EP0642576B1 - Procede de fabrication continue d'un detergent et/ou d'un nettoyant granulaire - Google Patents

Procede de fabrication continue d'un detergent et/ou d'un nettoyant granulaire Download PDF

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Publication number
EP0642576B1
EP0642576B1 EP93909975A EP93909975A EP0642576B1 EP 0642576 B1 EP0642576 B1 EP 0642576B1 EP 93909975 A EP93909975 A EP 93909975A EP 93909975 A EP93909975 A EP 93909975A EP 0642576 B1 EP0642576 B1 EP 0642576B1
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EP
European Patent Office
Prior art keywords
weight
granules
granulator
mixer
granulation
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EP93909975A
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German (de)
English (en)
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EP0642576A1 (fr
Inventor
Hans-Friedrich Kruse
Hans-Josef Beaujean
Thomas Holderbaum
Jochen Jacobs
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Henkel AG and Co KGaA
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Henkel AG and Co KGaA
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D11/00—Special methods for preparing compositions containing mixtures of detergents
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D11/00—Special methods for preparing compositions containing mixtures of detergents
    • C11D11/0082—Special methods for preparing compositions containing mixtures of detergents one or more of the detergent ingredients being in a liquefied state, e.g. slurry, paste or melt, and the process resulting in solid detergent particles such as granules, powders or beads
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D11/00—Special methods for preparing compositions containing mixtures of detergents
    • C11D11/0082—Special methods for preparing compositions containing mixtures of detergents one or more of the detergent ingredients being in a liquefied state, e.g. slurry, paste or melt, and the process resulting in solid detergent particles such as granules, powders or beads
    • C11D11/0088—Special methods for preparing compositions containing mixtures of detergents one or more of the detergent ingredients being in a liquefied state, e.g. slurry, paste or melt, and the process resulting in solid detergent particles such as granules, powders or beads the liquefied ingredients being sprayed or adsorbed onto solid particles
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D17/00—Detergent materials or soaps characterised by their shape or physical properties
    • C11D17/06—Powder; Flakes; Free-flowing mixtures; Sheets
    • C11D17/065—High-density particulate detergent compositions

Definitions

  • the invention relates to a process for the continuous production of granular detergents and / or cleaning agents, wherein non-dusting and non-greasy granules are obtained by suitably chosen process conditions, which preferably have a bulk density between 600 and 1000 g / l.
  • the prior art knows a number of proposals for the batchwise or continuous production of compacted granules.
  • Either high-speed, high-speed mixers / granulators are used, or two mixers / granulators are connected in series, whereby the first mixer / granulator is a high-speed, high-speed mixer / granulator and the second mixer / granulator is a slow-running, low-speed mixer / granulator.
  • granulations in a high-speed, high-speed mixer / granulator are disclosed in European patent applications 351 937 and 339 996.
  • EP-A-390 251 describes a two-stage granulation process in which 0.1 to 40% by weight of the solid starting material is added after the first granulation stage (high-speed mixer / granulator) and, if appropriate, during the second granulation stage (slow-speed mixer / granulator) becomes.
  • a common feature of these known processes is that the granules obtained by them have a bulk density of between about 600 and 900 g / l, but tend to cake, stick and grease if the processes are not nearly water-free and / or essentially free of nonionic surfactants and / or be carried out in a certain temperature range.
  • the bulk density can only be set to a small extent in a targeted manner.
  • This process should also make it possible to adjust the bulk density of the granules in a targeted manner, as well as to produce granules with a relatively low proportion of coarse particles.
  • a special feature of the process according to the invention is that in the two-stage granulation process, in which a low-speed and a high-speed mixer / granulator are used, in contrast to the known processes of the prior art, the first part of the granulation in a low-speed mixer / granulator and only the second part is carried out in a high-speed mixer / granulator, the process conditions in the high-speed mixer / granulator being set according to the requirements of the desired granulate so that the The first, low-speed mixer / granulator, the resulting granulate is not adhesive, but is nevertheless plastic to the extent that it can be deformed to compress it. As a result, the proportion of coarse-grain granules formed in the first low-speed mixer / granulator can be largely reduced without the coarse-grain fraction being ground or pulverized.
  • all mixers / granulators through which the product flows horizontally can be used in the first granulation stage, in which the product is moved in the mixer room by mixing tools.
  • the granulation can be carried out by. cutter heads located in the lower part of the mixer drum are accelerated. Granulation in these mixers / granulators is possible at peripheral speeds of the mixing tools between 2 m / s and 7 m / s and is preferably carried out at peripheral speeds between 4 m / s and 5 m / s.
  • Low-speed mixers / granulators which are preferably used are, for example, the ploughshare mixers from Lödige (Federal Republic of Germany) and the intensive mixers from IMCATEC (Federal Republic of Germany).
  • the first granulation stage is preferably carried out in a time of 0.5 to 10 minutes, average residence times in the first granulation stage between 1 and 6 minutes being preferred.
  • mixers / granulators are used as high-speed mixers / granulators, through which the mixture to be granulated flows vertically and whose mixing tools can be operated at peripheral speeds of at least about 8 m / s. It is preferred that a concentrically arranged in a cylindrical mixing chamber and fast rotating shaft on which the mixing tools are in the form of mixing knives or beaters, the product in a spiral downward annular layer along the mixer chamber wall at a peripheral speed of the mixing tools of 8 m / s to 35 m / s, preferably at peripheral speeds of 12 m / s to 30 m / s, is transported to the mixer outlet.
