EP0339996B1 - Verfahren zur Herstellung von Waschmittelzusammensetzungen - Google Patents

Verfahren zur Herstellung von Waschmittelzusammensetzungen Download PDF

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Publication number
EP0339996B1
EP0339996B1 EP89304205A EP89304205A EP0339996B1 EP 0339996 B1 EP0339996 B1 EP 0339996B1 EP 89304205 A EP89304205 A EP 89304205A EP 89304205 A EP89304205 A EP 89304205A EP 0339996 B1 EP0339996 B1 EP 0339996B1
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EP
European Patent Office
Prior art keywords
detergent
granulation
starting material
mixer
particulate starting
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EP89304205A
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English (en)
French (fr)
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EP0339996A1 (de
Inventor
Robert Donaldson
Andrew Timothy Hight
Michael William Hollingsworth
Keiichi Kawafuchi
Donald Peter
Peter John Russell
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Unilever PLC
Unilever NV
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Unilever PLC
Unilever NV
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Priority claimed from GB888810194A external-priority patent/GB8810194D0/en
Priority claimed from GB888817386A external-priority patent/GB8817386D0/en
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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
    • C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
    • C11D1/66—Non-ionic compounds
    • C11D1/82—Compounds containing silicon
    • 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
    • C11D3/00—Other compounding ingredients of detergent compositions covered in group C11D1/00
    • C11D3/02—Inorganic compounds ; Elemental compounds
    • C11D3/12—Water-insoluble compounds
    • C11D3/124—Silicon containing, e.g. silica, silex, quartz or glass beads
    • C11D3/1246—Silicates, e.g. diatomaceous earth
    • C11D3/128—Aluminium silicates, e.g. zeolites
    • 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
    • C11D11/04—Special methods for preparing compositions containing mixtures of detergents by chemical means, e.g. by sulfonating in the presence of other compounding ingredients followed by neutralising
    • 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 present invention relates to a process for preparing granular detergent compositions of high bulk density having good washing performance and good powder properties.
  • GB-A-1 517 713 discloses a process in which a detergent powder produced by spray-drying or pan granulation is spheronised and granulated in a "marumerizer" (Trade Mark) with some increase in bulk density.
  • EP-A-229 671 discloses a process in which a spray-dried detergent powder containing surfactant and builder is subjected successively to pulverising and granulating treatments in a high-speed mixer/granulator, the granulation being carried out in the presence of an "agent for improving surface properties" and optionally a binder.
  • the agent for improving surface properties is zeolite 4A (10 parts), used together with water (2 parts) as binder. After granulation, a further 3 parts of zeolite 4A are admixed with the product.
  • JP-B-84 041680 (Kao) describes a process in which a spray-dried detergent base powder is pulverised, mixed with powdery granules, having a crystallinity of 0-100% and a particle size of 0.1-300 microns, of sodium aluminosilicate, calcium silicate, calcium carbonate, magnesium silicate or sodium carbonate, and simultaneously or subsequently mixed with a tackifying substance, for example, a nonionic surfactant, alkyl ether sulphate or higher alcohol.
  • a tackifying substance for example, a nonionic surfactant, alkyl ether sulphate or higher alcohol.
  • EP-A-220 024 discloses a process for the densification of a spray-dried powder containing a high level (30-85 wt%) of anionic surfactant.
  • the powder is compacted and granulated, inorganic builder (sodium tripolyphosphate, or crystalline sodium aluminosilicate and sodium carbonate) being added before compaction and/or after granulation.
  • inorganic builder sodium tripolyphosphate, or crystalline sodium aluminosilicate and sodium carbonate
  • detergent compositions of high bulk density and excellent flow properties can be prepared by granulating a spray-dried or dry-mixed detergent base powder in a high-speed mixer/granulator and then admixing a small amount of finely divided amorphous aluminosilicate after granulation is complete.
  • the amorphous material is substantially more weight-effective than crystalline zeolite for this purpose.
  • the present invention accordingly provides a process for the preparation of a granular detergent composition or component having a bulk density of at least 650 g/litre, which comprises the steps of:
  • a particulate starting material (detergent base powder) prepared by any suitable method is treated in a high-speed mixer/granulator to increase its bulk density and simultaneously to improve its powder properties.
  • the process of the invention provides a route for the production of very dense granular detergent compositions having excellent cleaning performance and good powder properties.
