copolymer) an additional partial stream of the low viscosity fluid (water) is added.

The nozzle has the effect that the low viscosity fluid is the continuous phase. Then a high surface area is achieved by the individual channels from which the high viscosity fluid exits and a rapid dispersion takes place. Furthermore, the addition of the low viscosity fluid on the side of the channels which are faced towards the exterior side of the pipeline leads to a separation of the high viscosity fluid from the wall f the pipeline. This prevents a prolonged contact with the wall. Because contacting the wall may lead to a chemical degradation of the polymer as ev ident in the occurrence of discoloring, particle agglomeration or gel formation.

It has surprisingly also been found that the amount f neutralizing agent has a direct influence on the viscosity and the size f particles in the polymer dispersion obtained in the method according to the invention. From conventional stirring batch processes it is known that viscosity and particle size cannot be adjusted over a wide range but rather only small changes in the polymer properties are possible by adding a very specific amount of neutralizing agent. This fact opens a convenient possibility for a new process control and for quality control. Therefore, in another embodiment of the method according to the inv ention in the dispersion of step IV) the size of the particles is measured and the amount of neutralizing agent added in step II) is controlled so as to reach a lies i red particle size. The particle size ( mean particle size) may be determined by methods such as laser correlation spectroscopy, dynamic light scattering, ultracentrifugation or acoustic attenuation spectroscopy. It may be necessary to take samples from the product stream. Preferably this is done automatically.

In another embodiment f the method according to the inv ent ion the viscosity of the dispersion f step IV) is measured and the amount of neutralizing agent added in step II) is controlled as to reach a desired viscosity. The viscosity may be determined by known methods such as the pressure drop over a capillary r by osci llatory measurements. The present invention will be further described with reference to the following figures and examples without wishing to be limited by them. Examples

FIG. 1 shows the apparatus set up used in Example 1 F IG. 2 shows the apparatus set up used in Example 2 FIG. 3 shows the parameters of the resulting dispersions from Example 2 (viscosity and mean particle size as function of the neutralization degree)

FIG. 4 shows the parameters of the resulting dispersions from Example 3 (viscosity and mean particle size as function of the neutralization degree)

FIG. 5 shows an example of the nozzle design according to the invent ion FIG. 6 shows the incorporation of the inventive nozzle into the flange Glossary:

Base resin 1 : an 85 weight-% solution of a hydroxy! group-containing acrylate resin with a hydroxy! group content of 195 mmol per 100 g of solid resin, an acid group content of 50 mmol per 100 g of solid resin. This resin was prepared according to the Example I of EP-A 0947557. Solvent: butyl glycol: solvent naphtha 50:50 weight-%. Base resin 2: an 85 weight-% solution of a hydroxy! group-containing acrylate resin with a hydroxy! group content of 230 mmol per 1 00 g of solid resin, an acid group content of 50 mmol per 100 g of solid resin. This resin was prepared according to the Example 1 of EP-A 1391469. Solvent: propylene glycol-n-butyl ether (Dowanol ^® PnB) : solvent naphtha (Solvesso ^® SN100) 50:50 weight-%. Methods: Particle size measurements: laser correlation spectroscopy, Malvern® Zetasizer, Z-mean value.

Viscosity measurement : mPa s according to DIN EN I SO 3219/A.3.

Hydroxy! group content: calculated from the OH group-containing acrylate monomers.

Acid group content: calculated using the acid number determined according to DIN EN ISO 2 1 14. p! l v alue: dilution of the dispersion with deionized water by 1 :4; DIN ISO 976. Example 1 (emulsifying step): in a reaction system according to FIG. 1 a 1 0 l iter vessel 1 was charged with 7.5 kg of the base resin 1 solution, followed by heating to 90 °C. Over the course f one minute the neutralization agent, 199 g dimethylethanolamine, were added and it was homogenized by stirring f r 20 minutes.

Deionized water from vessel 4, which can be connected or disconnected via valve 5, was metered using pump 6, heated to 90 °C in heat exchanger 7 and was contacted with the resin-amine mixture in nozzle 8. The product streams were then dispersed in static mixer 9.

Using heat exchanger 10 the dispersion was cooled and transferred to storage vessel 12 via pressure reducing valve 1 1 .

The static mixer 9 was an SMX mixer with a diameter f 34 mm and a rat io f length to diameter of 20.

The throughput f the resin-amine mixture was 7.7 kg/h and f the water was 7.5 kg/h. The particle size determined was 145 nm and the viscosity 0.83 Pa s.

Residence (dwell) time in the static mixer was 1 1 7 seconds.

Example 2 ( neutral ization and emulsifying): In a reaction system according to FIG. 2 a 10 liter vessel 1 was charged with 7.6 kg of the base resin 1 solution, fol lowed by heating to 90 °C. 7.82 kg/h of the resin solution were metered using pump 3 and mixed with dimethylethanolamine from vessel 13 using pump 1 5 in static mixer 1 .

6.97 kg/h f deionized water from vessel 4, which can be connected r disconnected via valve 5, were metered with pump 6, heated to 90 °C using heat exchanger 7 and contacted with the resin- amine mixture in nozzle 8.

The amine throughput was varied between 188 g/h and 232 g/h. This corresponded to a neutralization degree f 94% to 1 16%. The product streams were then dispersed in static mixer 9.

Using heat exchanger 10 the dispersion was cooled and transferred to storage vessel 12 via pressure reducing valve 1 1. The static mixer 1 6 was an SMX mixer with a diameter f 22 mm and a ratio of length to diameter of 2 1 . The residence time in the static mixer was 70 s.

The static mixer 9 was an SMX mixer with a diameter of 27 mm and a rat io of length to diameter of 15. Residence time in the static mixer was 45 seconds. FIG. 3 shows the results obtained according to example 2, where the particle size is given as a function of the neutralization degree, it can be seen that all particle diameters were less than 145 nm, which is a surprising result. It can also be seen that the amine addition has a direct, approximately linear influence on the viscosity and the particle size. This surprising effect may be the basis of a process control concept.

Example 3 (neutralization and emiilsifving): In a reaction system according to FIG. 2 a 10 liter vessel 1 was charged with 7.3 kg of the base resin 2 solution, followed by heating to 105 °C. 7.74 kg resin were metered using pump 3 and combined with a mixture of 75 mass-% triethanolamine and 25 mass-% dimethylethanolamine from vessel 13 using pump 1 in static mixer 16.

6.89 kg/h deionized water from vessel 4, which can be connected or disconnected v ia valve 5, were metered with pump 6, heated to 70 °C using heat exchanger 7 and contacted with the resin-amine mixture in nozzle 8.

The amine throughput was v aried between 354 g h and 402 g h. This corresponded to a neutralization degree of 95% to 1 10%. The product streams were then dispersed in static mixer 9.

Using heat exchanger 10 the dispersion was cooled and transferred to storage vessel 12 v ia pressure reducing v alve 1 1.

The static mixer 16 was an SMX mixer with a diameter of 22 mm and a ratio of length to diameter of 2 1 . The residence time in the static mixer was 70 s.

The static mixer 9 was an SMX mixer with a diameter of 27 mm and a rat io of length to diameter of 15. Residence time in the static mixer was 46 seconds. FIG. 4 shows the results obtained according to example 3, where the particle size is giv en as a function of the neutralization degree. It can be seen that all particle diameters were less than 200 nm, which is a surprising result. It can also be seen that the amine addition has a direct, approximately linear influence on the viscosity and the particle size. This surprising effect may be the basis of a process control concept.