  • a suitable high-speed mixer / granulator is, for example, the ring-layer mixer from Schugi (Netherlands).
  • the second stage of granulation is generally in a much shorter time than the first granulation stage, for example up to 30 seconds.
  • Preferred granulation times in the second granulation stage are 0.1 to 10 seconds and in particular 0.5 to 2 seconds.
  • the sequence of the granulation steps defined according to the invention (first granulation in a low-speed mixer / granulator, then in a high-speed mixer / granulator) enables almost any desired bulk density between 600 and Selectively set 1100 g / l.
  • the parameter of the first granulation stage by means of which the bulk density can be influenced, is the energy input to the mixture to be granulated, a high energy input being achieved over long dwell times and over the number and speed of the cutter heads to be used. Heavy granules are obtained through high energy inputs.
  • the second pelletizing stage in which the peripheral speeds of the mixing tools and the energy input are increased by increasing the speeds of the mixer shaft, which leads to an increase in the bulk density in addition to the reduction of coarse particles.
  • the most important parameter for setting the bulk density is the addition of the liquid constituents, which also serve as granulating liquid and which can be added either only in the first, low-speed mixer / granulator or partly in the low-speed mixer / granulator and partly in the high-speed mixer / granulator.
  • the general rule is that by adding granulating liquids alone in the first, low-speed mixer / granulator, higher ones Bulk weights, for example between 800 and 950 g / l, can be achieved, while for setting lower bulk weights, for example bulk weights between 600 and 800 g / l, it is advisable to add part of the granulating liquid only in the second, high-speed mixer / granulator.
  • granules with a bulk density of about 850 g / l were obtained by adding the entire granulating liquid in the first mixer / granulator.
  • granules with a bulk density of 680 g / l were obtained for the same formulation.
  • granules with a bulk density between 600 g / l and 570 g / l were obtained for the same recipe.
  • some of the solid components - either alone or in addition to the part of the granulating liquid - can only be used in the high-speed mixer / granulator.
  • solids in particular fine-particle solids such as zeolite powder, for example Wessalith P (R) (commercial product from Degussa, Federal Republic of Germany), sodium sulfate or sodium carbonate, increases the bulk density in the second mixer / granulator can.
  • the addition of solids in the second granulation stage can also serve to improve the further processability of the granules and the flow properties of the finished granules.
  • 40 to 100% by weight, preferably 60 to 100% by weight and in particular up to 95% by weight of the solid and liquid constituents are pregranulated in the first mixer / granulator and then with 0 to 60% by weight %, preferably 5 to 40% by weight of remaining solid and / or liquid constituents are mixed in the second mixer / granulator and then transferred to the finished, but not yet dried and therefore possibly still moist granulate.
  • the solid constituents can be introduced into the process as powders or granules which have been obtained by granulation or spray drying and have a bulk density of, for example, 200 to 600 g / l.
  • the powders are usually individual components, for example zeolite, sodium carbonate, tripolyphosphate, water glass or sodium sulfate, while the granules preferably contain several components, mostly also small components and liquid feedstocks. Powder alone or granules alone can be used.
  • the constituents used in the granulation in the first mixer / granulator preferably 10 to 100% by weight and in particular 40 to 100% by weight, in each case based on those used in the first mixer / granulator solid components, used as granules.
  • solid ingredients of detergents and / or cleaning agents can be used as solid constituents.
  • Preferred solid constituents are anionic surfactants, builder substances, alkaline and neutral salts, bleaching agents and graying inhibitors.
  • Preferred surfactants of the sulfonate type are C 9 -C 13 alkylbenzenesulfonates, olefin sulfonates, ie mixtures of alkene and hydroxyalkanesulfonates and disulfonates such as are obtained, for example, from C 12 -C 18 monoolefins with a terminal or internal double bond by sulfonating with gaseous Sulfur trioxide and subsequent alkaline or acidic hydrolysis of the sulfonation products is considered.
  • alkanesulfonates obtained from C 12 -C 18 alkanes, for example by sulfochlorination or sulfoxidation with subsequent hydrolysis or neutralization.
  • Preferred anionic surfactants are also the salts of alkylsulfosuccinic acid, which are also referred to as sulfosuccinates or as sulfosuccinic acid esters, and the monoesters and / or diesters of sulfosuccinic acid Alcohols, preferably fatty alcohols and especially ethoxylated fatty alcohols.
  • Preferred sulfosuccinates contain C 8 to C 18 fatty alcohol residues or mixtures thereof.
  • Particularly preferred sulfosuccinates contain a fatty alcohol residue which is derived from ethoxylated fatty alcohols, which in themselves are nonionic surfactants (description see below).
  • sulfosuccinates the fatty alcohol residues of which are derived from ethoxylated fatty alcohols with a restricted homolog distribution, are particularly preferred.
  • esters of ⁇ -sulfo fatty acids e.g. the ⁇ -sulfonated methyl esters of hydrogenated coconut, palm kernel or tallow fatty acids.