  • granulation is effected by means of a high-speed mixer/granulator having both a stirring action and a cutting action.
  • the stirrer and cutter may be operated independently of one another and at separately variable speeds.
  • Such a mixer is capable of combining a high energy stirring input with a cutting action, but can also be used to provide other, gentler stirring regimes with or without the cutter in operation. It is thus a highly versatile and flexible piece of apparatus.
  • a preferred type of high-speed mixer/granulator for use in the process of the invention is bowl-shaped and preferably has a substantially vertical stirrer axis.
  • mixers of the Fukae (Trade Mark) FS-G series manufactured by Fukae Powtech Kogyo Co., Japan are essentially in the form of a bowl-shaped vessel accessible via a top port, provided near its base with a stirrer having a substantially vertical axis, and a cutter positioned on a side wall.
  • the stirrer and cutter may be operated independently of one another, and at separately variable speeds.
  • Another mixer found to be suitable for use in the process of the invention is the Lödige (Trade Mark) FM series batch mixer ex Morton Machine Co. Ltd., Scotland. This differs from the mixers mentioned above in that its stirrer has a horizontal axis.
  • the use of a high-speed mixer/granulator is essential in the process of the invention to effect granulation and densification.
  • the mixer may also be used for a pretreatment step before granulation is carried out.
  • the particulate starting material prefferably be prepared at least in part by mixing in the high-speed mixer/granulator.
  • a dry-mixed starting powder may be prepared from its raw materials in the high-speed mixer/granulator; or one or more further ingredients may be admixed with an otherwise premixed powder prepared elsewhere (for example, by spray-drying).
  • a suitable stirring/cutting regime and residence time may be chosen in accordance with the materials to be mixed.
  • pulverisation Another possible pretreatment that may be carried out in the high-speed mixer/granulator is pulverisation; whether or not this is necessary depends, among other things, on the method of preparation of the starting powder and its free moisture content. Powders prepared by spray-drying, for example, are more likely to require pulverisation than powders prepared by dry-mixing. Again, the flexibility of the apparatus allows a suitable stirring/cutting regime to be chosen: generally relatively high speeds for both stirrer and cutter. A relatively short residence time (for example, 2-4 minutes for a 35 kg batch) is generally sufficient.
  • An essential feature of the process of the invention is the granulation step, during which densification to the very high values of at least 650 g/litre, preferably at least 700 g/litre occurs, giving a dense, granular product of very uniform particle size and generally spherical particle shape.
  • Granulation is effected by running the mixer at a relatively high speed using both stirrer and cutter; a relatively short residence time (for example, 5-8 minutes for a 35 kg batch) is generally sufficient.
  • the final bulk density can be controlled by choice of residence time, and it has been found that the powder properties of the resulting granulate are not optimum unless the bulk density has been allowed to rise to at least 650 g/litre.
  • binder preferably water
  • binder may be added before or during granulation, but some starting powders will inherently contain sufficient moisture.
  • the liquid binder it may be sprayed in while the mixer is running. In one preferred mode of operation, the mixer is first operated at a relatively slow speed while binder is added, before increasing the speed of the mixer to effect granulation.
  • pulverisation if required
  • granulation need not be regarded as separate process steps but as one single operation. Indeed, it is not, in that case, necessary to decide in advance whether or not pulverisation is required: the mixer may simply be allowed to do what is necessary, since the mixer conditions required are generally substantially the same for pulverisation and for granulation.
  • finely divided amorphous sodium aluminosilicate is admixed with the granular material after granulation is complete.
  • the amorphous sodium aluminosilicate is added while the granulate is still in the high-speed mixer/granulator, and the mixer is operated at a slow speed for a further short period. No further granulation occurs at this stage. It is also within the scope of the invention to add the amorphous sodium aluminosilicate to the granulate after removing the latter to different apparatus.
  • the granulation stage is preferably carried out at a controlled temperature somewhat above ambient, preferably above 30°C.
  • the optimum temperature is apparently formulation-dependent, but appears generally to lie within the range of from 30 to 45°C, preferably about 35°C. This temperature may also be maintained during the admixture of the finely divided amorphous sodium aluminosilicate.
  • the amorphous sodium aluminosilicate used in the process of the present invention is a finely divided particulate material.
