MXPA98006665A - Process to cool dispersions and liqui - Google Patents

Abstract

The present invention relates to a process for deodorizing and subsequently cooling dispersions or liquids, comprising: a) passing a current through the dispersion or liquid to be deodorized and maintained in a container (1), causing the dispersion or liquid forms foam as a result, b) discharge the foam from the upper section of the container through the nozzle (5) to a vacuum separation vessel (4) breaking the foam in the process, c) condensing the formed water vapor of the foam in a heat exchanger (8) and remove the volatile organic components at the same time, and d) return the broken foam to the container (1), steps a) and d) are carried out until the dispersion or liquid has been deodorized to the desired degree, for its application, wherein after the end of the deodorization according to steps a) to d), the dispersion or liquid is discharged from the container section (1) through e the nozzle (5) towards the vacuum separation vessel (4), so that the dispersion or the liquid is cooled, the nozzle (5) and the vacuum separation vessel (4) are also used in advance to perform step b), wherein the water vapor maintained in the separation vessel (4) is condensed in the heat exchanger (8) which was also employed beforehand in step c), and where the dispersion or liquid cooled It is discharged from the bottom of the separation vessel (

Description

PROCESS TO COOL DISPERSIONS AND LIQUIDS The invention relates to a process for cooling dispersions and liquids, which are first deodorized in a container. The preparation of the polymer dispersions by suspension polymerization or emulsion polymerization is known. The products usually still contain undesirable volatile organic compounds such as residual monomers resulting from incomplete reaction, impurities of the starting materials, decomposition products of the initiators or low molecular weight products of the side reactions. These compounds are referred to hereafter by the collective term "residual volatiles". In decision 96/13 / EC of the commission regarding the definition of environmental criteria for publishing the environmental symbol EC for interior paints and coatings on December 5, 1995, these residual volatiles are divided into volatile organic compounds (VOCs) ) and volatile aromatic hydrocarbons. In both cases these organic compounds have a boiling point (or initial boiling point) not exceeding 250 ° C under conditions of atmospheric pressure. The volatile aromatic hydrocarbons in this context have at least one aromatic nucleus in their structural formulas. The collective term "residual volatiles" as used herein refers to all these organic compounds having a boiling point (or initial boiling point) not greater than 250 ° C. Residual volatiles may be present not only in the dispersions but also in the liquids. For example, when a dispersion formed by emulsion polymerization is broken by means of an electrolyte or acid, at least some of the residual volatiles remain in the liquid that is separated from the polymer. Residual volatiles can present problems related to the environmentally compatible waste of these liquids. In addition, residual volatiles are undesirable for multiple applications of dispersions or suspensions, for example, in the food or cosmetics sector or for indoor applications, and what is involved is the substantially complete elimination of these. Dispersions or liquids are therefore the object of a treatment that eliminates residual volatiles. This treatment is known as deodorization. Various methods and apparatus are known for this purpose: in addition to the chemical processes, which normally, however, only affect the unsaturated compounds, these are predominantly depuration processes in which the entrainment gas is passed through the suspension or dispersion. The entrained gases used are air, nitrogen, super critical carbon dioxide, ozone or steam. Devices in which the suspension or dispersion is treated with the entrained gas can take various forms. In the simplest design, the apparatus comprises a container that maintains the suspension or dispersion and in which the entrainment gas is introduced by means of lances (hose) or valves in the lower part of the container. In accordance with the international standard of DRAFT ISO / DIS 13741, part 1, the level of residual volatiles in this context is measured by means of gas chromatography. In this standard, these are mentioned as residual monomers and other organic components. The examples mentioned include acrylic esters such as n-butyl acrylate and isobutyl acrylate, methacrylic esters such as methyl methacrylate, acrylonitrile, butadiene, styrene, vinyl acetate, vinyl chloride, but also by-products, for example, acetaldehyde and ethylbenzene. Also mentioned is propionitrile, ethyl acrylate and 4-vinylcyclohexene. The degree of deodorization desired, the perfection with which residual volatiles are removed, will depend on the application and quality or environmental compatibility of the dispersions or liquids in question. These dispersions and liquids that are preferred for the purposes are mentioned below.

Liquids The liquids used in the process according to the invention can be any liquid having a removable level of residual volatiles. Preferably, solutions or aqueous liquids having a high viscosity are used. Examples of these liquids include solutions resulting from suspension polymerization or emulsion polymerization after the polymer has been separated, viscous liquids such as paraffinic waxes of relatively long chain or glycols containing undesirable volatile components, in particular if These serve as solvents. Other examples include polymer solutions, especially aqueous polymer solutions. These, having been prepared in the relevant solvent, often still contain residual monomers and other components that can be removed by deodorization.