  • Suitable surfactants of the sulfate type are the sulfuric acid monoesters from primary alcohols of natural and synthetic origin, in particular from fatty alcohols, for example from coconut oil alcohol, tallow fatty alcohol, oleyl alcohol, lauryl, myristyl, cetyl or stearyl alcohol, or the C 10 -C 20 oxo alcohols, and those secondary alcohols of this chain length.
  • Fatty alcohol mixtures which may additionally contain proportions of unsaturated alcohols, for example oleyl alcohol, are also preferred.
  • Suitable anionic surfactants are, in particular, soaps, preferably in amounts of 0.5 to 8% by weight.
  • Saturated fatty acid soaps are suitable, such as the salts of lauric acid, myristic acid, palmitic acid or stearic acid, and in particular soap mixtures derived from natural fatty acids, for example coconut, palm kernel or tallow fatty acids.
  • soap mixtures are preferred which are composed of 50 to 100% by weight of saturated C 12 -C 18 fatty acid soaps and 0 to 50% by weight of oleic acid soap.
  • the anionic surfactants can be in the form of their sodium, potassium or ammonium salts and as soluble salts of organic bases, such as mono-, di- or triethanolamine.
  • the anionic surfactants are preferably in the form of their sodium or potassium salts, in particular in the form of the sodium salts.
  • the anionic surfactants are preferably used in amounts of 3 to 25% by weight, in particular in amounts of 10 to 20% by weight, in each case based on the sum of the constituents used. However, their content can also exceed 15% by weight.
  • Preferred anionic surfactants are fatty alkyl sulfates, alkylbenzenesulfonates, sulfosuccinates and mixtures thereof, such as mixtures of fatty alkyl sulfates and sulfosuccinates or fatty alkyl sulfates and fatty alkylbenzenesulfonates, especially in combination with soap. It is particularly preferred that at least some of the sulfonate and / or sulfate surfactants are used as a component of the granulating liquid rather than as a solid component.
  • the known zeolites and phosphates are particularly suitable as builder substances.
  • Their content is preferably 20 to 60% by weight, in particular 20 to 50% by weight, in each case based on the sum of the constituents used and calculated as an anhydrous active substance.
  • the finely crystalline, synthetic and bound water-containing zeolite used is preferably zeolite NaA in detergent quality. It is preferably used as a spray-dried powder.
  • Preferred zeolites have an average particle size of less than 10 ⁇ m (volume distribution; measurement method: Coulter Counter) and preferably contain 20 to 22% by weight of bound water.
  • Usable organic builders are, for example, the polycarboxylic acids preferably used in the form of their sodium salts, such as citric acid, succinic acid, glutaric acid, adipic acid, tartaric acid and nitrilotriacetic acid (NTA), provided that such use is not objectionable for ecological reasons, and mixtures of these.
  • polycarboxylic acids preferably used in the form of their sodium salts, such as citric acid, succinic acid, glutaric acid, adipic acid, tartaric acid and nitrilotriacetic acid (NTA), provided that such use is not objectionable for ecological reasons, and mixtures of these.
  • Polymeric polycarboxylates come into consideration as further organic builder substances.
  • Suitable polymeric polycarboxylates are, for example, the sodium salts of polyacrylic acid or polymethacrylic acid, for example those with a relative molecular weight of 800 to 150,000 (based on acid).
  • Suitable copolymeric polycarboxylates are, in particular, those of acrylic acid with methacrylic acid and of acrylic acid or methacrylic acid with maleic acid. Copolymers of acrylic acid with maleic acid which contain 50 to 90% by weight of acrylic acid and 50 to 10% by weight of maleic acid have proven to be particularly suitable. Copolymers in which 60 to 85% by weight of acrylic acid and 40 to 15% by weight of maleic acid are present are particularly preferred.
  • Their relative molecular weight, based on free acids is generally 5,000 to 200,000, preferably 10,000 to 120,000 and in particular 50,000 to 100,000.
  • the content of (co) polymeric polycarboxylates in the agents is preferably 0.5 to 8% by weight.
  • polyacetals which can be obtained by reacting dialdehydes with polyolcarboxylic acids which have 5 to 7 carbon atoms and at least 3 hydroxyl groups, for example as described in European patent application 280 223.
  • Preferred polyacetals are obtained from dialdehydes such as glyoxal, glutaraldehyde, terephthalaldehyde and their mixtures and from polyol carboxylic acids such as gluconic acid and / or glucoheptonic acid.
  • the alkaline salts used with preference include water-soluble inorganic salts such as bicarbonates, carbonates, silicates or mixtures thereof; in particular alkali carbonate and alkali silicate, especially sodium silicate with a molar ratio of 1: 1 to 1: 4.5, used.
  • the sodium carbonate content of the agents is preferably up to 20% by weight, advantageously between 1 and 15% by weight.
  • the content of sodium silicate in the agents, for example amorphous or crystalline sodium disilicate is generally up to 10% by weight and preferably between 2 and 8% by weight.
  • sulfates are used, this is preferably done in amounts between 15 and 40% by weight, based on the finished granulate. However, processes in which no sulfate is used are also preferred.
  • bleaching agents that can be used are, for example, sodium percarbonates, peroxypyrophosphates, citrate perhydrates and H 2 O 2 -producing peracidic salts or peracids, such as perbenzoates, peroxaphthalates, diperazelaic acid or diperdodecanedioic acid.