  • the preferred average particle size is 0.1 to 20 ⁇ m, more preferably 1 to 10 ⁇ m.
  • a suitable material is available commercially from Crosfield Chemicals Ltd, Warrington, Cheshire, under the trade mark Alusil.
  • the amorphous sodium aluminosilicate is advantageously used in an amount of from 0.2 to 5.0 wt%, based on the starting powder, more preferably from 0.5 to 3.0 wt%.
  • This material is effective even at very low levels in improving flow properties, and also has the effect of increasing bulk density. It is therefore possible to adjust bulk density by appropriate choice of the level of amorphous aluminosilicate added after granulation.
  • amorphous material used in the process of the invention should be distinguisbed from zeolite (hydrated crystalline sodium aluminosilicate) which is substantially less weight-effective in the context of the present invention. Substantially higher levels than those quoted above are needed before any comparable flow or bulk density benefit is observed.
  • zeolite hydrated crystalline sodium aluminosilicate
  • the process of the invention may be used to densify and improve any detergent powder prepared by any tower or non-tower method, for example, spray-drying or dry mixing.
  • the particulate starting material may be prepared at least partially by mixing in the high-speed mixer/granulator itself.
  • the particulate starting material may consist at least partially of a spray-dried powder.
  • the process of the invention has been found to give especially satisfactory results with detergent base powders containing low to moderate levels of surfactant and relatively high levels of inorganic builder.
  • the process is used for the preparation of high-bulk-density powders containing substantial levels of sodium aluminosilicate builder.
  • These powders preferably contain not more than 5 wt% of phosphate builders, and are more preferably substantially free of phosphate builders.
  • a preferred starting powder might comprise:
  • the process of the invention is outstandingly suitable for preparing the high-bulk-density powders, containing moderate levels of surfactant and high levels of zeolite, described and claimed in our copending EP-A-340 013.
  • These powders comprise:
  • the aluminosilicate builder present in the starting powder may be crystalline or amorphous or a mixture thereof, and has the general formula 0.8-1.5 Na2O.Al2O3.0.8-6 SiO2.
  • aluminosilicates contain 1.5-3.5 SiO2 units (in the formula above) and have a particle size of not more than about 100 ⁇ m, preferably not more than about 20 ⁇ m. Both amorphous and crystalline aluminosilicates can be made readily by reaction between sodium silicate and sodium aluminate, as amply described in the literature.
  • Crystalline aluminosilicates are preferred in the low- or zero-phosphate starting powders treated by the process of the present invention. Suitable materials are described, for example, in GB-A-1 473 201 (Henkel) and GB-A-1 429 143 (Procter & Gamble).
  • the preferred sodium aluminosilicates of this type are the well-known commercially available zeolites A and X, and mixtures thereof. Type 4A zeolite is especially preferred.
  • the ratio of aluminosilicate builder (anhydrous basis) to total non-soap surfactant in the starting powder is preferably within the range of from 1.2:1 to 1.8:1.
  • the process is used for the preparation of high-bulk-density powders containing substantial levels of water-soluble inorganic salts, including sodium tripolyphosphate and/or sodium carbonate.
  • a preferred starting powder might comprise:
  • the weight ratio of (y) to (x) is within the range of from 0.4:1 to 9:1, more preferably from 1:1 to 9:1.
  • An especially preferred starting powder contains from 15 to 70 wt% of water-soluble inorganic salts, more preferably from 15 to 50 wt%, especially from 20 to 40 wt%, of sodium tripolyphosphate.
  • the non-soap surfactant present in the starting powder preferably consists at least partially of anionic surfactant.
  • anionic surfactants will be well known to those skilled in the art, and include linear alkylbenzene sulphonates, particularly sodium linear alkylbenzenesulphonates having an alkyl chain length of C8-C15; primary and secondary alkyl sulphates, particularly sodium C12-C15 primary alcohol sulphates; alkyl ether sulphates; alpha-olefin and internal olefin sulphonates; alkane sulphonates; dialkyl sulphosuccinates; fatty acid ester sulphonates; and combinations thereof.
  • the starting powder may contain nonionic surfactant.
  • Nonionic surfactants too will be well known to those skilled in the art, and include primary and secondary alcohol ethoxylates, especially the C12-C15 primary and secondary alcohols ethoxylated with an average of from 3 to 20 moles of ethylene oxide per mole of alcohol.
