+

WO1999032599A1 - Procede de production de particules - Google Patents

Procede de production de particules Download PDF

Info

Publication number
WO1999032599A1
WO1999032599A1 PCT/GB1998/003791 GB9803791W WO9932599A1 WO 1999032599 A1 WO1999032599 A1 WO 1999032599A1 GB 9803791 W GB9803791 W GB 9803791W WO 9932599 A1 WO9932599 A1 WO 9932599A1
Authority
WO
WIPO (PCT)
Prior art keywords
anionic surfactant
surfactant
builder
extruder
extrusion
Prior art date
Application number
PCT/GB1998/003791
Other languages
English (en)
Inventor
John Hibbs
Original Assignee
Manro Performance Chemicals Limited
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Manro Performance Chemicals Limited filed Critical Manro Performance Chemicals Limited
Publication of WO1999032599A1 publication Critical patent/WO1999032599A1/fr

Links

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
    • C11D17/00—Detergent materials or soaps characterised by their shape or physical properties
    • C11D17/06—Powder; Flakes; Free-flowing mixtures; Sheets
    • 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

Definitions

  • This invention relates to a method of manufacturing surfactant particles comprising an anionic surfactant.
  • Some processes seek to overcome the problems by using pre-dried surfactant, typically produced by spray-drying.
  • a small amount of liquid is added to act as a binding agent.
  • a further limitation of conventional agglomeration systems is that they tend to give a granule of lower bulk density than the feed materials, due to the inclusion of air in the granules.
  • EP-A-349200 describes a process for making dense, concentrated detergent granules from a surfactant paste using fine dispersion cold granulation.
  • a preferred temperature range is from about -30°C to about 0°C.
  • the surfactant paste can be introduced into the mixer at an initial temperature in the range about 5-70°C, especially about 20-30°C; it is stated that a temperature greater than about 70°C can lead to poor initial mixing due to increased product stickiness.
  • the paste is preferably cooled to the granulation temperature by addition of dry ice.
  • EP-A-340966 describes a process of making a high density particulate detergent composition, involving turbodrying a mixture of an anionic surfactant, water and bentonite.
  • turbodryer subjects the mixture to centrifugal and axial forces while it is being dried.
  • US-A-5290496 describes a process for manufacturing granules by a process in which detergent components are mixed together to form a free-flowing premix, for charging a homogenizing unit, for example a twin-screw kneader in which it is kneaded at a moderate temperature, for example at a temperature of 45° to 60°C, and then extruded through specially designed bores in an extruder head, which may be heated to the predetermined extrusion temperature, for example to around 45 to 50°C. The resulting strands are then pelletized.
  • the temperature of the "molding compound" in the kneader is said to be an important parameter. Those molding compounds which are temperature sensitive may have to be cooled during the process to prevent destruction.
  • the temperature of the mass immediately prior to its extrusion is at least 60°C; more preferably at least 70°C; most preferably at least 80°C.
  • the temperature of the material may increase a few degrees as it is forced through the extrusion head.
  • a specially designed extrusion head as there is with the method of US-A-5290496.
  • any ordinary multi-aperture axial or radial extrusion head may be used.
  • the apertures thereof may comprise plain cylindrical apertures of diameter not exceeding 2 mm; 0.5- 1.5 mm is a preferred range.
  • Such apertures may be entirely cylindrical or may have a funnel portion on their upstream side, tapering to the main, cylindrical portion.
  • the maximum temperature of the mass during the method should be such that there is no significant degradation.
  • preferred sulphate and sulphonate anionic surfactants may be taken to temperatures well in excess of 80°C, without significant degradation; and in some cases up to 130°C.
  • the maximum temperature of the material at any stage of the method does not exceed 100°C.
  • the mass within the extruder is in a plastic and/or semi-solid form at least when it reaches the extrusion head.
  • the mass is plastic and/or semi-solid when it is mechanically worked within the extruder.
  • the mass is at an elevated temperature when mechanically worked, suitably at least 40°C; preferably at least 60°C; more preferably at least 70°C; most preferably at least 80°C.
  • the feed material is added to the extruder at a temperature of at least 40°C, more preferably at least 60°C. It may be added as a solid or in plastic or molten form.
  • the feed material is preferably an anionic surfactant paste, whose activity (i.e. anionic surfactant content) is suitably at least 40%wt, preferably at least 70%wt, most preferably at least 90%wt.
  • the dried product is a waxy or pasty solid at ambient temperature, not a flowable powder.