  • the bleaching agent content of the agents is preferably 5 to 25% by weight and in particular 10 to 20% by weight, based on the finished granulate.
  • the bleaching agents can be added either in the granulation process according to the invention or in a subsequent processing step.
  • bleaching agents preferably perborates and percarbonate
  • they are preferably added in the second granulation stage, the granule temperature not exceeding 70 ° C. If necessary, this can be achieved by cooling.
  • Graying inhibitors have the task of keeping the dirt detached from the fibers suspended in the liquor and thus preventing graying.
  • Water-soluble colloids of mostly organic nature are suitable for this, for example the water-soluble salts of polymeric carboxylic acids, glue, gelatin, salts of ether carboxylic acids or ether sulfonic acids of starch or cellulose or salts of acidic sulfuric acid esters of cellulose or starch.
  • Water-soluble polyamides containing acidic groups are also suitable for this purpose. Soluble starch preparations and starch products other than those mentioned above can also be used, for example degraded starch, aldehyde starches etc.
  • Carboxymethyl cellulose, methyl cellulose, methyl hydroxyethyl cellulose and mixtures thereof and polyvinylpyrrolidone are preferably used in amounts between 0.1 and 5% by weight, in particular up to 3% by weight.
  • a granulating liquid which either consists only of pure liquid constituents or mixtures thereof or which contains solid constituents in dissolved and / or suspended form.
  • the granulating liquid is preferably used in amounts of 5 to 30% by weight, based on the total amount of the constituents used. Overall, it can only be used in the first mixer / granulator or partly in the first mixer / granulator and partly in the second mixer / granulator. It is preferred that, depending on the desired bulk density, 0 to 20% by weight, preferably up to 10% by weight, based in each case on the total amount of the constituents used, of granulating liquid are added in the second, high-speed mixer / granulator.
  • the granulating liquid preferably consists of liquid constituents of detergents and / or cleaning agents or of water, of aqueous solutions and / or of mixtures which contain per se solid constituents and liquid constituents of detergents and / or cleaning agents.
  • the liquid constituents of washing and / or cleaning agents include, in particular, nonionic surfactants which are in liquid, ie pumpable and flowable, form at the process temperature.
  • nonionic surfactants preferably include addition products of 1 to 12 moles of ethylene oxide with primary C 12 -C 18 fatty alcohols and their mixtures, such as coconut oil, tallow oil or oleyl alcohol, or with primary alcohols (oxo alcohols) branched with methyl in the 2-position.
  • C 12 -C 14 alcohols with 3 EO or 4 EO C 9 -C 11 alcohol with 7 EO, C 13 -C 15 alcohols with 3 EO, 5 EO, 7 EO or 8 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.
  • the degrees of ethoxylation given represent statistical mean values which, for a specific product, are an integer or a fraction can.
  • Preferred alcohol ethoxylates have a restricted homolog distribution (narrow range ethoxylates, NRE).
  • the content of the ethoxylated fatty alcohols in the finished granules is preferably 5 to 15% by weight.
  • the liquid nonionic surfactants are used in a mixture with lower polyalkylene glycols which are derived from straight-chain or branched glycols having 2 to 6 carbon atoms.
  • Preferred lower polyalkylene glycols are polyethylene glycols or polypropylene glycols which have a relative molecular mass between 200 and 12,000, in particular between 200 and 4,000, for example up to 2,000.
  • the weight ratio of liquid nonionic surfactant to lower polyalkylene glycol in these mixtures is preferably 10: 1 to 1: 1.
  • the preferred aqueous mixtures also include aqueous alkyl glycoside pastes in which alkyl glycosides of the general formula RO (G) x are used, in which R is a primary straight-chain or aliphatic radical with 8 to 22, preferably 12 to 18 C, methyl-branched in the 2-position -Atoms means and G is the symbol which stands for a glycose unit with 5 or 6 carbon atoms, preferably for glycose.
  • the degree of oligomerization X which indicates the distribution of monoglycosides and oligoglycosides, is any number between 1 and 10 and is preferably 1.2 to 1.4.
  • the preferred aqueous solutions also include the solutions of (co) polymeric polycarboxylates already mentioned. They are preferably added in the first, low-speed mixer / granulator in order to obtain heavy granules. A reduction in the bulk density can preferably be achieved by adding this solution in the second, high-speed mixer / granulator.
  • aqueous suspensions of zeolites which preferably contain stabilizers for these suspensions, can preferably be used in the first, low-speed mixer / granulator.
  • concentrated aqueous anionic surfactant solutions and anionic surfactant pastes is also particularly preferred. These are preferably by neutralizing the Anionic surfactants in their acid form with highly concentrated aqueous bases, for example a 45 to 55% strength by weight sodium hydroxide solution, are produced in a commercially available rotor-stator machine, for example a Supraton (R) , or a stirred kettle.
  • nonionic surfactants are particularly preferred, the nonionic surfactants preferably being used in amounts such that the viscosity of the anionic surfactant pastes is reduced and thus their processability, in particular pumpability and flowability, is improved.
  • These mixtures have a pH of at least 7.0, preferably from 7.5 to 12, and are added as constituents of the granulating liquid either in the first or in the second mixer / granulator. It is preferred that 8 to 20% by weight, preferably 10 to 18% by weight, based in each case on the total amount of the constituents used, of these anionic surfactant-nonionic surfactant mixtures are added, in particular in the first, low-speed mixer / granulator.