Dispersions The dispersions that can be used in the novel process can be any dispersion containing removable levels of residual volatiles. Examples of these dispersions can be dispersions of contaminated soils, dispersions of inorganic particles, dispersions of biological molecules and, preferably, dispersions of organic compounds, especially polymer dispersions, with aqueous dispersions being preferred. The aqueous polymer dispersions preferably suitable for the process according to the invention are the fluid systems which, like the phase dispersed in the diffuse dispersion medium, contain polymer particles in a stable dispersed distribution. The diameter of the polymer particles is generally in the range of 0.01 to 5 μ, often mainly in the range of 0.01 to 1 μ. The stability of the dispersion distribution often extends over a period of at least one month, in many cases even over a period of at least 6 months. Like the polymer solutions, when the solvent is evaporated, the aqueous polymer dispersions have the tendency, when the aqueous dispersing medium is being evaporated, to form polymeric films, which is the reason why the aqueous polymer dispersions are applied in the polymeric dispersions. a variety of forms as binders, for example, for paints or compounds for coating leather or skin.

In principle, a difference can be made, with the aqueous polymer dispersions, between aqueous secondary dispersions and aqueous primary dispersions. Aqueous secondary dispersions are those, in the course of which preparation the polymer is produced outside the aqueous dispersion medium, for example, in solution of a suitable non-aqueous solvent. This solution is then transferred to the aqueous dispersion medium and the solvent, while the dispersion is carried out, is separated, as a rule by distillation. In contrast, aqueous primary dispersions are those in which the polymer is produced directly in a dispersed distribution in the aqueous dispersion medium itself. All preparation processes essentially have in common that the conformation and the polymer includes the use, exclusively or together with other materials, of monomers having at least one ethylenically unsaturated group the incorporation of these monomers having at least one ethylenically unsaturated group per the common is carried out by initiated polymerization, the nature of the initiation being determined, in particular, by the desired performance characteristics of the target product and consequently designed for these. Possible examples are ionic and free radical initiation. However, the incorporation can also be carried out by reaction of the catalytically initiated polymer-analog. Initiation by free radicals is used with particular frequency, and therefore the incorporation of the monomers containing ethylenically unsaturated groups is generally carried out by aqueous free-radical emulsion polymerization in the case of primary aqueous dispersions and by polymerization in the case of aqueous primary dispersions. free radical solution in the case of aqueous secondary dispersions. The polymerization conditions are chosen so that the desired characteristics of the polymer can be achieved as molecular weight, molecular weight distribution and degree of branching. If the objective is rapid reaction, it is not advisable, as a general rule, to carry out the reaction to its end. The aqueous polymer dispersions obtained after the reaction, therefore, will normally still contain monomers, especially ethylenically unsaturated ones. Due to the increased reactivity of the ethylenically unsaturated double bonds, these residual monomers, such as acrylonitrile and vinyl acetate, are not completely safe from the toxicological point of view and therefore must be removed from the dispersion. This purpose is carried out through the process of the present. The process can be used for any of the polymers dispersed in an aqueous medium, regardless of the type of polymer. The term "polymer" therefore comprises, in the context of the present invention, polycondensates such as polyesters, poly-adducts such as polyurethanes and polymers accessible by ionic polymerization or by free radicals. Mixed versions of the syntheses in the same manner produce dispersions that can be used according to the invention, such as copolymers. The preparation of the aqueous polymer dispersions of the different types of polymers mentioned above is known, for example, from Encyclopedia of Polymer Science and Engineering, volume 8, p. 659 et seq (1987); D. C Blackley, in High Polymer Latices, volume 1 p. 35 et seq. (1966); H. arson, the Application of Synthetic Resin Emulsions, page 246 et seq., Chapter 5 (1972); [Publisher?] D. Diederich, Che ie in unserer Zeit, 24, pp. 135 to 142 (1990); Emulsion Polymerization, Interscience Publishers, New York (1965); DE-A 40 03 422 and Dispersionen synthetischer Hochpolumerer, F. Hdlscher, Springer-Verlag, Berlin (1969). The monomers having at least one monoethylenically unsaturated group, which are suitable for the novel process, among others include, in particular, monomers which in themselves give rise to the direct polymerization by free radicals, such as the definitions, for example, ethylene, vinyl aromatic monomers such as styrene α-methylstyrene, o-chlorostyrene or vinyl toluenes, vinyl alcohol esters and monocarboxylic acids having 1 to 18 carbon atoms, such as vinyl acetate, vinyl propionate, n-butyrate vinyl, vinyl laurate, vinyl divalate and vinyl stearate, and the monomers that are commercially available VEOVA 9 to 11 (VEOVA is a trademark of Shell and means vinyl esters of carboxylic acids which are also known as Versatic® X acids), esters of the ct, β-monoethylenically unsaturated mono- and dicarboxylic acids preferably having 3 to 6 carbon atoms; bonus, such as acrylic acid, methacrylic acid, maleic acid, fumaric acid and itaconic acid, wherein the albandes generally have from 1 to 12, preferably from 1 to 8 and especially from 1 to 4 carbon atoms. Such as methyl, ethyl, n-butyl, isobutyl, t-butyl and 2-ethylhexyl esters of acrylic acid and methacrylic acid, dimethyl maleate or n-butyl maleate, nitriles of ct, β-monoethylenically unsaturated carboxylic acids such as acryl nitrile and conjugated C4-8 dienes such as 1,3-butadiene and isoprene. In the case of the marked polymer dispersions produced exclusively by the free radical aqueous emulsion polymerization method, these monomers, as a rule, form the main monomers which, based on the total amount of the monomers to be polymerized by the aqueous process [lacuna] by free radicals usually make up a fraction of more than 50% by weight. In general, these monomers are only moderately to sparingly soluble in water under normal conditions (25 ° C, 1 atm). Examples of the monomers are only moderately to sparingly soluble in water under normal conditions (25 ° C, 1 atm). Examples of the monomers whose solubility in water under the aforementioned conditions is higher include the α, β-monoethylenically unsaturated mono- and dicarboxylic acids and their amides, such as acrylic acid, methacrylic acid, maleic acid, fumaric acid, acid itaconic, acrylamide and methacrylamide, as well as vinylsulfonic acid and its water soluble salts and N-vinylpyrrolidone. In the case of aqueous polymer dispersions produced exclusively by aqueous free radical emulsion polymerization, the aforementioned monomers having increased water solubility are usually copolymerized only as modifying monomers in amounts, based on the total amount of the monomers that are they will polymerize, less than 50% by weight, as a general rule from 0.5 to 20, preferably from 1 to 10% by weight.

