TECHNICAL FIELD
[0001] The present invention relates to granular detergent compositions of high bulk density
having good washing performance and good powder properties, and a process for preparing
them.
BACKGROUND AND PRIOR ART
[0002] Recently there has been considerable interest within the detergents industry in the
production of detergent powders having relatively high bulk density, for example,
600 g/litre and above. Particular attention has been paid to the densification of
spray-dried powders by post-treatment. EP 219 328A (Unilever) discloses a granular
low-phosphate detergent composition prepared by spray-drying a slurry to give a base
powder containing a low to moderate level of sodium tripolyphosphate builder and low
levels of inorganic salts, and then postdosing solid material including sodium sulphate
of high bulk density and of smaller particle size than the base powder, thus filling
the voids between base powder particles and producing a product of high bulk density.
[0003] JP 61 069897A (Kao) discloses a process in which a spray-dried detergent powder containing
a high level of anionic surfactant and a low level of builder (zeolite) 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" having an average particle size up to 10αrn and optionally a binder. It
would appear that in the high-speed mixer/granulator, the spray-dried powder is initially
broken down to a fine state of division; the surface-improving agent and optional
binder are then added and the pulverised material granulated to form a final product
of high bulk density. The surface-improving agent, which is a finely divided particulate
solid such as fine sodium aluminosilicate, is apparently required in order to prevent
the composition from forming into large balls or cakes.
[0004] EP 229 671A (Kao) discloses postdosing a crystalline alkaline inorganic salt, for
example, sodium carbonate, to a spray-dried base powder prepared as in the above-mentioned
JP 61 069897A (Kao) and containing a restricted level of water-soluble crystalline
inorganic salts, to produce a high bulk density product.
[0005] GB 1 517 713 (Unilever) discloses a process in which spray-dried or granulated detergent
powders containing sodium tripolyphosphate and sodium sulphate are densified and spheronised
in a "marumerizer" (Trade Mark).
GB 1 453 697 (Unilever) discloses the use of the same apparatus to granulate together
detergent powder components in the presence of a liquid binder to form a granular
detergent composition. The "marumerizer" comprises a substantially horizontal roughened
rotatable table positioned within and at the base of a substantially vertical smooth-walled
cylinder. The disadvantage associated with this apparatus is that it produces powders
or granules having a rather wide particle size distribution, and in particular containing
a relatively high proportion of oversize particles. Such products exhibit poor dissolution
and dispersion characteristics, particularly in low-temperature short duration machine
washes as used in Japanese and other far-eastern washing machines. This can be apparent
to the consumer as deposits on washed fabrics, and in machine washing leads to a high
level of wastage.
[0006] EP 220 024A (Procter & Gamble) discloses a process in which a spray-dried detergent
powder containing a high level (30-85 wt%) of anionic surfactant is mixed with an
inorganic builder (sodium tripolyphosphate, or sodium aluminosilicate and sodium carbonate)
and compacted under high pressure using a roll compactor ("chilsonator"); the compacted
material, after removal of oversize material and fines, is then granulated using conventional
apparatus, for example, a fluidised bed, tumble mixer, or rotating drum or pan.
[0007] EP 158 419A (Hashimura) discloses the preparation of a detergent powder by mixing
a major proportion of soda ash (preferably 70 to 85 wt% of the mixture) and a minor
proportion of surfactant (wholly or predominantly nonionic) in a high-speed mixer/granulator.
DE-A-3617756 describes a process in which constituents of a composition are mixed
in a kneader, then comminuted in a mill and coated with finely divided zeolite before
being granulated in a Marumerizer.
[0008] It has now been found that spray-dried powders containing moderate or high levels
of water-soluble crystalline inorganic salts, including sodium tripolyphosphate and/or
sodium carbonate, can be granulated and densified in a high-speed mixer/granulator,
if necessary after pulverisation, without the need for an "agent for improving surface
properties" or similar pulverulent material, even when high levels of anionic surfactant
are present.