  • the surfactant component of the starting powder may be constituted by from 0 to 70%, preferably from 8 to 60% by weight, of anionic surfactant, and from 0 to 20%, preferably from 0 to 10%, by weight of nonionic surfactant.
  • non-soap surfactant for example, cationic, zwitterionic, amphoteric or semipolar surfactants, may also be present if desired.
  • suitable detergent-active compounds are available and are fully described in the literature, for example, in "Surface-Active Agents and Detergents", Volumes I and II, by Schwartz, Perry and Berch.
  • soap may also be present, to provide foam control and additional detergency and builder power; soap is not included in the figures for the surfactant content quoted previously.
  • the final granulate has a bulk density of at least 650 g/litre and preferably at least 700 g/litre. It is also characterised by an especially low particle porosity, not exceeding 0.25 and preferably not exceeding 0.20, which distinguishes it from even the densest powders prepared by spray-drying alone.
  • the final granulate may be used as a complete detergent composition in its own right. Alternatively, it may be admixed with other components or mixtures prepared separately, and may form a major or minor part of a final product. Generally any additional ingredients such as enzymes, bleach and perfume that are not suitable for undergoing the granulation process may be admixed to the granulate to make a final product.
  • a detergent base powder may, for example, be prepared by spray-drying an aqueous slurry of heat-insensitive and compatible ingredients; if desired, other ingredients may then be admixed; and the resulting powder densified and granulated in accordance with the present invention. Yet further ingredients may if desired be admixed after granulation; the densified granulate may typically constitute from 40 to 100 wt% of a final product.
  • a detergent base powder may be prepared by dry mixing one or more raw materials and/or one or more premixes of raw materials, in the high-speed mixer/granulator itself or in other apparatus, and then densified and granulated in accordance with the present invention. Again, further ingredients may if desired be added after granulation.
  • the granulate prepared in accordance with the present invention may be an "adjunct" comprising a relatively high level of detergent-active material on an inorganic carrier; and this may be admixed in a minor amount with other ingredients to form a final product.
  • a detergent composition having a bulk density of 350 g/litre was prepared to the following composition by spray-drying an aqueous slurry: % Linear alkylbenzene sulphonate 20.0 Nonionic surfactant 2.0 Soap 1.0 Zeolite (anhydr.) 35.0 Water with zeolite 10.0 Sodium silicate 4.0 Sodium succinate 2.0 Acrylate/maleate copolymer 2.0 Sodium sulphate 10.45 Sodium carbonate 10.0 Minor ingredients 1.55 Free moisture 2.0 100.0
  • Alusil Trade Mark fine amorphous sodium aluminosilicate (250 g, 1%) was introduced into the Fukae mixer, which was then operated at a slow speed (stirrer 90 rpm, cutter 300 rpm) for 1 minute. The resulting granular product was free-flowing and showed no tendency to cake. Its properties, and those of a sample removed before the addition of the Alusil, are shown in Table 1 below.
  • Example 2 3 A B Flow aid (wt %): Alusil 1.0 1.7 - - Zeolite - - 1.0 3.0 Bulk density (g/l) 856 854 740 784 Dynamic flow rate (ml/s) 92.3 92.3 33.5 42.5 Particle size ( ⁇ m) 507 546 530 529 Fines content (wt% ⁇ 180 ⁇ m) 11 8 2 1
  • This Example describes the preparation of a complete detergent product using the process of the invention.
  • a detergent composition was prepared to the following composition by spray-drying an aqueous slurry to a free moisture content of substantially zero: parts Linear alkylbenzene sulphonate 24.0 Nonionic surfactant 2.0 Soap 1.0 Zeolite (anhydr.) 38.0 Water with zeolite 10.84 Sodium silicate 4.0 Acrylate/maleate copolymer 2.0 Minor ingredients 2.0 Sodium carbonate 10.0 94.64
  • Example 4 35 kg of the spray-dried powder used in Example 4 were introduced into a Lödige (Trade Mark) FM series high-speed mixer/granulator, and pulverised for 4 minutes. Water (1.1 kg, 3.5%) was then sprayed in while the mixer continued to run at the same speed, then the mixer was allowed to run for a further 3 minutes while the temperature was maintained at about 35°C. During this period granulation occurred.