Monomers that usually increase the internal strength of the films formed of the aqueous polymer dispersions generally have at least one epoxy, hydroxyl, N-methylol, carbonyl double bond or at least two ethylenically unsaturated conjugated double bonds. Suitable examples of these are N-alkylamides of carboxylic, β-monoethylenically unsaturated acids having from 3 to 10 carbon atoms and the esters of these with alkenols having from 1 to 4 carbon atoms, among which N-methylol acrylamide and N-methylolmethacrylamide are particularly preferred, monomers containing two vinyl radicals, vinyls containing two vinylidene radicals and monomers containing two alkenyl radicals. Particularly advantageous in this context are the diesters of the dihydric alcohols with α, β-monoethylenically unsaturated monocarboxylic acids, among which acrylic and methacrylic acid are preferred, examples of their monomers containing two ethylenically unsaturated, non-conjugated double bonds are alkylene glycol diacrylates and dimethacrylates such as ethylene glycol diacrylate, 1,3-butylene glycol diacrylate, 1,4-butylene glycol diacrylates and propylene glycol diacrylate, divinyl benzene, vinyl methacrylate, vinyl acrylate, allyl methacrylate, allyl acrylate, • diallyl maleate, diallyl fumarate, methylene bis acrylamide, cyclopentadienyl acrylate or triallyl cyanurate. Of particular importance in this context are also the hydroxyalkyl esters of Ci-Cs of the acid methacrylic and acrylic acid, as can be acrylate and methacrylate n-hydroxyethyl, n-hydroxypropyl or n-hydroxybutyl acrylate and the compounds as diacetone acrylamide and acetylacetoxyethyl acrylate and methacrylate, ureidoethyl methacrylate and acrylamidoglycolic acid. In the case of aqueous polymer dispersions produced exclusively by the free radical aqueous emulsion polymerization method, the aforementioned monomers are usually copolymerized in amounts from 0.5 to 10% by weight, based on the total amount of the monomers that are will polymerize. In the course of polymerization in aqueous emulsion by free radicals it is common to include dispersants that guarantee the stability of the aqueous polymer dispersion produced. The dispersants that can be considered include emulsifiers as well as the protective colloids that are normally used to carry out the polymerizations in aqueous emulsion by free radicals. Suitable protective colloids are, for example, polyvinyl alcohols, cellulose derivatives or copolymers containing vinylpyrrolidone. A detailed description of other suitable protective colloids is found in Houben eyl, Methoden der organischen Chemie, Volume XIV / 1, Makro-molekulare Stoffe [Macromolecular Substances], Georg-Thieme-Verlag, Stuttgart, 1969, p. 411 to 420. Of course, it is also possible to use mixtures of emulsifiers and / or protective colloids. The dispersants which are used preferably are exclusively emulsifiers whose relative molecular weights, in contrast to the protective colloids, are usually below 1000. These may be anionic, cationic or non-ionic. If mixtures of active surface substances are used, the individual components must, of course, be compatible with each other, which can be verified with some preliminary experiments if there is doubt. In general, anionic emulsifiers are compatible with each other and with nonionic emulsifiers. The same applies to cationic emulsifiers, since anionic and cationic emulsifiers are usually mutually incompatible. Examples of common emulsifiers are mono-, di- and trialkylphenols ethoxylated (EO units: 3 to 100, alkyl: C4 to C12), ethoxylated fatty alcohols (EO units: 3 to 100, alkyl: Cs to Cis) , alkali metal salts and ammonium salts of alkyl sulphates (alkyl: Cs to Cie) of semi esters • sulfuric acid etiloxilados alkylphenols (EO units: 3 to 100, alkyl: C4 to C12), of alkylsulfonic acids (alkyl: C12 to CIE) and alkyl aryl sulfonic acids (alkyl: C9 to CIE) - Other emulsifiers 5 Suitable as sulfosuccinic esters are found in Houben-Weyl, Methoden der organischen Chemie, Volume XIV / 1, Makro-molekulare Stoffe, Georg-Thieme-Verlag, Stuttgart, 1961, pp.192-208. As a rule, the amount of dispersant that is used is from 0.5 to 6, preferably from 1 to 3%, based on the weight of the monomers that are subjected to free radical polymerization. Of course, the aforementioned dispersants are very generally suitable for stabilizing the products of the process according to the invention. The products of the novel process also include, however, aqueous polymer dispersions of self-emulsifying polymers, that is, polymers having ionic groups which, due to the repulsion of the same sign charges, are capable of effecting stabilization. Preferably, the direct products of the novel process exhibit anionic stabilization (in particular anionic dispersants).