  • a feed material comprises an anionic surfactant which contains 2-10%wt of water, and whose activity is 90-98%wt. It is found that the presence of this water aids the processing of the surfactant, within the extruder and/or during a downstream spheronisation step, if carried out.
  • a dried surfactant may be employed in the feed material, and there may be a separate addition of water to aid processing, either when the feed material is introduced to the extruder, or subsequently.
  • the amount of water present after the addition may be as defined above. In preferred methods however no water is added to the extruder and the desired amount of water is preferably controlled by control of the water content of the feed material. This is preferably controlled not by adding water to a dried anionic surfactant, but by removing water to the extent required, in a prior surfactant drying process.
  • the feed material is dried immediately prior to its introduction into the extruder.
  • it is fed directly from a drier to the extruder, without being actively cooled therebetween.
  • a non-ionic surfactant may aid the processing of the anionic surfactant within the extruder, and/or their downstream handling.
  • an anionic surfactant and a non-ionic surfactant are present.
  • the weight ratio of non-ionic surfactant to the anionic surfactant is suitably up to 1 part, preferably up to 0.5 parts, of non-ionic surfactant per part of anionic surfactant (with reference to their active contents).
  • the higher alkyl group of such anionic surfactants is of 8 to 24, especially 10 to 20 carbon atoms, preferably 12 to 18 carbon atoms, and the alkoxylate content of such anionic surfactants that are alkoxylated (preferably ethoxylated or ethoxylated/propoxylated) is in the range of 1 to 4 alkoxy groups per mole.
  • a preferred non-ionic surfactant is a condensation product of a higher fatty alcohol with a lower alkylene oxide, such as ethylene oxide or a mixture of ethylene oxide and propylene oxide.
  • a lower alkylene oxide such as ethylene oxide or a mixture of ethylene oxide and propylene oxide.
  • the higher fatty moiety will normally be of 12 to 15 carbon atoms and there will usually be present from 3 to 20, preferably 4 to 15 moles of alkylene oxide per mole of higher fatty alcohol.
  • the particles contain a builder.
  • a builder in particulate form is suitably added to the material comprising the anionic surfactant during or, preferably, prior to the mechanical working thereof.
  • the builder is preferably not present during the drying step. It is preferably introduced subsequently, for example added to the material comprising the anionic surfactant prior to feeding into the extruder; at the time that material is fed into the extruder; or, preferably, subsequent to the feeding of the material comprising the anionic surfactant into the extruder, through a separate feed point.
  • the builder when present, is added to the material comprising the anionic surfactant within the extruder during or, preferably, prior to the mechanical working thereof, said material already being at an elevated temperature, preferably at least 40°C, more preferably at least 60°C.
  • Suitable builders include water soluble inorganic salt builders, preferably sodium salts, such as sodium polyphosphates, e.g. sodium tripolyphosphate and sodium pyrophosphate, sodium carbonate, sodium bicarbonate, sodium sesquicarbonate , sodium silicate, sodium disilicate, sodium metasilicate and sodium borate.
  • water insoluble builders may also be useful, including the ion exchanging zeolites, such as Zeolite 4A.
  • Organic builders may be employed but if heat sensitive may need to be added after extrusion.
  • suitable organic builders are polyacetal carboxylates, as described in US-B-4725455, and water soluble salts of lower hydroxycarboxylic acids, such as sodium citrate and sodium gluconate.
  • a builder when present, may suitably be present in an amount of from 0.1-10 parts per part of the anionic surfactant (active content), by weight.
  • the anionic surfactant is, or is predominantly, an alkali metal alkyl sulphate
  • the builder may suitably be present in an amount of from 0.2-6 parts per part of the anionic surfactant (active content), by weight, preferably 0.5-5, most preferably 0.7-4 parts, by weight.
  • the builder may suitably be present in an amount of from 0.1-5 parts per part of the anionic surfactant (active content), by weight, preferably 0.1-1, most preferably 0.15-0.5 parts, by weight.
  • a component for example a builder
  • proportions of constituents are given herein there refer to the total content of the respective components , for example the total content of builders.
  • the main ingredients of the extruded particles are preferably anionic surfactant and builder.
  • Other constituents discussed already are water and non-ionic surfactant.
  • adjuvants may be desirable for eventual detergent formulations. These may include a polymer, bleaching agent, optical brightener, sequestrant, conditioning agent, anti-foaming agent, filler, colorant, soil release agent, enzyme etc.