  • a drying stage can be added. This is not necessary if the granulating liquid contains no water, or is not absolutely necessary if the granulating liquid contains water only in small amounts, for example up to 12% by weight, based on the total amount of the constituents used. The amount of water tolerable without drying depends heavily on the overall composition. However, if the granulating liquid contains water, irrespective of the amount, the subsequent drying step is preferred. In particular, this drying is carried out in the fluidized bed at supply air temperatures below 180 ° C. The granulating liquid preferably contains only so much water that under these conditions a maximum of 15% by weight, based on the total amount of the constituents used, of water evaporate.
  • the continuous process according to the invention is not only distinguished by the fact that it enables the targeted setting of a desired bulk density of the granules produced; granules are also obtained which are distinguished by a very homogeneous grain spectrum with small coarse grain fractions, the fraction of granules with a diameter above 2 mm and in particular above 1.6 mm being preferred is a maximum of 12% by weight and in particular a maximum of 10% by weight (sieve analysis).
  • Existing coarse-grained fractions that is to say granules with a diameter above 2 mm, preferably with a diameter above 1.6 mm, are preferably screened off and can advantageously be returned to the continuous production process after comminution, for example in a mill. It is preferred to return the crushed coarse particles to the sieve and thus to feed further finished granules. It is also possible to recycle crushed coarse particles or fine particles, i.e. granules with a diameter of less than 0.1 mm, in every granulation stage.
  • the granules obtained by the process according to the invention can be used directly as detergents and / or cleaning agents and / or they are mixed with further amounts, preferably small amounts, for example in the range from 2 to 10% by weight, based on the total amount of the constituents used , sprayed on liquid nonionic surfactants or nonionic surfactant mixtures in a manner known per se and / or they are mixed in a preparation step with further constituents, preferably granular and in particular granular and compacted constituents of detergents and cleaning agents.
  • the other granular constituents include, for example, compacted bleach or bleach activator granules, enzyme granules, foam inhibitor granules, preferably concentrated foam inhibitor granules and granular carriers for colorants and fragrances.
  • N-acyl or O-acyl compounds preferably N, N'-tetraacylated diamines, also carboxylic anhydrides and esters of polyols such as glucose pentaacetate.
  • the bleach activators contain bleach activators in the usual range, preferably between 1 and 10% by weight and in particular between 2 and 8% by weight.
  • Particularly preferred Bleach activators are N, N, N ', N'-tetraacetylethylenediamine (TAED) and 1,5-diacetyl-2,4-dioxo-hexahydro-1,3,5-triazine (DADHT).
  • Suitable enzymes are those from the class of proteases, lipases, amylases, cellulases or mixtures thereof. Enzymes obtained from bacterial strains or fungi such as Bacillus subtilis, Bacillus licheniformis and Streptomyces griseus are particularly suitable. Proteases of the subtilisin type and in particular proteases which are obtained from Bacillus lentus are preferably used. Their proportion can be about 0.2 to about 2% by weight. The enzymes can be adsorbed on carriers and / or embedded in coating substances in order to protect them against premature decomposition.
  • Suitable stabilizers are, for example, the salts of polyphosphonic acids, in particular 1-hydroxyethane-1,1-diphosphonic acid (HEDP).
  • HEDP 1-hydroxyethane-1,1-diphosphonic acid
  • Suitable foam inhibitors are, for example, soaps of natural or synthetic origin, which have a high proportion of C 18 -C 24 fatty acids.
  • Suitable non-surfactant-like foam inhibitors are, for example, organopolysiloxanes and their mixtures with microfine, optionally silanized silica, and paraffins, waxes, microcrystalline waxes and their mixtures with silanized silica. Mixtures of various foam inhibitors are also advantageously used, for example those made of silicone, paraffins or waxes. It is also possible for silicone oils and / or paraffin oils to be used in the two-stage granulation process according to the invention and preferably in the first, low-speed mixer / granulator.
  • optical brighteners the agents can contain derivatives of diaminostilbenedisulfonic acid or its alkali metal salts. Suitable are, for example, salts of 4,4'-bis (2-anilino-4-morpholino-1,3,5-triazin-6-yl-amino) stilbene-2,2'-disulfonic acid or compounds of the same structure which are used instead of Morpholino group, a diethanolamino group, a methylamino group, an anilino group or one Wear 2-methoxyethylamino group.
  • Brighteners of the substituted 4,4'-distyryl-di-phenyl type may also be present, for example the compound 4,4'-bis (4-chloro-3-sulfostyryl) diphenyl. Mixtures of the aforementioned brighteners can also be used. Particularly uniform white granules are obtained if, in addition to the usual brighteners, the agents are also used in customary amounts, for example between 0.1 and 0.5% by weight, preferably between 0.1 and 0.3% by weight, contains, for example, 10 -6 to 10 -3 % by weight, preferably around 10 -5 % by weight, of a blue dye.
  • a particularly preferred dye is Tinolux (R) (commercial product from Ciba-Geigy).
  • optical brighteners or the mixtures of optical brightener and dye are preferably dissolved in ethoxylated nonionic surfactants and sprayed onto the granules produced by the process according to the invention in a known manner.