Definition and determination of the relief-bes quantities that must be measured. Glass transition temperature The glass transition temperature is preferably determined from the temperature dependence of the specific heat in a differential thermal analysis (G.

Goldbach in: Kunstostoffe, Ordnungszustande Encyklopádie der technischen Chemie, Volume 15, pp. 219 to 222, inheim, 1980). The transition temperature of the glass of the copolymers can also be calculated from the glass transition temperatures of the particular homopolymers, weighted according to the fraction of the mass of the monomers and the coefficient of expansion of the polymers.

Minimum Film Formation Temperature The minimum temperature for polymer film formation is the lowest temperature at which a dispersion still forms a coherent film after the water has evaporated. This temperature is close to the glass transition temperature of the polymer (H. Gerrens in: Polymerisationstechnik [Polymerization technology] in: Ullmanns Encyklopadie der technischen Chemie, volume 29 p, 141, Weinheim, 1989).

The measuring instrument used is a metal plate to which a temperature gradient is adjusted. What is observed is that temperature the film begins to present fissures (E. Penzel in: Polacryl-und Polymethacryl-Verbnindugen [Polyacrylic and polymethacrylic compounds] in: Ullmanns Encyklopadie der technischen Chemie, Volume 19, pp. 17 to 18, Weinheim, 1980). The glass transition temperature of the acrylates that are preferably used as the dispersion in the novel process is between -62 and + 6 ° C (see table 8 of E. Penzel in: Polacryl-und Polymethacryl-Vernindugen [polyacrylic and polymethacrylic compounds] in: Ullmanns Encyklopadie der technischen Chemie, Volume 19, pp. 17-18, Weinheim, 1980). The resulting minimum temperatures for film formation of the polymers in the dispersions are, therefore, often much lower than the preferred temperature at which the process according to the invention operates. The dispersions that are to be treated, therefore, tend to be soft at the process temperature and easily form films.