  • a sample (Comparative Example C) was removed from the mixer and its properties are shown in Table 3 below.
  • Alusil (Trade Mark) finely divided amorphous sodium aluminosilicate (1.2 kg) was then introduced into the mixer which was allowed to run for a further 0.5 minutes.
  • the properties of the resulting powder (Example 5) are shown in Table 3 below, from which the benefits of adding a flow aid after granulation is complete are apparent.
  • the presence of the Alusil did result in an increase in the content of fine particles ⁇ 180 ⁇ m, but not to an unacceptable level.
  • Comparative Example D The procedure of Comparative Example D was repeated, but the Alusil was added before the pulverisation step instead of after it. Pulverisation and granulation were carried out as in previous Examples, but the resulting product had a dynamic flow rate of zero.
  • Example 4 20 kg of the spray-dried powder used in Example 4 were introduced into a Fukae (Trade Mark) FS-30 high-speed mixer/granulator, and pulverised for 4 minutes. Water (0.8 kg) was then added and the mixture granulated over a period of 4 minutes, while the temperature was maintained at about 35°C. A sample (Comparative Example F) was removed from the mixer and its powder properties determined: these are shown in Table 4 below.
  • Fukae Trade Mark
  • Example 4 20 kg of the spray-dried powder used in Example 4 were introduced into the Fukae high-speed mixer/granulator, and pulverised for 4 minutes. Alusil (Trade Mark) finely divided amorphous sodium aluminosilicate (0.2 kg) was then introduced into the mixer. Water (0.8 kg) was then added and the mixture granulated over a period of 4 minutes, while the temperature was maintained at about 35°C. Physical properties of the resulting powder are shown in Table 4 below: the results were similar to those obtained using the Lödige mixer (Comparative Example D).
  • the ratio of aluminosilicate to non-soap surfactant in this mixture was 1.46.
  • the powder properties of the granulate before and after the addition of Alusil were as follows: H 7 Bulk density (g/l) 750 810 Dynamic flow rate (ml/s) 80 96 Compressibility ( %v/v) 17.0 15.3 Particle size ( ⁇ m) - 607 Particle porosity ⁇ 0.20 ⁇ 0.20
  • a detergent powder built with sodium tripolyphosphate was prepared by spray-drying an aqueous slurry to the following formulation: wt % Linear alkylbenzene sulphonate 9.7 Nonionic surfactant 2.8 Soap 4.9 Sodium tripolyphosphate 42.5 Sodium sulphate 14.8 Sodium silicate 10.0 Minor ingredients 2.8 Water 12.5 100.0
  • the ratio of water-soluble crystalline inorganic salts (sodium tripolyphosphate and sodium sulphate) to non-soap surfactant was 4.6:1.
  • Example 8 To the first sample (Example 8), Alusil (1.5 wt% ) was added over a period of 1 minute while the mixer was operated at a stirrer speed of 90 rpm and a cutter speed of 300 rpm.
  • Powder properties were as follows: 8 J Yield ⁇ 1700 ⁇ m (wt%) 93 97 Average particle size ( ⁇ m) 555 480 Bulk density (g/litre) 840 780 Dynamic flow rate (ml/s) 92 61 Compressibility (%v/v) 7 12 Particle porosity ⁇ 0.20 ⁇ 0.20
  • This Example illustrates the sequential addition of zeolite and Alusil to a densified powder.
  • a detergent base powder was prepared to the following composition by spray-drying an aqueous slurry to a free moisture content of substantially zero:
  • the weight ratio of anhydrous zeolite to non-soap detergent in this base powder was 1.05:1.

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Claims (13)

  1. Verfahren für die Herstellung einer körnigen Waschmittelzusammensetzung oder einer Komponente mit einer Schüttdichte von zumindest 650 g/ℓ, dadurch gekennzeichnet, daß es die nachfolgenden Stufen umfaßt:
    (i) Behandeln eines teilchenförmigen Materials, enthaltend ein oder mehrere seifenfreie detergentaktive Verbindungen und einen oder mehrere anorganische Builder in einem Hochgeschwindigkeitsmischer/Granulator, der sowohl eine Rührwirkung und eine Schneidwirkung hat, in Anwesenheit eines flüssigen Bindemittels, wodurch die Granulierung und die Verdichtung zu einer Schüttdichte von zumindest 650 g/ℓ bewirkt werden,
    (ii) anschließend an die Granulierung und Verdichtung von Stufe (i) Zumischen von feinzerteiltem amorphen Natriumaluminosilicat zu dem in Stufe (i) erhaltenen körnigen Material.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das feinzerteilte amorphe Natriumaluminosilicat in einer Menge von 0,2 bis 5,0 Gewichtsprozent, auf Basis der gesamten Zusammensetzung, zugegeben wird.