  • a hydrotrope may be a useful adjuvant, firstly in preventing the anionic surfactant from becoming sticky as a result of water content and/or water absorption, and secondly in aiding washing processes, by promoting good dissolution. Examples of suitable hydrotropes are alkali metal arylsulphonates, for example sodium xylene sulphonate and sodium toluene sulphonate.
  • adjuvants can be added to the material comprising the anionic surfactant prior to extrusion; for example prior to a prior drying step (when carried out); or subsequent to a prior drying step (when carried out) but prior to feeding of the material comprising the anionic surfactant into the extruder; or at the same time as that material is fed into the extruder; or subsequent to the feeding of the material comprising the anionic surfactant into the extruder, through one or more separate feed points, for example during or, preferably, prior to the mechanism working.
  • adjuvants may be blended with the particles after their extrusion and cooling.
  • adjuvants which are heat sensitive, such as enzymes post-extrusion blending may be preferred.
  • the method of the present invention may produce particles which constitute a ready-to-use multi-component detergent or an intermediate product to be admixed or incorporated with other components, to produce a product for sale.
  • an anionic surfactant in the form of a solid, semi-solid or paste is preferably fed in. It may be fed in in whatever way is most convenient - for example in lumps or shavings, or poured or pumped in. Other components may be co-fed, without a requirement for them to be carefully blended in; or may be added downstream, via one or more separate feed points.
  • the mixing required to produce a good distribution of the components takes place within the extruder at an elevated temperature; and the mixing takes place most efficiently at temperatures which have previously been considered too high for the processing of the preferred sulphate and sulphonate anionic surfactants.
  • the material in the extruder is plastic and/or semi-solid, and highly workable, at the temperature employed.
  • the temperature of the material as it is extruded is higher than the melting or softening point of the anionic surfactant.
  • the method may produce a granule containing a builder and an anionic surfactant, the primary elements of a detergent formulation, in one straightforward step from the as-supplied builder and surfactant; or in two steps if a prior drying step is employed, for drying the surfactant. No prior agglomeration step is required; indeed no prior mixing step of any kind is required, although prior mixing of certain adjuvants may be carried out, if this is the favoured way of incorporating them.
  • an anionic surfactant, and a builder and other components when present, form an extrudate which has very good physical characteristics, even at temperatures at which the surfactant would normally be in a liquid state, and/or expected to hydrolyse or otherwise degrade.
  • This allows intensive mixing within the extruder barrel, without the need for significant cooling of the mass prior to extrusion.
  • compositions may be treated as a "dried” (solid) surfactant ingredient, without a downstream drying process; in preferred processes no forced or active drying process is carried out downstream of the extruder.
  • the particles produced by the present invention are particularly suitable for use by formulators of laundry powders to deliver multiple ingredients into products .
  • the particles may be admixed into a particulate blend of other ingredients, or may be partly ground, and re- agglomerated to give a fully formulated product.
  • the prior art practice is to simply admix particles of relatively pure surfactant, particularly alkyl sulphates, into a powder.
  • the invention offers the same ease of incorporation, with the benefits arising from the prior intimate mixing of the alkyl sulphate with other, often more readily soluble components. In the latter case, ease of formulation is improved by the delivery of multiple components, in the correct formulation ratio, suitably obtained by the process of the invention via a single solids addition.
  • the invention offers a form of product which would be difficult for formulators to achieve without special equipment to make a densified powder.
  • the process used is also more efficient than many formulators' own drying and blending operations, offering energy savings and reduced inventory.
  • APV MP 2050 (trade mark) twin screw mixer-extruder was used, with 50 mm diameter screws, and a L:D ratio of 30:1.
  • the barrel of the extruder was electrically heated and water cooled, with independently controlled heating zones. Unless otherwise stated the temperature was measured by means of thermocouples set into the inside surface of the barrel, at intervals along it.
  • the extrusion was either axial extrusion through a standard 0.9 mm noodle plate or radial extrusion via a radial extrusion head, using a 1 mm mesh.
  • the radial extrusion head allowed greater throughputs, and lower operating pressures. In general, for axial extrusions the operating pressures were relatively low, about 10 bar unless otherwise stated. For radial extrusions very low pressures were used; essentially no significant over pressure was applied.