  • the granular detergents and / or cleaning agents produced in this way and having advantages generally have a bulk density between 600 and 1100 g / l, preferably between 700 and 950 g / l and, after sieving the coarse-grained fractions, preferably above 1.6 mm in particular between 750 and 850 g / l.
  • the granules are non-greasy, dust-free and, after drying, if appropriate, have a proportion of granules with a diameter above 1.6 mm of at most 25% by weight, preferably at most 20% by weight and in particular from 6 to 12% by weight, which is screened off and returned.
  • the content of anionic and nonionic surfactants in the granules is preferably 10 to 40% by weight and in particular 15 to 30% by weight, in each case based on the finished granules, and 20 to 60% by weight, preferably 25 to 55% by weight. -%, each based on the finished granulate and calculated as an anhydrous active substance, on builder substances.
  • the finished granules have a content of 7 to 15% by weight of nonionic surfactants and 0 to 20% by weight, preferably 0 to 10% by weight, of free, ie non-chemically or non-physically bound water .
  • the fill level of this low-speed mixer was about 50%.
  • the residence time of the ingredients in this mixer was about 3 minutes.
  • the pregranules were then granulated in a Schugi ring bed mixer for a maximum of 1 second at peripheral speeds of the ring bed of about 30 m / s and at temperatures of 35 ° C. and dried in a fluidized bed at supply air temperatures of 130 ° C.
  • the finished non-greasy, free-flowing and non-dusting granules had a bulk density of 860 g / l.
  • the proportion of the dried granules with a diameter above 1.6 mm was below 12% by weight before sieving.
  • Grain spectrum (sieve analysis) in% by weight: > 1.6 mm > 0.8 mm > 0.4 mm > 0.2 mm > 0.1 mm ⁇ 0.1 mm 9.1 28.7 32.9 26.6 2.7 -
  • granules were mixed with other constituents of washing and / or cleaning agents such as perborate tetrahydrate, bleach activator, foam inhibitor granules, enzyme, nonionic surfactant and optical brightener.
  • cleaning agents such as perborate tetrahydrate, bleach activator, foam inhibitor granules, enzyme, nonionic surfactant and optical brightener.
  • the spray-dried granules used in the low-speed mixer / granulator had the following composition: 10th % By weight C 9 -C 13 alkylbenzenesulfonate, sodium salt 4th % By weight C 12 -C 14 fatty acid soap, sodium salt 2.5 % By weight C 12 -C 18 fatty alcohol with 5 EO 20.0 % By weight Polyacrylate, sodium salt, (Sokalan CP5 (R) ) 9.0 % By weight Sodium silicate, Na 2 O: SiO 2 1: 2.0 (?) 42.5 % By weight sodium 2.0 % By weight 1-hydroxyethane-1,1-diphosphonate, sodium salt rest Water, dye, optical brightener
  • Example 1 was repeated. However, the pre-granulate was produced without the Sokalan (R) CP 5 solution. The sokalan was added in the form of a 30% by weight aqueous solution via nozzles during the second granulation step. The bulk density of these granules after drying and after sieving was 720 g / l. The coarse grain fraction above 1.6 mm was 6% by weight.
  • Example 2 was repeated. However, the second granulation step was carried out at peripheral speeds of the ring layer of 17 m / s. The bulk density of these granules after drying and after sieving was 621 g / l. The coarse grain fraction above 1.6 mm was 21% by weight.
  • Example 1 was repeated.
  • the temperature of the pre-granulate was 48 ° C. when entering the second granulation stage.
  • the bulk density of these granules was 830 g / l.
  • Example 1 was repeated.
  • the residence time in the first mixer was 4 minutes while simultaneously reducing the Sokalan (R) CP 5 solution to 6% by weight. After drying and sieving 23% by weight of coarse particles above 1.6 mm, a bulk density of 930 g / l was obtained.

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Claims (12)

  1. Procédé de production en continu d'un produit de lavage et/ou d'un produit de nettoyage granuleux, ayant une densité apparente élevée par une granulation en deux étapes dans deux mélangeurs/granulateurs connectés l'un derrière l'autre, caractérisé en ce que dans le premier mélangeur/granulateur à nombre de tours faible, qui est traversé horizontalement par le produit et dans lequel la granulation à des vitesses périphériques des outils de mélange, entre 2 m/s et 7 m/s est possible, on pré-granule 40 à 100 % en poids, rapportés à la quantité globale de constituants mis en jeu, des constituants solides et liquides et dans un deuxième mélangeur/granulateur, qui est traversé verticalement par le mélange à granuler et dont les outils de mélange peuvent être actionnés avec des vitesses périphériques d'au moins environ 8 m/s, le pré-granulé provenant de la première étape de procédé est mélangé le cas échéant avec les constituants résiduels solides et/ou liquides et est transformé en granulé, le granulé formé étant plastique à la périphérie, et en ce qu'il peut être déformé dans la deuxième étape de granulation d'une manière compactante et en ce que la quantité de granulés ayant un diamètre au-dessus de 2 mm s'élève à moins de 25 % en poids.