Viscosity Dispersions have a wide range in rheological behavior. The behavior of the flow depends on the content of the solids, the particle size, the particle size distribution and the system of the auxiliaries that were used during the preparation. The anomalies commonly observed in flow behavior include pseudo-plasticity and dilatation. Viscosity is measured under standardized measurement conditions in capillary viscometers, Couette viscometers and cone and plate viscometers (C. Gerth: Rheometrie corCouette and cone and plate viscometers (C. Gerth: Rheometrie [Rheometry], Ullmans Encyklopadie der technischen Chemie, volume 19, pp. 17 to 18, Weinheim 1980).

Aqueous polymer dispersions are generally very good film formers and have a tendency to form a layer at the polymerization temperature. Because of this they have to be cooled down to 35 ° C for storage and transport. These dispersions contain from 30 to 80% water and therefore have a high thermal capacity, which is usually above 3 kJ / kg K. Depending on the application, they have a viscosity from about 20 mPas to 10 Pas. The cooling of this dispersion therefore requires that large amounts of heat be dissipated. With low viscosity dispersions having a viscosity less than 100 mPas, cooling, as a rule, does not present problems. These dispersions can be cooled by means of a jacket while they are still contained in the container where they were prepared, or otherwise while the product is transferred to a container for standardization or storage tank. This purpose is served by the heat transfer units by means of which the dispersions are brought to the desired temperature. However, for dispersions that have higher viscosities this indirect heat dissipation is not convenient, since the heat transfer coefficient hw can fall below 100 W / m K. This results in correspondingly large heat transfer areas or very long cooling times. Since the entaltia of water evaporation, at 2260 KJ / kg, is very high, it can be used to cool dispersions. For this purpose, the dispersion is introduced into a partial vacuum which is low at the partial pressure of the water. The water evaporates and the dispersion cools in the process, while increasing its concentration at some percentage, which is generally a desirable side effect. This increase in concentration is also used in a manner known as the main effect, by the dispersion cyclically heated and depressurized in a partial vacuum until the desired solids content is reached (US-3, 073, 380). Physical deodorization by steam distillation often makes use of an apparatus known as a batch scrubber. One embodiment and the corresponding process are described in DE-A-1 248 943. In the process the dispersion or liquid after the deodorization step, depending on the characteristics of the product will be between approximately 60 and 90 ° C. This dispersion or liquid can then be cooled by a "subsequent process" (allowing the rest or by agitation under reduced pressure without introducing steam). However, in practice serious device failures will occur if dispersions containing polymers are used. The dispersion forms thin films and layers that build up to form a wall covering that eventually detaches and can block the apparatus. This gives rise to frequent and laborious cleaning operations and in consequence to production losses. These problems will also occur when carried out in cooling by means of a jacket bath. In addition, especially where the dispersions or viscous liquids are cooled by means of a jacket bath, the cooling times are very long. The economic viability of the aforementioned process is carried out for the duration of the cooling operation and, in the case of the specific dispersions used, also for the degree of concomitant failure of the apparatus. An object of the present invention is to improve the deodorization process described above in such a way that: 1. The cooling time of the dispersion or the liquid after the deodorization is reduced, 2. In the case of dispersions containing polymer during the cooling does not take place the formation of a thin layer or film which causes faults and / or blocking of the apparatus, 3. At the same time, the complexity of the apparatus is reduced to a minimum. The objective is achieved by a process to cool dispersions or liquids after deodorization by means of: a) passing vapor through the dispersion or liquid to be cooled or held in a container, causing the dispersion or liquid to form foam as a result, b) discharge the foam from the upper section of the container through a nozzle to a vacuum separation vessel, breaking the foam in the process, c) the water vapor formed from the foam condenses in an exchanger heat and volatile organic components are removed at the same time, and d) the broken foam is returned to the container, steps a) to d) are carried out until the dispersion or liquid has been deodorized to the desired degree. What defines the process according to the invention is that, after finishing the deodorization (according to steps a) ad)), the dispersion or hot liquid is discharged from the lower section of the container through the nozzle towards the vacuum separation vessel, so that the dispersion or the liquid is cooled, the nozzle and the vacuum separation vessel is also used in advance to perform step b), that the water vapor maintained in the separation vessel is condenses in the heat exchanger that was also used beforehand in step c), and that the cooled dispersion or liquid is discharged from the bottom of the separation vessel. Surprisingly we have found that the feeding nozzle used for the vacuum separation vessel is suitable for two different applications: first application: breaking the foam (due to the sudden pressure difference) during the deodorization, and second application: the cooling the dispersion or deodorized liquid during transfer to the vacuum separation vessel. Consequently, it is possible that not only the nozzle, but also the larger part of the apparatus, specifically the vacuum separation vessel, the heat exchanger and the pump, are used for the deodorization process for the cooling process. As a result, the complexity of the apparatus is reduced and the efficiency of the process is improved. According to an advantageous embodiment of the invention, the hot dispersion is pumped from the container by means of a pump and is passed to an elevator for the separation container. In the process, the separation vessel is advantageously emptied from 30 to 100 mbar absolute, preferably 50 mbar absolute. The foam that is collected in the lower part of the separator is sent to a product tank by means of a pump. The water vapor formed from the dispersion is condensed in a heat transfer unit. The vacuum in the separation vessel is preferably generated by means of a two-stage water pump. The polymer dispersions are generally cooled below 35 ° C, to counteract the subsequent formation of the film in the container 7. Preferably, the process employs dispersions or high viscosity liquids. Other details and advantages of the invention can be obtained from the specific embodiment shown in the drawing. In this, the dispersion or hot liquid after the deodorization is pumped from the container 1 by means of a pump 2 and is passed through the elevator 3 through the nozzle 5 towards the separation vessel 4 which has been evacuated to 50 mbar (corresponding to 33 ° C). The dispersion or cooled liquid is collected in the lower part of the separator 4, from where it is sent by means of the pump 6 to a container 7 for the finished product. The water vapor formed from the dispersion or liquid is condensed in a heat exchanger 8 and recycled. The necessary vacuum is generated by means of a two-stage water ring pump 9.