DEFINITION OF THE INVENTION
[0009] The present invention 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 step of treating a particulate starting material comprising:
(a) from 12 to 70 wt% of non-soap detergent-active material, and
(b) at least 15 wt% of water-soluble crystalline inorganic salts, including sodium
tripolyphosphate and/or sodium carbonate,
the weight ratio of (b) to (a) being at least 0.4:1, and optionally other detergent
components to 100 wt%, in a high speed mixer/granulator having both a stirring action
and a cutting action, in the absence of a finely divided particulate agent for improving
surface properties having particle size not greater than 10µrn, whereby granulation
and densification to a bulk density of at least 650 g/litre are effected.
DETAILED DESCRIPTION OF THE INVENTION
[0010] The invention is concerned with a process for the preparation of a detergent powder
combining high bulk density, good powder properties and excellent washing and cleaning
performance.
[0011] The present inventors have found that a detergent base powder prepared by any suitable
method and containing substantial levels of water-soluble crystalline inorganic salts
may be processed in a high-speed mixer/granulator, without the need for the use of
an "agent for improving surface properties" during the granulation step as prescribed
by JP 61 069897A (Kao), to give a dense granulate having good flow properties, even
if relatively high levels of anionic surfactant are present. The product is characterised
by an especially narrow particle size distribution, and in particular by a very small
proportion or oversize material, giving good and rapid cold water dispersability and
low insolubles.
The starting powder
[0012] A preferred starting powder has a ratio of total water-soluble crystalline inorganic
salts (b) to total non-soap surfactant (a) within the range of from 0.4:1 to 9:1,
more preferably from 0.4:1 to 5:1. An especially preferred range for the ratio of
(b) to (a) is from 1:1 to 5:1.
[0013] Preferably the starting powder contains a total of from 15 to 70 wt% of water-soluble
crystalline inorganic salts. As well as sodium tripolyphosphate and sodium carbonate,
examples of such salts include sodium sulphate, sodium ortho- and pyrophosphates,
and crystalline sodium silicates, that is to say, sodium silicates having a ratio
(Si0
2 to Na
20) 1, such as sodium orthosilicate and sodium metasilicate. The alkaline and neutral
silicates of higher ratio commonly used in detergent compositions are not to be regarded
as crystalline.
[0014] According to a preferred embodiment of the invention, the starting powder contains
from 15 to 50 wt%, more preferably from 20 to 40 wt%, of sodium tripolyphosphate.
[0015] The non-soap surfactant present in the starting powder preferably consists at least
partially of anionic surfactant. Suitable 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 C
8-C
15; primary and secondary alkyl sulphates, particularly sodium C
12-Cl5 primary alcohol sulphates; alkyl ether sulphates; alpha-olefin and internal olefin
sulphonates; alkane sulphonates; dialkyl sulphosuccinates; fatty acid ester sulphonates;
and combinations thereof.
[0016] If desired, 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 C
12-C15 primary and secondary alcohols ethoxylated with an average of from 3 to 20 moles
of ethylene oxide per mole of alcohol.
[0017] Suitably the surfactant component of the starting powder may be constituted by from
0 to 70%, preferably from 8 to 60 wt%, of anionic surfactant, and from 0 to 20%, preferably
from 0 to 10%, by weight of nonionic surfactant.
[0018] Other types of non-soap surfactant, for example, cationic, zwitterionic, amphoteric
or semipolar surfactants, may also be present if desired. Many 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.
[0019] If desired, soap may also be present, to provide foam control and additional detergency
and builder power; soap is not included in the 12 to 70% figure for the surfactant
content quoted previously.
[0020] The starting powder may be prepared by any suitable tower or non-tower method, for
example, spray-drying or dry mixing. The invention is especially useful for the densification
of a spray-dried powder.
[0021] If desired, at least part of the water-soluble crystalline inorganic salt to be included
in the final product may be admixed to the remainder of the starting powder in the
high-speed mixer/granulator itself. In this embodiment of the invention, the percentages
and ratios specified above should be based on the total material introduced into the
high-speed mixer/granulator, including the added salt.
[0022] Thus it is within the scope of the present invention to introduce into the high-speed
mixer/granulator a starting powder, prepared for example by spray-drying, containing
less than the amount of water-soluble crystalline inorganic salt specified above,
and then to admix with that powder, in the high-speed mixer/granulator, sufficient
water-soluble crystalline inorganic salt to bring the salt percentage (b) and the
ratio (b) to (a) up to the specified level.