  • the anionic surfactant feeds were metered into the extruder using a weight-belt feeder. Builders and other solid ingredients were added using a screw feeder, with a loss in weight system. The builders were added at a distance of 9D from the surfactant feed. This allowed the surfactant feeds to be heated and worked, to become fully plastic, before builders were added.
  • Extrudate temperature itself was measured by quickly collecting a mass of extrudate and immediately measuring the temperature in the centre of the mass by means of a thermocouple probe. Liquid additions were made using a volumetric pump.
  • the particles were chopped into pieces in standard manner and then spheronisation was carried out in each case, using a CALEVA (trade mark) model 15 Disc spheroniser to give roughly spherical particles of approximately 1 mm diameter.
  • CALEVA trade mark
  • the surfactant used was a paste of sodium alkyl sulphate, based on a C 16.18 alcohol, containing about 70% surfactant (the remainder being water, sodium hydroxide, sodium sulphate, and unreacted alcohol), known as MANRO SNO (trade mark).
  • MANRO SNO trade mark
  • the molten as-prepared paste was allowed to cool until it solidified, and was broken into small pieces, to allow it to be fed into the extruder.
  • the surfactant portion of the formulation was added as a molten liquid at about 80°C. It was observed that the temperature profile along the extruder barrel reflected the initial high temperature of the molten feed but from the mixing zone on, there was no significant difference between molten feed and solid feed. It was also demonstrated that using this form of feed material the extrudate could be produced at a rate of 80 kg/hr.
  • the surfactant feed was based on sodium alkylbenzene sulphonate (LAS).
  • the feed was made by drying a paste of 60% active LAS in a BALESTRA DRYEX (trade mark) wiped film evaporator, to an active content of 96-98%.
  • the dried LAS was fed straight into the main feed port of the extruder at a temperature of 60°C, at a rate of 36.5 kg/hr.
  • the surfactant was heated to 80°C and conveyed and to the mixing zone.
  • the builder used was a blend of zeolite (VEGOBOND AX - trade mark) and sodium carbonate, in the ratio 3:1 wt:wt.
  • the addition rate of builder was 27 kg/hr.
  • the product was axially extruded through the 0.9 mm noodle die, at a higher pressure of 30 bar in this example, with an extrudate temperature of 90- 100°C.
  • Sodium C 12 . 18 alkyl sulphate paste was previously dried, as described in the example above.
  • the surfactant was fed into the extruder at a rate of 37.1 kg/hr. This was conveyed and heated to about 80°C.
  • the builder was then added at a rate of 30.8 kg/hr.
  • the builder was sodium disilicate and sodium carbonate, 3:1 wt:wt. It was observed that a small water addition (2.1 kg/hr) improved the downstream spheroniser performance.
  • the extrusion was carried out using the radial extrusion head, with an extrusion temperature of 101°C.
  • the product obtained contained 53% (w/w) of surfactant, 4% water and had a bulk density of 730 g/1.
  • This product also gave a significant improvement in spheroniser performance, the product being more evenly sized with less dusting and reduced the extrusion temperature to 88°C, due to lesser heat gain during the passage through the extrusion head.
  • This product contained 54% of anionic surfactant, 5% of non-ionic surfactant, and had a bulk density of 750 g/1.
  • the dried sodium alkyl sulphate was fed at a rate of 18.2 kg/hr. This was conveyed and heated as previously.
  • the builder (VEGOBOND AX zeolite only) was added at a rate of 29.3 kg/hr, and non-ionic surfactant was added at a rate of 2.5 kg/hr.
  • the extrusion was via the axial head, at a temperature of 84°C.
  • the product obtained contained 37% anionic surfactant, 5.2% non-ionic surfactant, and had a bulk density of 640 g/1.
  • Dried sodium alkyl sulphate was fed as previously, at a rate of 10.7 kg/hr.
  • Builder VEGOBOND AX zeolite : sodium carbonate, 11:1 wt:wt
  • non-ionic surfactant was added at a rate of 4 kg/hr
  • an acrylic-maleic polymer SOKOLAN CP5 (trade mark - an ingredient useful in laundry formulations) was added at a rate of 2.7 kg/hr.
  • the temperature of the extrudate from the radial extruder was 80°C.
  • the composition spheronised well.
  • the product contained 20.2% anionic surfactant, 7.6% non-ionic surfactant, 5% polymer, and had a bulk density of 720 g/1.
  • Sodium C 12 . 16 alkyl sulphate paste was dried as described in example 2.
  • the surfactant was fed into the extruder at a rate of 50.0 kg/hr. This was conveyed and heated to 80°C. No builder or other components were added.
  • the extrusion was carried out using the axial extrusion head with an extrusion temperature of 101°C.
  • the product obtained was substantially pure surfactant particles of very high activity, and of bulk density of 600-750 g/1. The resultant particles could be handled and spheronised without difficulty.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Detergent Compositions (AREA)

