DE4304062A1 - Process for the preparation of surfactant granules - Google Patents

Abstract

During the production of anionic surfactant-containing granulates having more than 450 g/l apparent weight by granulation of a surfactant preparation composition containing a non-surfactant liquid component, the water required and thus the energy required to evaporate the water may be reduced by separately applying a gaseous medium to the anionic surfactant in its acid form or to a mixture which contains one or several anionic surfactants in their acid form, and to an aqueous alkaline solution, which are then sprayed together or separately in almost stoichiometric amounts under a high propellant gas pressure in the granulating and drying chamber, where they are granulated and at the same time dried, if required with the admixture of one or several inorganic or organic solids.

Description

"Process for the Production of Surfactant Granules"

The invention relates to a method for transferring liquid to pasty These forms of preparation of detergent compounds active in washing and cleaning in storage-stable and dust-free granules with increased bulk density.

Surfactant granules can, for example, by conventional drying technology of surfactant-containing solutions and pastes, especially in the spray tower, getting produced. For example, in the European patent message 319 819 a process for the production of surfactant granules Spray drying discloses a sulfonic acid and a highly concentrated trated aqueous sodium hydroxide separately with a gaseous medium strikes, then merged in stoichiometric amounts, in egg ner multi-component nozzle neutralized and at a high propellant pressure in the Drying tower is sprayed. The products obtained are solid or pasty, with solid products mostly being relatively dusty, one relatively high water content and a low bulk density Zen.

Granu is an alternative to spray drying surfactant pastes The European patent application EP 403 148 describes this Process for the preparation of fatty alcohol sulfate granules in cold Water are dispersible. It becomes a highly concentrated aqueous Fatty alcohol sulfate paste containing less than 14% water and less than Contains 20% by weight of other additives at temperatures between 10 and 45 ° C mechanically processed until granules are formed. In this way are obtained fatty alcohol sulfate granules, which are already in washing temperatures between 4 and 30 ° C are dispersed; the one to be followed Process temperature and the relatively low maximum water content of the However, surfactant paste are critical process parameters  does not disclose the bulk densities produced by this process have granules.

European patent application EP 402 112 describes a method for Production of fatty alcohol sulfate and / or alkylbenzenesulfonate granules known, the neutralization of the anionic surfactants in acid form to a Paste with a maximum of 12% by weight of water with the addition of auxiliaries such as Polyethylene glycols, ethoxylated alcohols or alkylphenols, which have a melting point above 48 ° C, and the granulation in one high-speed mixer takes place. Again, the what to be followed quantity is a critical process parameter reveals which bulk weights obtained by this method Have surfactant granules.

From the European patent application EP 402 111 a method for Production of detergent granules with active washing and cleaning properties Bulk density between 500 and 1200 g / l is known, a surfactant Form of preparation that contains water as a liquid component and in addition can contain organic polymers and builder substances with a fine Partial solid and added gra in a high-speed mixer is canceled. Here, too, the water content of the surfactant paste is a problem critical process parameters. If the water content of the surfactant paste is too high, the solid is dispersed so that it no more than Deagglomeration agent can act. If the solids content exceeds On the other hand, a certain value, the mass does not have that for the Granulation necessary consistency.

In the older, unpublished German patent application P 41 27 323.0 becomes a process for the production of washing and cleaning active Surfactant granules with a bulk density above 500 g / l through granules tion of a surfactant formulation that is a non-surfactant liquid Component has been described, wherein a surfactant preparation form, the under normal pressure at temperatures between 20 and 40 ° C in liquid to pasty form is present, if desired with the addition of an anorga African or organic solid granulated and dried at the same time is not. This granulation and simultaneous drying takes place  preferably in a fluidized bed (fluidized bed granulation) instead. The In addition to the surfactants, the surfactant preparation form used also contains one non-surfactant liquid component, which is preferably water or a represents aqueous solution. In contrast to ge called prior art the content of a non-surfactant liquid component is not a critical process parameter. On the contrary, Formulations containing anionic surfactants are usually produced by Neutra lization of the anionic surfactants in their acid form with concentrated aqueous made alkaline solutions. So such a form of preparation however, at 20 to 40 ° C in liquid to pasty form, the Mixture should generally be diluted with water. Here is the high one Energy consumption required to remove the water, however, as to look at disadvantageously.