Claims (6)

2. . A process for cooling dispersions or liquids after deodorization by means of: a) a stream that passes through the dispersion or liquid to be cooled and maintained in a container (1), causing the dispersion or liquid to foam as a result, b) the foam that is discharged from the upper section of the container through the nozzle (5) into a vacuum separation vessel (4) breaking the foam in the process, c) the water vapor formed from the foam is condensed in a heat exchanger (8) and the volatile organic components are removed at the same time, and d) the broken foam returns to the container (1), steps a) ad) are made until the dispersion or liquid has been deodorized to the desired degree. Where, after the end of the deodorization (according to steps a) ad)), the dispersion or hot liquid is discharged from the lower section of the container (1) through the nozzle (5) to the separation vessel evacuated (4), so that the dispersion or the liquid is cooled, the nozzle (5) and the vacuum separation vessel (4) are also used in advance to perform step b), wherein the water vapor maintained in the separation vessel (4) is condensed in the heat exchanger (8) which also used in advance in step c), and in which the dispersion or cooled liquid is discharged from the bottom of the separation vessel (4) . 2. The process as claimed in claim 1, wherein the dispersion or hot liquid is pumped from the container (1) by means of a pump (2) and passed to the separation vessel (4) in an elevator.
3. 3. The process as claimed in claim 2, wherein the separation vessel (4) is evacuated from 30 to 100 mbar absolute, preferably 50 mbar absolute.
4. 4. The process as claimed in any of claims 1 to 3, wherein the vacuum is generated by means of the two-stage water ring pump (9). The process as claimed in any of claims 1 to 4, wherein the vapor of the lower section of the container (1) is introduced into the dispersion or liquid. The process as claimed in any of claims 1 to 5, wherein the cooled dispersion is sent, by means of a pump (6) to a container (7) for the finished product. The process as claimed in any of claims 1 to 6, wherein dispersions or liquids of high viscosity are used. SUMMARY OF THE INVENTION The present invention relates to a process for cooling dispersions or liquids after a deodorization 5 by means of: a) passing steam through the dispersion or liquid to be cooled and maintained in a container, causing the dispersion of liquid form foam as a result, b) discharge the foam from the upper section of the container through a nozzle to an evacuated separation vessel by breaking the foam in the process, c) condensing the water vapor formed from the foam in a recycle exchanger. heat and remove the organic components 15 volatile at the same time, and fr d) return the dissolved or broken foam to the container, steps a) to d) are carried out until the dispersion or liquid has been deodorized to the desired degree, where, after completing the deodorization ( in accordance with 20 steps a) to d)), the hot dispersion or liquid is discharged from the lower section of the container through the nozzle to the evacuated separation vessel, so that the dispersion or liquid cools, the nozzle and the container of proper separation is also 25 use in advance to perform step b), wherein the water vapor that is maintained in the separation vessel is condensed in the heat exchanger which was also used in advance in step c), and where the dispersion or Cooled liquid is discharged from the bottom of the separation vessel.