Abstract

Procédé de production de particules pour détergent à lessive. Le procédé est un procédé d'extrusion dans lequel un adjuvant pour détergent et un tensioactif, ce dernier contenant en tant que constituant principal un tensioactif anionique sulfaté ou sulfoné, sont envoyés dans une extrudeuse, travaillés mécaniquement à une température au moins égale à 40 °C puis extrudés par une tête d'extrudeuse comportant une multitude d'orifices d'extrusion. Le procédé d'extrusion permet de produire des particules de détergent ayant une masse volumique apparente qui est au moins égale à 400g/l et qui est de préférence comprise entre 550 et 900 g/l.
PCT/GB1998/003791 1997-12-19 1998-12-17 Procede de production de particules WO1999032599A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9726824.7 1997-12-19
GBGB9726824.7A GB9726824D0 (en) 1997-12-19 1997-12-19 Method of manufacturing particles

Publications (1)

Publication Number Publication Date
WO1999032599A1 true WO1999032599A1 (fr) 1999-07-01

Family

ID=10823870

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/GB1998/003791 WO1999032599A1 (fr) 1997-12-19 1998-12-17 Procede de production de particules

Country Status (2)

Country Link
GB (1) GB9726824D0 (fr)
WO (1) WO1999032599A1 (fr)