The object of the invention was to provide the method mentioned To further develop granulation and simultaneous drying, that the energy required for drying can be reduced.

The invention accordingly relates to a process for the production wash and cleaning active surfactant granules with a bulk density above 500 g / l by granulating a surfactant preparation form has a non-surfactant liquid component, the anionic surfactant preparation form is prepared such that the Anionic surfactant in its acid form or a mixture which one or more rere contains anionic surfactants in their acid form, and an aqueous alka mixed solution separately with a gaseous medium finally separated or combined in almost stoichiometric amounts leads to a high propellant pressure in the granulating and drying room are sprayed and the subsequent granulation if desired Addition of one or more inorganic or organic solids and is carried out with simultaneous drying.

The preparation of the anionic surfactant preparation form can be invented according to the invention either directly after the introduction of the individual reactants flows into the granulation and drying room or before. It should be noted in the latter case that the distance of the location of the  Merging of the gas-charged reactant streams from the spraying unit direction of the process conditions and the material used Stemen is dependent, but is preferably kept as small as possible to a clogging of the nozzle due to the early start of neutralization to avoid actions. In a preferred embodiment of the invention is therefore the anionic surfactant in its acid form or the mixture containing a or contains several anionic surfactants in their acid form, with a gas acted medium and through a multi-component nozzle, for example sprayed into the granulating and drying room via a two-component nozzle. Likewise, an aqueous alkaline solution with a gaseous medium acted upon and at the same time with the anionic surfactant in its acid form or the mixture containing one or more anionic surfactants in their acid form contains, in almost stoichiometric amounts via another multi-component Sprayed nozzle into the granulating and drying room. In this case it takes place the neutralization and thus the production of the anionic surfactants directly in the granulating and drying room. In the context of this invention be "almost stoichiometric amounts" indicate that the ratio of the number acidic groups to alkaline groups preferably in the range of 1.1: 1 to 0.8: 1 and in particular from 1: 1 to 0.9: 1.

In a further and particularly preferred embodiment, the Invention, however, before that separated with a gaseous medium applied acidic and alkaline reactant streams over a single Multi-substance nozzle, for example via a 3-substance nozzle, brought together and be sprayed into the granulating and drying room. In this case, he the neutralization follows essentially in the nozzle or directly when exiting the nozzle. Of course, it is also possible that the combined acidic and alkaline reactant streams over several Multi-substance nozzles are sprayed into the granulating and drying room. This is particularly preferred when products are made of different types Anionic surfactants manufactured and thus different, merged acidic and alkaline reactant streams are to be sprayed.

In practicing the method of the invention, the Starting materials, for example, using piston pumps almost dosed stoichiometrically into one or two not further modified  commercially available nozzle (s) or one or two spray tube (s) introduced. Un The gaseous medium is mixed in indirectly in front of the nozzle (Propellant). In the case of spraying the combined reactants this means that the admixing of the gaseous medium into the Reactant flows before they meet in front of or in the nozzle. Further technical details on the implementation of the process at for example regarding the control of the reaction temperature, the currents rate of reactant flow or pressure at which the Reaction mixture is sprayed into the granulating and drying room, can be found in European patent application 319 819.

The anionic surfactants in their acid form can be carboxylic acids, sulfuric acid half ester and sulfonic acids, preferably fatty acids, alkylarylsulfonic acid ren, α-sulfofatty acid esters and the sulfuric acid semiesters of alkoxylated, especially ethoxylated fatty alcohols and / or the sul succinic acid can be used. In the broadest sense, fat can also acid esters, in particular fatty acid methyl esters, are used, wherein in in this case not a neutralization reaction, but a saponification of the Ester group is carried out.