  3. Verfahren nach irgendeinem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß die Stufe (ii) auch in dem Hochgeschwindigkeitsmischer/Granulator durchgeführt wird.
  4. Verfahren nach irgendeinem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß die Granulierung in einem schüsselförmigen Hochgeschwindigkeitsmischer/Granulator mit einer im wesentlichen vertikalen Rührerachse durchgeführt wird.
  5. Verfahren nach irgendeinem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial zumindest teilweise aus sprühgetrocknetem Pulver besteht.
  6. Verfahren nach irgendeinem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial zumindest zum Teil durch Mischen in dem Hochgeschwindigkeitsmischer/Granulator vor der Granulierung hergestellt ist.
  7. Verfahren nach irgendeinem der vorhergehenden Ansprüche, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial enthält:
    (a) Von 5 bis 35 Gewichtsprozent an nichtseifigem detergentaktivem Material, und
    (b) von 28 bis 45 Gewichtsprozent (wasserfreie Basis) an kristallinem oder amorphem Natriumaluminosilicat,
    wobei das Gewichtsverhältnis von (b) zu (a) zumindest 0,9 : 1 beträgt, und gegebenenfalls andere Waschmittelkomponenten bis zu 100 Gewichtsprozent.
  8. Verfahren nach Anspruch 7, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial enthält:
    (a) Von 17 bis 35 Gewichtsprozent an nichtseifigem detergentaktivem Material, bestehend zumindest teilweise aus anionischem detergentaktivem Material, und
    (b) von 28 bis 45 Gewichtsprozent (wasserfreie Basis) an kristallinem oder amorphem Natriumaluminosilicat,
    wobei das Gewichtsverhältnis von (b) zu (a) von 0,9 : 1 bis 2,6 : 1 beträgt, und gegebenenfalls andere Waschmittelkomponenten bis zu 100 Gewichtsprozent.
  9. Verfahren nach Anspruch 7 oder Anspruch 8, dadurch gekennzeichnet, daß das Aluminosilicat (b) in dem teilchenförmigen Ausgangsmaterial ein kristalliner Zeolith ist.
  10. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial enthält:
    (x) Von 12 bis 70 Gewichtsprozent nichtseifiges detergentaktives Material, und
    (y) zumindest 15 Gewichtsprozent an wasserlöslichen kristallinen anorganischen Salzen, einschließend Natriumtripolyphosphat und/oder Natriumcarbonat,
    wobei das Gewichtsverhältnis von (y) zu (x) zumindest 0,4 : 1 beträgt, und gegebenenfalls andere Waschmittelkomponenten bis zu 100 Gewichtsprozent.
  11. Verfahren nach Anspruch 10, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial ein Verhältnis von (y) zu (x) innerhalb des Bereiches von 1 : 1 bis 9 : 1 aufweist.
  12. Verfahren nach einem der Ansprüche 10 oder 11, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial von 15 bis 70 Gewichtsprozent kristalliner anorganischer Salze, einschließend Natriumtripolyphosphat und/oder Natriumcarbonat, enthält.
  13. Verfahren nach Anspruch 12, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial von 15 bis 50 Gewichtsprozent Natriumtripolyphosphat enthält.