Cited By (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001085893A1 (fr) * 2000-05-05 2001-11-15 The Procter & Gamble Company Procede de production de constituants nettoyants solides
WO2002102959A1 (fr) * 2001-06-19 2002-12-27 Henkel Kommanditgesellschaft Auf Aktien Produit de lavage et/ou produit de nettoyage pauvre en zeolithe et stable au stockage
WO2004027009A1 (fr) * 2002-09-12 2004-04-01 Henkel Kommanditgesellschaft Auf Aktien Produits de lavage ou de nettoyage comprimes sous l'effet d'une pression
WO2010014395A1 (fr) * 2008-07-28 2010-02-04 The Procter & Gamble Company Procédé pour la préparation d’une composition détergente
EP2243822A1 (fr) 2009-04-24 2010-10-27 Unilever PLC Poudre détergente dotée de particules riches en détergent
WO2010122051A1 (fr) 2009-04-24 2010-10-28 Unilever Plc Particules de détergent hautement actives
WO2010122050A2 (fr) 2009-04-24 2010-10-28 Unilever Plc Fabrication de particules détergentes extrêmement actives
EP2441820A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Particules de détergent pour le lavage du linge
EP2441821A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Particules de détergent pour le lavage du linge
EP2441825A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Procédé pour la préparation de particules de détergent pour le lavage du linge
EP2441822A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Particules de détergent pour le lavage du linge
WO2012048947A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2012048949A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particule de détergent à lessive
WO2012048950A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2012048948A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2012049178A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent pour lessive
WO2012049033A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Procédé à cuve à laver le linge à chargement par le haut
WO2012048951A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2013149755A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
WO2013149753A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
WO2013149754A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
WO2013149752A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
US8883702B2 (en) 2010-10-14 2014-11-11 Conopco, Inc. Packaged particulate detergent composition
US9062281B2 (en) 2010-10-14 2015-06-23 Conopco, Inc. Particulate detergent compositions comprising fluorescer
US9365811B2 (en) 2010-10-14 2016-06-14 Conopco Inc. Manufacture of coated particulate detergents
KR20180034509A (ko) * 2015-07-29 2018-04-04 제로스 리미티드 세척 방법, 장치 및 용도
IT201900003951A1 (it) * 2019-03-19 2020-09-19 Desmet Ballestra S P A Impianto per la realizzazione di un prodotto, in particolare costituito da un prodotto tensioattivo
CN111893008A (zh) * 2020-08-10 2020-11-06 纳爱斯集团有限公司 一种洗涤制剂及其制备方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0328880A1 (fr) * 1988-01-19 1989-08-23 Colgate-Palmolive Company Produit d'extrusion d'une composition détergente organique synthétique renforcée en forme particulaire et en forme de "petit pâté", et procédés de préparation et d'utilisation de ce dernier
WO1991002047A1 (fr) * 1989-08-09 1991-02-21 Henkel Kommanditgesellschaft Auf Aktien Fabrication de granules comprimes pour produits de lavage
EP0508543A1 (fr) * 1991-04-12 1992-10-14 The Procter & Gamble Company Structuration chimique de pâtes tensio-actives pour former des granulés tensio-actifs avec haute activité
EP0663439A1 (fr) * 1994-01-17 1995-07-19 The Procter & Gamble Company Procédé pour la préparation de granules de détergent
JPH0827495A (ja) * 1994-07-18 1996-01-30 Lion Corp 界面活性剤組成物の製造方法
DE19509752A1 (de) * 1995-03-17 1996-09-19 Henkel Kgaa Verfahren zur Herstellung eines pulverförmigen Waschmittels

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0328880A1 (fr) * 1988-01-19 1989-08-23 Colgate-Palmolive Company Produit d'extrusion d'une composition détergente organique synthétique renforcée en forme particulaire et en forme de "petit pâté", et procédés de préparation et d'utilisation de ce dernier
WO1991002047A1 (fr) * 1989-08-09 1991-02-21 Henkel Kommanditgesellschaft Auf Aktien Fabrication de granules comprimes pour produits de lavage
EP0508543A1 (fr) * 1991-04-12 1992-10-14 The Procter & Gamble Company Structuration chimique de pâtes tensio-actives pour former des granulés tensio-actifs avec haute activité
EP0663439A1 (fr) * 1994-01-17 1995-07-19 The Procter & Gamble Company Procédé pour la préparation de granules de détergent
JPH0827495A (ja) * 1994-07-18 1996-01-30 Lion Corp 界面活性剤組成物の製造方法
DE19509752A1 (de) * 1995-03-17 1996-09-19 Henkel Kgaa Verfahren zur Herstellung eines pulverförmigen Waschmittels

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
DATABASE WPI Section Ch Week 9614, Derwent World Patents Index; Class D25, AN 96-136605, XP002099513 *