[0023] Similarly, it is within the scope of the invention to add surfactant, or indeed any
other component, in the high-speed mixer/granulator provided that the final composition
is as specified above, and provided that the component so added is not a finely divided
"agent for improving surface properties" as described in JP 61 069897A (Kao) discussed
previously. Thus, in the process of the invention, any component other than a finely
divided particulate solid having a particle size up to 10αrn may be added to the high-speed
mixer/granulator prior to granulation.
[0024] One procedure according to the invention includes the step of admixing at least one
inorganic or organic salt having a particle size of at least 100 /1.m with the remainder
of the starting powder in the high-speed mixer/granulator. If the salt is water-soluble,
inorganic and crystalline, it should be included within the percentages and ratios
specified above which relate to the total amount of such salts in the material subjected
to granulation in the high-speed mixer/granulator.
[0025] Salts that may conveniently be incorporated by this method include borax, sodium
bicarbonate, sodium silicate, sodium tripolyphosphate, sodium carbonate, sodium perborate,
sodium percarbonate, sodium citrate, sodium nitrilotriacetate, sodium succinate, sodium
sulphate and combinations of these. These salts can give various benefits: for example,
borax and sodium bicarbonate are buffers giving mild products of low in-wash pH.
The process
[0026] In the process of the invention, granulation is effected by means of a high-speed
mixer/granulator having both a stirring action and a cutting action. Preferably the
stirrer and the 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.
[0027] 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. Especially
preferred are mixers of the Fukae (Trade Mark) FS-G series manufactured by Fukae Powtech
Kogyo Co., Japan; this apparatus is 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.
[0028] Other similar mixers found to be suitable for use in the process of the invention
are the Diosna (Trade Mark) V series ex Dierks & Söhne, Germany; and the Pharma Matrix
(Trade Mark) ex T K Fielder Ltd., England. Other similar mixers believed to be suitable
for use in the process of the invention include the Fuji (Trade Mark) VG-C series
ex Fuji Sangyo Co., Japan; and the Roto (Trade Mark) ex Zanchetta & Co srl, Italy.
[0029] Another mixer found to be suitable for use in the process of the invention is the
Lodige (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.
[0030] As indicated above, the use of a high-speed mixer/granulator is essential in the
process of the invention to effect granulation and densification. If desired, the
mixer may also be used for a pretreatment step before granulation is carried out.
[0031] For example, it is within the scope of the invention, as previously indicated, for
one or more further ingredients to 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.
[0032] 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.
[0033] The 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.
[0034] 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.
[0035] The presence of a liquid binder is necessary for successful granulation. The amount
of binder added preferably does not exceed that needed to bring the free moisture
content of the composition above about 6 wt%, since higher levels may lead to a deterioration
in the flow properties of the final granulate. If necessary, binder, preferably water,
may be added before or during granulation, but some starting powders will inherently
contain sufficient moisture. If a liquid binder is to be added, 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.
[0036] If the starting powder has a sufficient free moisture content to render the addition
of a binder unnecessary, pulverisation (if required) and 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.
[0037] According to a preferred embodiment of the invention, granulation is 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.
[0038] It is an essential feature of the present invention that during granulation no "agent
for improving surface properties" as defined in the above-mentioned JP 61 069897A
(Kao) be present. When processing a formulation having a relatively high ratio of
aluminosilicate builder to surfactant, in accordance with the present invention, the
use of a finely divided particulate material such as fine sodium aluminosilicate during
the granulation step is not only unnecessary but can with some formulations make granulation
more difficult, or even impossible.
The optional flow aid
[0039] In accordance with a preferred embodiment of the invention, a finely divided particulate
flow aid may be admixed with the granular material after granulation is complete.
Advantageously, flow aid 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 flow
aid to the granulate after removing the latter to different apparatus.
[0040] This embodiment of the invention should be distinguished from the prior art process
of JP 61 069897A (Kao), mentioned above, in which an "agent for improving surface
properties", which can be fine sodium aluminosilicate, is present during the granulation
stage itself. It is within the scope of the present invention to add a particulate
flow aid after granulation is complete, but, as explained above, it is essential to
the invention that no finely divided particulate "agent for improving surface properties"
be present during granulation. The addition of a flow aid after granulation is complete
can have an additional beneficial effect on the properties of the granulate, regardless
of the formulation, whereas the presence of this type of material during the granulation
step in the process of the invention makes processing more difficult.