Suitable anionic surfactants in their acid form are therefore in particular either an anionic surfactant in its acid form or a mixture of the group of anionic surfactants in their acid form, optionally in combination with nonionic, amphoteric and / or cationic surfactants. Preferred anionic surfactants in their acid form are C ₈ -C ₂₂ alkylsulfonic acids, C ₉ -C ₁₃ alkylbenzenesulfonic acids, usually called dodecylbenzenesulfonic acid, and methyl α-sulfofatty acid in their acid form. Particularly preferred alkyl sulfonic acids are the sulfuric acid monoesters from primary alcohols of natural and synthetic origin, in particular from fatty alcohols, e.g. B. from coconut fatty alcohols, tallow fatty alcohols, oleyl alcohol, lauryl, myristyl, palmityl or stearyl alcohol, or the C ₁₀ -C ₂₀ oxo alcohols, and those secondary alcohols of this chain length. The sulfuric acid monoesters of alcohols ethoxylated with 1 to 6 moles of ethylene oxide, such as 2-methyl-branched C ₉ -C ₁₁ alcohols with an average of 3.5 moles of ethylene oxide, are also suitable. In particular, according to the process according to the invention, esters of α-sulfofatty acids (ester sulfonic acids) which, by α-sulfonation of the methyl esters of fatty acids of plant and / or animal origin with 10 to 20 C atoms in the fatty acid molecule, for example the α-sulfonated methyl esters hydrogenated coconut, palm kernel or tallow fatty acids, and the α-sulfo fatty acids (diacids) obtainable by ester cleavage. The use of mixtures of the monoacids and diacids with other anionic surfactants in their acid form, for example with alkylbenzenesulfonic acids and / or fatty alkylsulfonic acids, is also preferred.

Also suitable are alkanesulfonic acids which can be obtained from C ₁₂ -C ₁₈ alkanes by sulfochlorination or sulfoxidation.

Preferred nonionic surfactants are derived from liquid alkoxylated, advantageously ethoxylated, in particular primary alcohols having preferably 9 to 18 carbon atoms and an average of 1 to 12 moles of ethylene oxide per mole of alcohol, in which the alcohol radical can be linear or methyl-branched in the 2-position , or can contain linear and methyl-branched residues in the mixture, as are usually present in oxo alcohol residues. In particular, however, linear residues of alcohols of native origin with 12 to 18 carbon atoms are preferred, such as. B. from coconut, tallow or oleyl alcohol. The degrees of ethoxylation given represent statistical averages, which can be an integer or a fraction for a specific product. Preferred alcohol ethoxylates have a narrow homolog distribution (narrow range ethoxylates, nre). In particular, alcohol ethoxylates are preferred which have an average of 2 to 8 ethylene oxide groups. The preferred ethoxylated alcohols include, for example, C ₉ -C ₁₁ oxo alcohol with 7 EO, C ₁₃ -C ₁₅ oxo alcohol with 3 EO, 5 EO or 7 EO and in particular C ₁₂ -C ₁₄ alcohol with 3 EO or 4 EO, C ₁₂ -C ₁₈ alcohols with 3 EO, 5 EO or 7 EO and mixtures thereof, such as mixtures of C ₁₂ -C ₁₄ alcohol with 3 EO and C ₁₂ -C ₁₈ alcohol with 5 EO. Furthermore, nonionic surfactants which can be used are alkyl glycosides of the general formula RO- (G) x, in which R is a primary straight-chain or aliphatic radical with 8 to 22, preferably 12 to 18, carbon atoms branched in the 2-position, G is a symbol which represents a glycose unit with 5 or 6 carbon atoms, and the degree of oligomerization x is between 1 and 10, preferably between 1 and 2 and in particular is significantly less than 1.4.