Cited By (49)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6747000B2 (en) 2000-05-05 2004-06-08 The Procter & Gamble Company Process for making solid cleaning components
WO2001085893A1 (fr) * 2000-05-05 2001-11-15 The Procter & Gamble Company Procede de production de constituants nettoyants solides
WO2002102959A1 (fr) * 2001-06-19 2002-12-27 Henkel Kommanditgesellschaft Auf Aktien Produit de lavage et/ou produit de nettoyage pauvre en zeolithe et stable au stockage
WO2004027009A1 (fr) * 2002-09-12 2004-04-01 Henkel Kommanditgesellschaft Auf Aktien Produits de lavage ou de nettoyage comprimes sous l'effet d'une pression
US8058222B2 (en) 2008-07-28 2011-11-15 The Procter & Gamble Company Process for manufacturing extruded alkyl sulfate particles
WO2010014395A1 (fr) * 2008-07-28 2010-02-04 The Procter & Gamble Company Procédé pour la préparation d’une composition détergente
EP2154235A1 (fr) 2008-07-28 2010-02-17 The Procter and Gamble Company Procédé pour préparer une composition détergente
EP2243822A1 (fr) 2009-04-24 2010-10-27 Unilever PLC Poudre détergente dotée de particules riches en détergent
WO2010122050A2 (fr) 2009-04-24 2010-10-28 Unilever Plc Fabrication de particules détergentes extrêmement actives
WO2010122050A3 (fr) * 2009-04-24 2010-12-16 Unilever Plc Fabrication de particules détergentes extrêmement actives
WO2010122051A1 (fr) 2009-04-24 2010-10-28 Unilever Plc Particules de détergent hautement actives
CN102414305A (zh) * 2009-04-24 2012-04-11 荷兰联合利华有限公司 高活性洗涤剂颗粒的制备
AU2010240944B2 (en) * 2009-04-24 2013-01-10 Unilever Plc Manufacture of high active detergent particles
US9228157B2 (en) 2009-04-24 2016-01-05 Conopco, Inc. Manufacture of high active detergent particles
CN102414305B (zh) * 2009-04-24 2014-07-23 荷兰联合利华有限公司 高活性洗涤剂颗粒的制备
US9284517B2 (en) 2010-10-14 2016-03-15 Conopco Inc. Laundry detergent particle
WO2012048947A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2012048949A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particule de détergent à lessive
WO2012048950A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2012048948A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
WO2012049178A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent pour lessive
WO2012049033A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Procédé à cuve à laver le linge à chargement par le haut
WO2012048951A1 (fr) 2010-10-14 2012-04-19 Unilever Plc Particules de détergent à lessive
EP2441822A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Particules de détergent pour le lavage du linge
US9273271B2 (en) 2010-10-14 2016-03-01 Conopco Inc. Laundry detergent particles
US9365811B2 (en) 2010-10-14 2016-06-14 Conopco Inc. Manufacture of coated particulate detergents
US9290723B2 (en) 2010-10-14 2016-03-22 Conopco Inc. Laundry detergent particles
US9290725B2 (en) 2010-10-14 2016-03-22 Conopco Inc. Laundry detergent particles
EP2441825A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Procédé pour la préparation de particules de détergent pour le lavage du linge
US8883702B2 (en) 2010-10-14 2014-11-11 Conopco, Inc. Packaged particulate detergent composition
US9290724B2 (en) 2010-10-14 2016-03-22 Conopco, Inc. Laundry detergent particles
US9062281B2 (en) 2010-10-14 2015-06-23 Conopco, Inc. Particulate detergent compositions comprising fluorescer
EP2441820A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Particules de détergent pour le lavage du linge
EP2441821A1 (fr) 2010-10-14 2012-04-18 Unilever Plc, A Company Registered In England And Wales under company no. 41424 of Unilever House Particules de détergent pour le lavage du linge
WO2013149755A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
CN104220581B (zh) * 2012-04-03 2017-03-01 荷兰联合利华有限公司 洗衣洗涤剂颗粒
US9222061B2 (en) 2012-04-03 2015-12-29 Conopco, Inc. Laundry detergent particle
CN104220581A (zh) * 2012-04-03 2014-12-17 荷兰联合利华有限公司 洗衣洗涤剂颗粒
WO2013149752A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
WO2013149754A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
WO2013149753A1 (fr) 2012-04-03 2013-10-10 Unilever Plc Particules de détergent à lessive
US9279098B2 (en) 2012-04-03 2016-03-08 Conopco, Inc. Laundry detergent particles
CN104220582B (zh) * 2012-04-03 2017-12-22 荷兰联合利华有限公司 洗衣洗涤剂颗粒
KR20180034509A (ko) * 2015-07-29 2018-04-04 제로스 리미티드 세척 방법, 장치 및 용도
US11414633B2 (en) * 2015-07-29 2022-08-16 Xeros Limited Cleaning method, apparatus and use
KR102536292B1 (ko) * 2015-07-29 2023-05-24 제로스 리미티드 세척 방법, 장치 및 용도
IT201900003951A1 (it) * 2019-03-19 2020-09-19 Desmet Ballestra S P A Impianto per la realizzazione di un prodotto, in particolare costituito da un prodotto tensioattivo
WO2020188461A1 (fr) * 2019-03-19 2020-09-24 Desmet Ballestra S.P.A. Installation de fabrication d'un produit, en particulier composé d'un produit tensioactif, de préférence de type anionique
CN111893008A (zh) * 2020-08-10 2020-11-06 纳爱斯集团有限公司 一种洗涤制剂及其制备方法