[0041] The preferred granulation temperature of from 30 to 45
° C, preferably about 35
° C, may also be maintained during the subsequent admixture of a flow aid.
[0042] The flow aid is a finely divided particulate material. The preferred average particle
size is 0.1 to 20 /1.m, more preferably 1 to 10 /1.m.
[0043] According to one preferred embodiment of the invention, the flow aid is finely divided
amorphous sodium aluminosilicate, as described and claimed in our copending application
of even date, now EP-A-339996. A suitable material is available commercially from
Crosfield Chemicals Ltd, Warrington, Cheshire, England, under the trade mark Alusil.
This material is effective in improving flow properties even at very low levels, 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 sodium aluminosilicate
added after granulation.
[0044] 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%.
[0045] Another preferred flow aid is finely divided crystalline sodium aluminosilicate.
The crystalline aluminosilicates discussed previously in the context of builders are
also suitable for use as flow aids. They are, however, less weight-effective than
the amorphous material and are suitably used in an amount of from 3.0 to 12.0 wt%,
more preferably from 4.0 to 10.0 wt%.
[0046] If desired, both crystalline and amorphous sodium aluminosilicates may be used, together
or sequentially, as flow aids.
[0047] Other flow aids suitable for use in the process of the invention include precipitated
silica, for example, Neosyl (Trade Mark), and precipitated calcium silicate, for example,
Microcal (Trade Mark), both commercially available from Crosfield Chemicals Ltd, Warrington,
Cheshire, England.
The final granulate
[0048] 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,
preferably not exceeding 0.25 and more preferably not exceeding 0.20, which distinguishes
it from even the densest powders prepared by spray-drying alone.
[0049] 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 and the steps that precede it may be admixed to the granulate to make a final
product.
[0050] In one preferred embodiment of the invention, for example, a detergent base powder
is prepared by spray-drying an aqueous slurry of heat-insensitive and compatible ingredients;
if desired, other ingredients may then be admixed as discussed above; and the resulting
powder is densified and granulated in accordance with the process of the 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.
[0051] In another embodiment of the invention, the densified granulate prepared in accordance
with the present invention is 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.
[0052] The invention is further illustrated by the following non-limiting Examples, in which
parts and percentages are by weight unless otherwise stated.
EXAMPLES
[0053] In the Examples which follow, the following abbreviations are used.
LAS: sodium linear alkylbenzene sulphonate
NI: nonionic surfactant (ethoxylated alcohol)
NSD: total non-soap detergent
STP: sodium tripolyphosphate
Carbonate: sodium carbonate
Sulphate: sodium sulphate
Silicate: sodium alkaline silicate
g: good
Alu: Alusil (Trade Mark) N, finely divided amorphous sodium aluminosilicate
Zeo: Zeolite 4A (Wessalith (Trade Mark) ex Degussa)
Examples 1 & 2
[0054] Powders containing sodium tripolyphosphate and sodium sulphate were prepared by spray-drying
aqueous slurries to the formulations (weight %) shown in Table 1.
[0055] 20 kg batches of each powder were densified in a Fukae (Trade Mark) high-speed mixer/granulator,
process conditions and resulting powder properties being shown in Table 2. In Example
1, the powder was initially subjected to a 2-3 minute warming up period, at a low
stirrer speed (50 rev/min) and without the cutter running, until the temperature had
reached about 30-35 °C. This was followed by pulverisation (optional), then binder
addition (also optional), then granulation, followed finally by addition of flow aid.
[0056] Comparison of Examples 2(a) and 2(b) shows the greater weight-effectiveness of Alusil
as flow aid.
Examples 3 to 5
[0057] Powders containing sodium tripolyphosphate as the sole water-soluble crystalline
inorganic salt were prepared by spray-drying aqueous slurries to the formulations
(weight %) shown in Table 3.
[0058] 20 kg batches of each powder were densified in a Fukae (Trade Mark) high-speed mixer/granulator
as described in Examples 1 and 2, process conditions and resulting powder properties
being shown in Tables 4 and 5.