The surfactant preparation form can contain additives, which are preferably ingredients of washing and cleaning agents, contain. In particular, surfactant Preparations used, the additives in amounts from 0.001 to 15 % By weight, based on the surfactant preparation form. Especially be preferred additives are colorants, foam inhibitors, bleaches and / or solubility enhancing ingredients.

Suitable dyes are temperature-stable dyes, preferably pig ment dyes, which are advantageously in amounts of 0.001 to 0.5 % By weight, based on the surfactant preparation form, are used.

Suitable foam inhibitors are, for example, soaps of natural and synthetic origin, which have a high proportion of C ₁₈ -C ₂₄ fatty acids. Suitable non-surfactant-like foam inhibitors are organopolysiloxanes and their mixtures with microfine, optionally silanized silica, paraffins, waxes, microcrystalline waxes and their mixtures with silanized silica or bistearylethylenediamide. Bisacylamides derived from C ₁₂ -C ₂₀ alkylamines and C ₂ -C ₆ dicarboxylic acids can also be used. Mixtures of different foam inhibitors are also advantageously used, e.g. B. from silicone and paraffins or waxes. The foam inhibitors are preferably bound to a granular, water-soluble or dispersible carrier substance. The foam inhibitor content of the surfactant preparation is preferably 0.01 to 0.5% by weight.

Of the compounds used as bleaching agents and providing H ₂ O ₂ in water, sodium perborate tetrahydrate and sodium perborate monohydrate are of particular importance. Other bleaching agents that can be used are, for example, peroxy carbonate, peroxypyrophosphates, citrate perhydrates, peroxophthalates, diperazelaic acid or diperdodecanedioic acid. In particular, it is also preferred to use hydrogen peroxide as a bleaching agent in surfactant preparation forms which are used according to the invention. The content of bleach in the surfactant preparation form is preferably 0.5 to 15% by weight, in particular the content of hydrogen peroxide is 0.5 to 5% by weight.

The constituents which improve the solubility include liquid, pasty and solid compounds which are soluble or dispersible in the other constituents of the Ten sid preparation form. Preferred solubility-improving constituents are polyethylene glycols with a relative molecular weight between 200 and 20,000 and highly ethoxylated fatty alcohols with 14 to 80 ethylene oxide groups per mole of alcohol, in particular C ₁₂ -C ₁₈ fatty alcohols with 20 to 60 ethylene oxide groups, for example tallow fatty alcohol with 30 EO or 40 EO used. The use of polyethylene glycols with a relative molecular weight between 200 and 600 is particularly preferred. These polyethylene glycols are advantageously used as a separate component of the non-surfactant liquid component. The content of the surfactant preparation form in these constituents which improve the solubility of the finished granules is preferably 1 to 15% by weight and in particular 2 to 10% by weight.

The neutralization or saponification reaction is preferably carried out with con centered aqueous alkaline solutions, for example solutions of Hydroxides, carbonates or hypochlorites of sodium or potassium, ins especially with a concentrated aqueous sodium hydroxide solution and / or potassium hydroxide solution carried out, with concentrations around 45 to 55 wt .-% especially before are moving. Another dilution of the reactant streams with water is not necessary, so that the method according to the invention compared to the the older German patent application P 41 27 323.0 described procedure Ren has the advantage that smaller amounts of water in the granulation and Drying room must be removed and the energy consumption re can be reduced.

As a gaseous medium (propellant) are particularly suitable compared to Starting and end materials are inert gases such as air or nitrogen. In principle steam is also suitable, especially if one of the reak tantalum streams or the reactant streams are heated prior to the merging should be.  

The sprayed reactant streams are now granulated and simultaneously dried. Under "drying" it is partially or completely Understand the removal of the non-surfactant liquid component. If ge wishes, residual values of free, i.e. unbound water and Residual quantities of alcohol are present as long as the finished granules are are capable and not sticky. However, a content of is preferably used free water of 10 wt .-% and in particular from 0.1 to 7 wt .-%, each based on the finished granules, not exceeded.