EP89304205A 1988-04-29 1989-04-27 Verfahren zur Herstellung von Waschmittelzusammensetzungen Expired - Lifetime EP0339996B1 (de)

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GB8810194 1988-04-29
GB888810194A GB8810194D0 (en) 1988-04-29 1988-04-29 Process for preparing detergent compositions
GB888817386A GB8817386D0 (en) 1988-07-21 1988-07-21 Detergent compositions & process for preparing them
GB8817386 1988-07-21

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EP0339996B1 true EP0339996B1 (de) 1993-07-07

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Families Citing this family (17)

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GB8810193D0 (en) * 1988-04-29 1988-06-02 Unilever Plc Detergent compositions & process for preparing them
EP0367339B1 (de) * 1988-11-02 1996-03-13 Unilever N.V. Verfahren zur Herstellung einer körnigen Reinigungsmittelzusammensetzung mit hoher Schüttdichte
GB8926718D0 (en) * 1989-11-27 1990-01-17 Unilever Plc Process for the preparation of detergent compositions
GB9007999D0 (en) * 1990-04-09 1990-06-06 Unilever Plc Particulate bleaching detergent composition
GB9008013D0 (en) * 1990-04-09 1990-06-06 Unilever Plc High bulk density granular detergent compositions and process for preparing them
GB9012613D0 (en) * 1990-06-06 1990-07-25 Unilever Plc Soap powder compositions
CA2027518A1 (en) * 1990-10-03 1992-04-04 Richard L. Tadsen Process for preparing high density detergent compositions containing particulate ph sensitive surfactant
DE4216774A1 (de) * 1992-05-21 1993-11-25 Henkel Kgaa Verfahren zur kontinuierlichen Herstellung eines granularen Wasch und/oder Reinigungsmittels
USH1604H (en) * 1993-06-25 1996-11-05 Welch; Robert G. Process for continuous production of high density detergent agglomerates in a single mixer/densifier
US5968891A (en) * 1993-07-13 1999-10-19 Colgate-Palmolive Co. Process for preparing detergent composition having high bulk density
EP0643129A1 (de) * 1993-09-07 1995-03-15 The Procter & Gamble Company Verfahren zur Herstellung von Waschmittelzusammensetzungen
US5431857A (en) * 1994-01-19 1995-07-11 The Procter & Gamble Company Process for producing a high density detergent composition having improved solubility by agglomeration of anionic surfactants and an agglomerating agent
DE4429550A1 (de) * 1994-08-19 1996-02-22 Henkel Kgaa Verfahren zur Herstellung von Wasch- oder Reinigungsmitteltabletten
US5565422A (en) * 1995-06-23 1996-10-15 The Procter & Gamble Company Process for preparing a free-flowing particulate detergent composition having improved solubility
EP0912716A1 (de) * 1996-05-07 1999-05-06 The Procter & Gamble Company Verfahren zur herstellung agglomerierte waschmittel mit verbesserte fliespfähigkeit
KR100448993B1 (ko) * 1997-09-09 2004-11-26 씨제이 주식회사 입상고밀도비이온성세제조성물및그제조방법
DE19801186A1 (de) 1998-01-15 1999-07-22 Henkel Kgaa Verfahren zur Herstellung gefärbter Wasch- und Reinigungsmittel

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1617109B2 (de) * 1967-12-05 1973-04-19 Großeinkaufs Gesellschaft deutscher Konsumgenossenschaften mbH, 2000 Harn bürg Verfahren zur herstellung von staubfreien und rieselfaehigen waschund reinigungsmitteln
JPS6072999A (ja) * 1983-09-30 1985-04-25 花王株式会社 超濃縮粉末洗剤の製法
JPH0672237B2 (ja) * 1984-09-14 1994-09-14 花王株式会社 流動性の改良された高密度の粒状洗剤の製法
DE3617756C2 (de) * 1985-05-29 1995-01-19 Lion Corp Verfahren zum Herstellen einer granularen Detergentien-Zusammensetzung mit hoher Schüttdichte
GB8810193D0 (en) * 1988-04-29 1988-06-02 Unilever Plc Detergent compositions & process for preparing them

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
DATABASE WPIL no. 133904, 1986, Derwent Publication *
DATABASE WPIL no. 6662309, 1989, Derwent Publication *
PATENT ABSTRACTS OF JAPAN vol. 2, no. 59, 27 April 1978 *

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KR920000113B1 (ko) 1992-01-09
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KR890016153A (ko) 1989-11-28
AU611555B2 (en) 1991-06-13
DE68907438T2 (de) 1993-10-14
MY104968A (en) 1994-07-30
BR8902005A (pt) 1989-12-05
HK47894A (en) 1994-05-20
CA1323277C (en) 1993-10-19
JPH0249100A (ja) 1990-02-19
EP0339996A1 (de) 1989-11-02
TR25924A (tr) 1993-09-17
PH25538A (en) 1991-07-24
DE68907438D1 (de) 1993-08-12

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