Examples 6 to 8
[0059] Powders containing sodium tripolyphosphate, sodium carbonate and sodium sulphate
were prepared to the formulations (weight %) shown in Table 6.
[0060] The powders were prepared by spray-drying aqueous slurries. However, the sodium carbonate
in the powder of Example 6 was not incorporated via the slurry but postdosed in the
Fukae mixer.
[0061] 20 kg batches of each powder were densified in a Fukae (Trade Mark) high-speed mixer/granulator
as described in Examples 1 and 2, process conditions and resulting powder properties
being shown in Table 7.
Examples 9 and 10
[0062] Powders containing sodium tripolyphosphate and sodium carbonate were prepared, by
spray-drying aqueous slurries, to the formulations (weight %) shown in Table 9, and
densified in the Fukae mixer as in previous Examples, as shown in Table 10.
Example 11
[0063] A powder containing sodium tripolyphosphate, sodium sulphate and borax was prepared
to the formulation (weight %) shown in Table 11.
[0064] The powder was prepared by spray-drying an aqueous slurry of all the ingredients
except the borax. 9.0 kg of spray-dried base powder and 1.0 kg of borax were mixed
and granulated/densified in the Fukae mixer, process conditions and resulting powder
properties being shown in Table 12.
[0065] During granulation the temperature rose from an initial 20 ° C to about 40-45 ° C.
It was not necessary to cool the mixer.
[0066] The properties of the densified granulate were as follows:
[0067] The product was a mild detergent powder giving a pH (1 wt% aqueous solution) of 9.2.
1. A process for the preparation of a granular detergent composition or component
having a bulk density of at least 650 g/litre, characterised by the step of treating
a particulate starting material comprising:
(a) from 12 to 70 wt% of non-soap detergent-active material, and
(h) at least 15 wt% of water-soluble crystalline inorganic salts, including sodium
tripolyphosphate and/or sodium carbonate,
the weight ratio of (b) to (a) being at least 0.4:1, and optionally other detergent
components to 100 wt%,
in a high-speed mixer/granulator having independently controllable stirrer and cutter
elements, in the absence of a finely divided particulate agent for improving surface
properties having an average particle size not greater that 10µrn, whereby granulation
and densification to a bulk density of at least 650 g/litre are effected.
2. A process as claimed in claim 1, characterised in that granulation is carried out
in a bowl-type high-speed mixer/granulator having a substantially vertical stirrer
axis.
3. A process as claimed in claim 1 or claim 2, characterised in that the particulate
starting material consists at least partially of a spray-dried powder.
4. A process as claimed in any preceding claim, characterised in that the particulate
starting material has a ratio of (b) to (a) within the range of from 0.4:1 to 5:1.
5. A process as claimed in claim 4, characterised in that the particulate starting
material has a ratio of (b) to (a) within the range of from 1:1 to 5:1.
6. A process as claimed in any preceding claim, characterised in that the particulate
starting material comprises from 15 to 70 wt% of water-soluble crystalline inorganic
salts including sodium tripolyphosphate and/or sodium carbonate.
7. A process as claimed in claim 6, characterised in that the particulate starting
material comprises from 15 to 50 wt% of sodium tripolyphosphate.
8. A process as claimed in any preceding claim, characterised in that the non-soap
detergent-active material of the particulate starting material consists at least partially
of anionic detergent-active material.
9. A process as claimed in any preceding claim, characterised in that the particulate
starting material is prepared by a process including the step of admixing at least
one inorganic or organic salt having a particle size of at least 100 /1.m with the
remainder of the particulate starting material in the high-speed mixer/granulator.
10. A process as claimed in claim 9, characterised in that the salt is selected from
borax, sodium bicarbonate, sodium silicate, sodium tripolyphosphate, sodium carbonate,
sodium perborate, sodium percarbonate, sodium citrate, sodium nitrilotriacetate, sodium
succinate, sodium sulphate and combinations thereof.
11. A process as claimed in any preceding claim, which further comprises the step
of admixing a finely divided particulate flow aid to the granular material after granulation
is complete.