The production of the surfactant granules can - as detailed in the older German patent application P 41 27 323.0 is described - in all Devices take place in which a granulation under simultaneous Drying can be done. Examples of these are heatable Mixers and granulators, in particular granulators of the Turbo dryer type ® (device from Vomm, Italy). In a preferred embodiment tion form, however, the invention provides that the combination of these the process steps in a batch or continuously running Fluidized bed is carried out. It is particularly preferred that Ver drive to perform continuously in the fluidized bed. It is also possible, a component of the non-surfactant liquid component, which has not been incorporated into the surfactant preparation form to be added early and separately. The nozzle or nozzles and the spray nozzle tion of the products to be sprayed can be arranged as desired. Be fluidized bed apparatuses which are preferably used have base plates with Ab measurements of at least 0.4 m. In particular, fluidized bed apparatus preferred, which is a base plate with a diameter between 0.4 and 5 m, for example 1.5 m or 2.6 m. However, they are also vertebrae Layer apparatus suitable for a base plate with a larger diameter have a diameter of more than 5 m. A perforated board is preferably used as the base plate denplatte or a Conidurplatte (commercial product from Hein & Leh mann, Federal Republic of Germany). Preferably that is Method according to the invention at swirl air speeds between 1 and 8 m / s and in particular between 1.5 and 5.5 m / s. The discharge the granules from the fluidized bed advantageously take place via a Size classification of the granules. This classification can, for example by means of a screening device or by means of an opposed air flow  (Classifier air), which is regulated so that only particles from one certain particle size removed from the fluidized bed and smaller Particles are retained in the fluidized bed. Thus, the inflowing air from the classifier air and the ground air together, whereby both either heated or unheated or one heated and the other can be unheated. In exceptional cases, cooled ground air can also be used be used. The soil air temperature is generally between - 20 and 400 ° C, preferably between 35 and 350 ° C and esp especially between 35 and 120 ° C. In a particularly preferred embodiment form the temperature of the vortex air is about 5 cm above the Base plate 10 to 120 ° C, preferably 20 to 90 ° C and especially 30 up to 85 ° C. The air outlet temperature inevitably results from the Reaction conditions. In the preferred method in the Fluid bed it is necessary that a start at the beginning of the process mass is present, which is the initial carrier for the sprayed Form of surfactant is used. In. Are particularly suitable as starting masses Detergents and cleaning agents, especially those that can also be used as solids in the process according to the invention can and have a grain size distribution, which is approximately the Grain size distribution of the finished granules corresponds. In particular is however, it is preferred to use surfactant granules as the starting mass which be have already been obtained in a previous process.

The components of the non-surfactant evaporate in the fluidized bed Partial or complete liquid component. There are dried ones to dried germs, with additional quantities of surfactant additives form coated, granulated and again dried at the same time become.

A particularly important embodiment provides that the surfactant Form of preparation with admixture of one or more inorganic or organic solids are granulated and dried at the same time, whereby the or the solid (s) pneumatically dusted via blow lines that can or can. This solid, which acts as a carrier for the tenside additive preparation form, preferably consists of ingredients of Detergents and cleaning agents. Suitable solids are, for example  also surfactants or surfactant mixtures by granulation, by spray drying or were produced by the method according to the invention and be recycled. In particular, the use of spray-dried and / or surfactant granules obtained by the process according to the invention prefers. Can advantageously be used as solids - as an alternative to incorporation into the surfactant preparation form - including highly ethoxylated fatty alcohols for example 20 to 80 EO, preferably 20 to 60 EO and in particular Tallow fatty alcohol with 30 or 40 EO can be used.