Also Published As

Publication number Publication date
GB9726824D0 (en) 1998-02-18

Similar Documents

Publication Publication Date Title
WO1999032599A1 (fr) Procede de production de particules
US5318733A (en) Production of compacted granules for detergents
US5290496A (en) Process for the production of granules of a detergent
DE69221357T2 (de) Chemische Strukturierung von oberflächenaktiven Pasten zwecks Herstellung hochwirksamer Tensidgranulate
AU678363B2 (en) Process for making compact detergent compositions
JPH05509119A (ja) 顆粒状の漂白活性化剤
WO1991015567A2 (fr) Procede pour la fabrication d'agents de lavage et de nettoyage
US5663136A (en) Process for making compact detergent compositions
EP0510746A2 (fr) Procédé pour la préparation de granules de détergent condensés
JP2001500557A (ja) 粒状洗浄または清浄剤の製法
CZ9594A3 (en) Process for preparing detergent composition containing alkyl sulfate particles and base granules
AU733708B2 (en) Chemically stable, insecticidally active phosphoroamidothioate pellet compositions and methods for their manufacture
EP0804529B1 (fr) Compose silicate alcalin amorphe
CN100513543C (zh) 阴离子型表面活性剂粉末
CA1322705C (fr) Procede de fabrication de granules d'agent tensioactif concentre
CZ213493A3 (en) Agglomeration process of highly active pastes onto surface-active granules intended for use in detergent mixtures
EP1036158B1 (fr) Procede de production de melanges de matieres premieres de masse volumique apparente elevee
JP4358613B2 (ja) 洗剤粒子群の製造方法
WO2001044427A1 (fr) Procede de preparation de savon et de tensioactifs
JP3510386B2 (ja) 漂白活性化剤造粒物の製造方法、該漂白活性化剤造粒物を含有する漂白剤又は洗剤の製造方法
JPH08199197A (ja) 洗剤ペレットの製造方法及びそれを用いる高嵩密度洗剤の製造方法
WO1997034991A1 (fr) Procede de production de detergents ou de nettoyants granulaires coulants
JPH09217089A (ja) 漂白活性化剤造粒物の製造方法
EP0876469A1 (fr) Procede de preparation de detergents et de nettoyants granulaires ou constituants utilises pour les preparer
JPH0913091A (ja) 漂白活性化剤造粒物の製造方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): BR MX US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
122 Ep: pct application non-entry in european phase
点击 这是indexloc提供的php浏览器服务，不要输入任何密码和下载