12. A process as claimed in claim 11, characterised in that the flow aid is amorphous
sodium aluminosilicate and is added in an amount of from 0.2 to 5.0 wt%, based on
the total composition.
13. A process as claimed in claim 11, characterised in that the flow aid is finely
divided crystalline sodium aluminosilicate and is added in an amount of from 3.0 to
12.0 wt% based on the total composition.
14. A process according to any preceding claim wherein the detergent composition or
component prepared by the process has a particle porosity of less than 0.25.
15. A process according to claim 14 wherein the detergent composition or component
has a particle porosity of less than 0.20.
1. Verfahren zur Herstellung einer körnchenförmigen Waschmittelzusammensetzung oder
-komponente mit einer Schüttdichte von mindestens 650 g/I, gekennzeichnet durch den
Schritt der Behandlung eines teilchenförmigen Ausgangsmaterials umfassend:
(a) 12 bis 70 Gew.-% eines nichtseifenartigen waschaktiven Materials und
(b) mindestens 15 Gew.-% wasserlöslicher kristalliner anorganischer Salze, einschließlich
Natriumtripolyphosphat und/oder Natriumcarbonat,
wobei das Gewichtsverhältnis von (b) zu (a) mindestens 0,4:1 beträgt, und gegebenenfalls
andere Waschmittelbestandteile bis zu 100 Gew.-%,
in einem Hochgeschwindigkeitsmischer/Granulator mit unabhängig voneinander regelbaren
Rühr-und Schneidelementen in Abwesenheit eines feinverteilten teilchenförmigen Mittels
zur Verbesserung der Oberflächeneigenschaften mit einer durchschnittlichen Teilchengröße
nicht größer als 10 um, wodurch Granulierung und Verdichtung zu einer Schüttdichte
von mindestens 650 g/I bewirkt wird.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Granulierung in einem
schalenförmigen Hochgeschwindigkeitsmischer/Granulator mit einer im wesentlichen vertikalen
Rührerachse ausgeführt wird.
3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß das teilchenförmige
Ausgangsmaterial zumindest teilweise aus einem sprühgetrockneten Pulver besteht.
4. Verfahren nach einem vorangehenden Anspruch, dadurch gekennzeichnet, daß das teilchenförmige
Ausgangsmaterial ein Verhältnis von (b):(a) innerhalb des Bereiches von 0,4:1 bis
5:1 aufweist.
5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial
ein Verhältnis von (b):(a) innerhalb des Bereiches von 1:1 bis 5:1 aufweist.
6. Verfahren nach einem vorangehenden Anspruch, dadurch gekennzeichnet, daß das teilchenförmige
Ausgangsmaterial 15 bis 70 Gew.-% wasserlöslicher kristalliner anorganischer Salze,
einschließlich Natriumtripolyphosphat und/oder Natriumcarbonat, umfaßt.
7. Verfahren nach Anspruch 6, dadurch gekennzeichnet, daß das teilchenförmige Ausgangsmaterial
15 bis 50 Gew.-% Natriumtripolyphosphat umfaßt.
8. Verfahren nach einem vorangehenden Anspruch, dadurch gekennzeichnet, daß das nichtseifenartige
waschaktive Material des teilchenförmigen Ausgangsmaterials zumindest teilweise aus
anionischem waschaktivem Material besteht.
9. Verfahren nach einem vorangehenden Anspruch, dadurch gekennzeichnet, daß das teilchenförmige
Ausgangsmaterial durch ein Verfahren, einschließlich des Schrittes der Anmischung
mindestens eines anorganischen oder organischen Salzes mit einer Teilchengröße von
mindestens 100 um mit dem Rest des teilchenförmigen Ausgangsmaterials in dem Hochgeschwindigkeitsmischer/Granulator
hergestellt wird.
10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, daß das Salz ausgewählt ist
aus Borax, Natriumbicarbonat, Natriumsilicat, Natriumtripolyphosphat, Natriumcarbonat,
Natriumperborat, Natriumpercarbonat, Natriumcitrat, Natriumnitrilotriacetat, Natriumsuccinat,
Natriumsulfat und Kombinationen davon.
11. Verfahren nach einem vorangehenden Anspruch, zusätzlich umfassend den Schritt
des Anmischens einer feinverteilten teilchenförmigen Fließhilfe zu dem körnchenförmigen
Material, nachdem die Granulierung vollständig ist.