In a further preferred embodiment, as solids non-surfactant ingredients of detergents and cleaning agents preferably one or more components from the group of Alkali carbonates, alkali sulfates, crystalline and amorphous alkali silicates and layered silicates and zeolite, in particular zeolite NaA in detergent tel quality, salts of citric acid or other polycarboxylic acids, solid peroxy bleach and optionally bleach activators and solid Polyethylene glycols with a molecular weight greater than or equal to 2,000, in particular between 4000 and 20,000, used.

Finely divided materials are preferably used as solids, the either directly produced in this condition, commercially available are commercially available or by conventional grinding methods, for example by grinding with conventional mills in this finely divided state be transferred.

Preferred solids, for example, have no more than 5% by weight Particles with a diameter above 2 mm and preferably no more than 5% by weight of particles with a diameter above 1.6 mm. In particular others are preferred which are at least 90% by weight of particles with a diameter of less than 1.0 mm. Examples of this are alkali carbonates with more than 90% by weight particles with a single pass knife less than or equal to 0.5 mm and zeolite NaA powder in detergent Quality, which at least 90 wt .-% particles with a diameter contains less than 0.03 mm. The added ones are particularly advantageous Solids in amounts of 10 to 50% by weight and in particular 20 to 45  % By weight, based in each case on the sum of the surfactant preparation form and Solid, used.

In a further embodiment, the surfactant granules are claimed which can be produced by the method according to the invention. Preferred Surfactant granules have a content of 10 to 100% by weight, in particular from 30 to 90% by weight and with particular advantage between 40 and 90% by weight, each based on the finished granules, of surfactants. Pure surfactant Granules are obtained when the non-surfactant liquid component completely evaporated and the granules are thus completely dried and the optionally added solid from a pure surfactant rial exists. In this case, preference is given to surfactant granules which, according to were produced by the process according to the invention and now as a solid serve in the process according to the invention, optionally to the ge desired grain size distribution crushed and recycled. The salary of the Granules of surfactants can be set to any of the desired values bar.

The surfactant granules obtained by the process according to the invention have preferably a bulk density between 550 and 1000 g / l, in particular between 550 and 850 g / l, and are dust-free, d. H. they contain ins especially no particles with a particle size below 50 µm. Anson Most corresponds to the grain size distribution of the surfactant granules of the usual Grain size distribution of a heavy duty detergent and cleaning agent State of the art. In particular, the surfactant granules have a grain size distribution, with a maximum of 5% by weight, preferably a maximum of 3% by weight the particles have a diameter above 2.5 mm and a maximum of 5% by weight a particular advantage is a maximum of 3% by weight of the particles with a diameter below have half 0.1 mm. The surfactant granules are characterized by their light colored and characterized by their flowability. There is another one Measure to prevent sticking of the manufactured according to the invention No surfactant granules required. If desired, however, a ver be followed step, the surfactant granules for the purpose further increase the bulk density in a known manner with fine particles Materials, for example with zeolite NaA, soda, are powdered. Be preferred surfactant granules have such a regular, in particular  Approximately spherical structure that usually rounds off is not necessary and is therefore not preferred.

Examples

In Examples 1 to 3, analogously to the disclosure of EP 319 819 ABSS (C ₁₂ -alkylbenzenesulfonic acid; Example 1) and FASS (sulfuric acid half-ester of C ₁₂ -C ₁₄ -fatty alcohol; Examples 2 and 3) via a multi-substance nozzle with NaOH ( 50% by weight sodium hydroxide solution) spray-neutralized (propellant gas: nitrogen) and granulated directly in a granulation drying system (AGT) from Glatt, Federal Republic of Germany, together with a solid and dried at the same time. A surfactant granulate was used as the starting mass, which had been obtained in a previous batch (under the same process conditions) and had approximately the same composition as the finished granules of Examples 1 and 2. The process conditions can be found in Table 1.

Soda (sodium carbonate with a bulk density of 620 g / l; Commercial product from Matthes & Weber, Federal Republic of Germany) used.

Dust-free and non-sticky granules were used in both examples high surfactant content (see Table 2). The proportion of granules with a grain size above 2.5 mm was less than 5 in all examples % By weight.  