  2. Procédé selon la revendication 1, caractérisé en ce que la granulation dans le premier mélangeur/granulateur est effectuée pendant une durée comprise entre 0,5 à 10 minutes et dans le deuxième mélangeur/granulateur à des vitesses périphériques de 8 m/s à 35 m/s pendant une durée comprise entre 0,1 et 30 sec., de préférence jusqu'à 10 secondes et en particulier entre 0,5 et 2 secondes.
  3. Procédé selon l'une des revendications 1 ou 2, caractérisé en ce que la température du pré-granulé lors de l'entrée dans la deuxième étape de granulation est comprise entre 30°C et 60°C.
  4. Procédé selon l'une des revendications 1 à 3, caractérisé en ce qu'au moins une partie des constituants mis en jeu lors de la granulation dans le premier mélangeur/granulateur, de préférence de 10 à 100 % en poids, rapportés aux constituants solides mis en jeu dans le premier mélangeur/granulateur, sont utilisés sous forme de granulé, dans lequel la proportion de ces granulés, de préférence des granulés séchés par pulvérisation, s'élève en particulier de 10 à 40 % en poids, rapportés à la formulation globale.
  5. Procédé selon l'une des revendications 1 à 4, caractérisé en ce que l'on pré-granule de 40 à 100 % en poids, de préférence de 60 à 100 % en poids et en particulier jusqu'à 95 % en poids de constituants solides et liquides dans le premier mélangeur/granulateur et qu'ensuite on mélange de 0 à 60 % en poids, de préférence de 5 à 40 % en poids, de constituants solides et/ou liquides résiduels dans le deuxième mélangeur/granulateur et qu'on le convertit en granulé éventuellement encore humide.
  6. Procédé selon l'une des revendications 1 à 5, caractérisé en ce que le liquide de granulation qui renferme éventuellement des constituants solides sous forme dissoute et/ou en suspension est mis en oeuvre, en quantités de 5 à 30 % en poids, rapportées à la quantité globale des constituants mis en jeu.
  7. Procédé selon la revendication 6, caractérisé en ce que comme liquide de granulation on met en oeuvre de l'eau, des solutions aqueuses, des agents tensioactifs non ioniques qui se présentent à la température du procédé sous forme liquide et/ou des mélanges de solutions aqueuses et d'agents tensioactifs non ioniques, de préférence un mélange à base d'une solution d'agent tensioactif anionique aqueuse et d'agents tensioactifs non ioniques, dans laquelle le mélange a une valeur de pH d'au moins 7,0.
  8. Procédé selon l'une des revendications 6 ou 7, caractérisé en ce que l'on ajoute de 0 à 20 % en poids, de préférence jusqu'à 10 % en poids, à chaque fois rapportés à la quantité globale des constituants mis en jeu, en liquide de granulation, de préférence un mélange à base d'une solution aqueuse d'agent tensioactif anionique et d'agents tensioactifs non ioniques, et/ou d'une solution aqueuse polymère de polycarboxylate, dans le deuxième mélangeur/granulateur à nombre de tours élevé.
  9. Procédé selon l'une des revendications 1 à 8, caractérisé en ce que le degré de remplissage du premier mélangeur/granulateur est ajusté de 10 à 80 % en poids et en ce que le deuxième mélangeur/granulateur est mis en fonctionnement à des vitesses périphériques élevées, d'environ 25 m/s à environ 30 m/s.
  10. Procédé selon l'une des revendications 1 à 9, caractérisé en ce que l'on sèche les granulés après la granulation de la deuxième étape, le séchage étant effectué, de préférence, en couche fluidisée à des températures d'amenée de l'air en dessous de 180°C et que l'on évapore pour cela au maximum 15 % en poids d'eau, rapporté à la quantité globale de constituants mis en jeu.
  11. Procédé selon l'une des revendications 1 à 10, caractérisé en ce que les granulés obtenus dans une étape de traitement sont mélangés avec des constituants supplémentaires de produits de lavage et/ou de nettoyage.
  12. Procédé selon l'une des revendications 1 à 11, caractérisé en ce que l'on produit un granulé ayant une densité apparente comprise entre 600 et 1 100 g/l, de préférence entre 700 et 950 g/l et en particulier entre 750 et 850 g/l, procédé dans lequel après séchage effectué éventuellement, la fraction de granulés ayant un diamètre au-dessus de 1,6 mm, est séparée par tamisage et est recyclée, cette fraction représentant au maximum 25 % en poids, de préférence au maximum 20 % en poids et en particulier de 6 à 12 % en poids.