Table I

Process parameters

Table 2

Characteristics of the products

Claims (14)

1. A process for the preparation of detergent-active and granular detergents with a bulk density above 500 g / l by granulating a surfactant preparation which has a non-surfactant liquid component, characterized in that the anionic surfactant preparation is prepared in such a way that the anionic surfactant in its acid form or a mixture which contains one or more anionic surfactants in their acid form, and an aqueous alkaline solution is separately charged with a gaseous medium, then separated or combined in almost stoichiometric amounts or sprayed into the granulation and drying room at a high propellant pressure and the subsequent granulation is carried out, if desired, with the addition of one or more inorganic or organic solids and with simultaneous drying. 2. The method according to claim 1, characterized in that the separately reactant flows charged with a gaseous medium in almost stoichiometric sets merged over one or more more fabric nozzles are sprayed into the granulating and drying room. 3. The method according to claim 1, characterized in that the anionic surfactant in its acid form or the mixture containing one or more anions contains side in its acid form, with a gaseous medium beats and a multi-component nozzle in the granulating and drying nungsraum is sprayed, while at the same time an aqueous, with a Alkaline solution in almost any gaseous medium stoichiometric amounts via another multi-component nozzle in the Gra nulier- and drying room is sprayed. 4. The method according to any one of claims 1 to 3, characterized in that the ratio of the number of acidic groups to the alkaline Groups in the range from 1.1: 1 to 0.8: 1, preferably from 1: 1 to 0.9: 1 lies.   5. The method according to any one of claims 1 to 4, characterized in that fatty acids, alkylarylsulfonic acids such as C ₉ -C ₁₃ alkylbenzenesulfonic acid, α-sulfofatty acid esters and the sulfuric acid semiesters of optionally alkoxylated, especially ethoxylated fatty alcohols and / or sulfosuccinic acid are used. 6. The method according to any one of claims 1 to 5, characterized in that an anionic surfactant in its acid form or a mixture of the Group of anionic surfactants in their acid form in combination with not ionic, amphoteric and / or cationic surfactants is used. 7. The method according to any one of claims 1 to 6, characterized in that air, nitrogen or water vapor is used as the propellant. 8. The method according to any one of claims 1 to 7, characterized in that the granulation and simultaneous drying in the fluidized bed batchwise or continuously, preferably continuously leads. 9. The method according to any one of claims 1 to 8, characterized in that the discharge of the granules from the fluidized bed over a size the granules are classified. 10. The method according to any one of claims 1 to 9, characterized in that the soil air temperature between -20 and 400 ° C, preferably between 35 and 350 ° C and in particular between 35 and 120 ° C, the Temperature of the vortex air between about 5 cm above the base plate 10 and 120 ° C, preferably between 65 and 20 ° C and in particular is between 30 and 85 ° C. 11. The method according to any one of claims 1 to 10, characterized in that that as solids non-surfactant ingredients of washing and Detergents, preferably one or more components from the Group of alkali carbonates, alkali sulfates, crystalline and amorphous Alkali silicates and layered silicates as well as zeolite, salts of Citric acid or other polycarboxylic acids, solid peroxy bleach  and optionally bleach activators and solid polyethylene glycols a molecular weight greater than or equal to 2000, in particular between 4,000 and 20,000. 12. The method according to any one of claims 1 to 11, characterized in that the added solids in an amount of 10 to 50 wt .-% and in particular from 20 to -5% by weight, based in each case on the sum Surfactant preparation form and solid, are used. 13. surfactant granules, produced according to one of claims 1 to 12, characterized characterized in that it is 10 to 100% by weight, preferably 30 to 90 % By weight and in particular 40 to 90% by weight, in each case based on the finished granules, containing tensides. 14. surfactant granules according to claim 13, characterized in that it is a Bulk density between 500 and 1000 g / l, in particular between 550 and 850 g / l and no particles with a particle size below 50 µm having.