EP93909975A 1992-05-21 1993-05-13 Procede de fabrication continue d'un detergent et/ou d'un nettoyant granulaire Expired - Lifetime EP0642576B1 (fr)

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DE4216774A DE4216774A1 (de) 1992-05-21 1992-05-21 Verfahren zur kontinuierlichen Herstellung eines granularen Wasch und/oder Reinigungsmittels
DE4216774 1992-05-21
PCT/EP1993/001191 WO1993023523A1 (fr) 1992-05-21 1993-05-13 Procede de fabrication continue d'un detergent et/ou d'un nettoyant granulaire

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EP0642576B1 true EP0642576B1 (fr) 1996-07-10

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JP (1) JP3488235B2 (fr)
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ES (1) ES2089820T3 (fr)
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US7186677B2 (en) 2001-12-21 2007-03-06 Henkel Kommanditgesellschaft Auf Aktien (Henkel Kgaa) Method for the production of surfactant granulates containing builders
EP1842900A1 (fr) 2004-04-03 2007-10-10 Henkel Kommanditgesellschaft auf Aktien Procédé destiné à la fabrication de granulés et leur utilisation dans des agents de lavage et/ou de nettoyage
US7300782B2 (en) 2001-12-21 2007-11-27 B.R.A.I.N. Biotechnology Research And Information Network Ag Glycosyl hydrolases
US7510859B2 (en) 2002-12-20 2009-03-31 Henkel Kommanditgesellschaft Auf Aktien Subtilisin variants with improved perhydrolase activity
US7803604B2 (en) 2000-07-28 2010-09-28 Henkel Ag & Co. Kgaa Amylolytic enzyme extracted from Bacillus sp. A 7-7 (DSM 12368) and washing and cleaning agents containing this novel amylolytic enzyme
US7888104B2 (en) 2000-11-28 2011-02-15 Henkel Ag & Co. Kgaa Cyclodextrin glucanotransferase (CGTase), obtained from<I>Bacillus agaradherens<λ>(DSM 9948) and detergents and cleaning agents containing said novel cyclodextrin glucanotransferase
US8263541B2 (en) 2005-08-19 2012-09-11 Henkel Ag & Co. Kgaa Triazine derivative dye transfer inhibitors, washing products containing the same and uses therefor
DE102004047776B4 (de) 2004-10-01 2018-05-09 Basf Se Gegen Di- und/oder Multimerisierung stabilisierte Alpha-Amylase-Varianten, Verfahren zu deren Herstellung sowie deren Verwendung
DE102004047777B4 (de) 2004-10-01 2018-05-09 Basf Se Alpha-Amylase-Varianten mit erhöhter Lösungsmittelstabilität, Verfahren zu deren Herstellung sowie deren Verwendung

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DE10138753B4 (de) * 2001-08-07 2017-07-20 Henkel Ag & Co. Kgaa Wasch- und Reinigungsmittel mit Hybrid-Alpha-Amylasen
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DE10160319B4 (de) * 2001-12-07 2008-05-15 Henkel Kgaa Tensidgranulate und Verfahren zur Herstellung von Tensidgranulaten
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WO2005123893A1 (fr) * 2004-06-16 2005-12-29 Henkel Kommanditgesellschaft Auf Aktien Granulation ciblee obtenue par neutralisation dans une machine de type compomix
DE102004029475A1 (de) * 2004-06-18 2006-01-26 Henkel Kgaa Neues enzymatisches Bleichsystem
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US6391838B1 (en) 1999-03-31 2002-05-21 Henkel Kommanditgesellschaft Auf Aktien Detergents containing enzymes and bleach activators
US7803604B2 (en) 2000-07-28 2010-09-28 Henkel Ag & Co. Kgaa Amylolytic enzyme extracted from Bacillus sp. A 7-7 (DSM 12368) and washing and cleaning agents containing this novel amylolytic enzyme
US7888104B2 (en) 2000-11-28 2011-02-15 Henkel Ag & Co. Kgaa Cyclodextrin glucanotransferase (CGTase), obtained from<I>Bacillus agaradherens<λ>(DSM 9948) and detergents and cleaning agents containing said novel cyclodextrin glucanotransferase
US7186677B2 (en) 2001-12-21 2007-03-06 Henkel Kommanditgesellschaft Auf Aktien (Henkel Kgaa) Method for the production of surfactant granulates containing builders
US7300782B2 (en) 2001-12-21 2007-11-27 B.R.A.I.N. Biotechnology Research And Information Network Ag Glycosyl hydrolases
US7510859B2 (en) 2002-12-20 2009-03-31 Henkel Kommanditgesellschaft Auf Aktien Subtilisin variants with improved perhydrolase activity
EP1842900A1 (fr) 2004-04-03 2007-10-10 Henkel Kommanditgesellschaft auf Aktien Procédé destiné à la fabrication de granulés et leur utilisation dans des agents de lavage et/ou de nettoyage
DE102004047776B4 (de) 2004-10-01 2018-05-09 Basf Se Gegen Di- und/oder Multimerisierung stabilisierte Alpha-Amylase-Varianten, Verfahren zu deren Herstellung sowie deren Verwendung
DE102004047777B4 (de) 2004-10-01 2018-05-09 Basf Se Alpha-Amylase-Varianten mit erhöhter Lösungsmittelstabilität, Verfahren zu deren Herstellung sowie deren Verwendung
US8263541B2 (en) 2005-08-19 2012-09-11 Henkel Ag & Co. Kgaa Triazine derivative dye transfer inhibitors, washing products containing the same and uses therefor
US8785362B2 (en) 2005-08-19 2014-07-22 Henkel Ag & Co. Kgaa Triazine derivative dye transfer inhibitors, washing products containing the same and uses therefor

Also Published As

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JPH07506611A (ja) 1995-07-20
DE59303203D1 (de) 1996-08-14
DE4216774A1 (de) 1993-11-25
ES2089820T3 (es) 1996-10-01
US5616550A (en) 1997-04-01
ATE140264T1 (de) 1996-07-15
WO1993023523A1 (fr) 1993-11-25
JP3488235B2 (ja) 2004-01-19
EP0642576A1 (fr) 1995-03-15

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