12. Verfahren nach Anspruch 11, dadurch gekennzeichnet, daß die Fließhilfe ein amorphes
Natriumaluminosilicat darstellt und in einer Menge von 0,2 bis 5,0 Gew.-%, bezogen
auf die Gesamtzusammensetzung, zugegeben wird.
13. Verfahren nach Anspruch 11, dadurch gekennzeichnet, daß die Fließhilfe ein feinverteiltes
kristallines Natriumaluminosilicat darstellt und in einer Menge von 3,0 bis 12,0 Gew.-%,
bezogen auf die Gesamtzusammensetzung, zugegeben wird.
14. Verfahren nach einem vorangehenden Anspruch, wobei die durch das Verfahren hergestellte
Waschmittelzusammensetzung oder -komponente eine Teilchenporosität von weniger als
0,25 aufweist.
15. Verfahren nach Anspruch 14, wobei die Waschmittelzusammensetzung oder -komponente
eine Teilchenporosität von weniger als 0,20 aufweist.
1. Procédé de préparation d'une composition ou composant détergent granulaire ayant
une densité apparente d'au moins 650 g/I, caractérisé en ce qu'il consiste à traiter
une matière particulaire de départ comprenant
(a) de 12 à 70% en poids d'un détergent actif non savonneux, et
(b) au moins 15% en poids de sels minéraux cristallins hydrosolubles, notamment le
tripolyphosphate de sodium et/ou le carbonate de sodium,
le rapport pondéral (b):(a) étant d'au moins 0,4:1 et, facultativement, d'autres composants
détergents q.s.p 100% en poids,
dans un mélangeur/granulateur à grande vitesse comportant des éléments d'agitateur
et de cisaille indépendamment réglables, en l'absence d'un agent particulaire finement
divisé pour améliorer les propriétés superficielles, présentant une granulométrie
moyenne qui ne dépasse pas 10 um, de sorte qu'on effectue la granulation et la densification
jusqu'à une densité apparente d'au moins 650 g/I.
2. Procédé selon la revendication 1, caractérisé en ce qu'on effectue la granulation
dans un mélangeur/granulateur à grande vitesse du type à cuvette présentant un axe
d'agitateur sensiblement vertical.
3. Procédé selon la revendication 1 ou 2, caractérisé en ce que la matière particulaire
de départ consiste en poudre au moins partiellement séchée par pulvérisation.
4. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce
que, dans la matière particulaire de départ, le rapport (b):(a) est compris entre
0,4:1 et 5:1.
5. Procédé selon la revendication 4, caractérisé en ce que le rapport (b):(a) dans
la matière particulaire de départ est compris entre 1:1 et 5:1.
6. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce
que la matière de départ comprend de 15 à 70% en poids de sels minéraux cristallins
hydrosolubles, notamment du tripolyphosphate de sodium et/ou du carbonate de sodium.
7. Procédé selon la revendication 6, caractérisé en ce que la matière particulaire
de départ comprend de 15 à 50% en poids de tripolypnosphate de sodium.
8. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce
que le détergent actif non savonneux dans la matière particulaire de départ consiste
au moins partiellement en détergent actif anionique.
9. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce
qu'on prépare la matière particulaire de départ par un procédé consistant à mélanger
au moins un sel minéral ou organique d'une granulométrie d'au moins 100 um avec le
complément de la matière particulaire de départ dans le mélangeur/granulateur à grande
vitesse.
10. Procédé selon la revendication 9, caractérisé en ce que le sel est choisi parmi
le borax, le bicarbonate de sodium, le silicate de sodium, le tripolyphosphate de
sodium, le carbonate de sodium, le perborate de sodium, le percarbonate de sodium,
le citrate de sodium, le nitrilotriacétate de sodium, le succinate de sodium, le sulfate
de sodium et des combinaisons de ceux-ci.
11. Procédé selon l'une quelconque des revendications prcédentes, qui consiste à incorporer
dans la matière granulaire après achèvement de la granulation, un agent particulaire
finement divisé d'assistance à l'écoulement.
12. Procédé selon la revendication 11, caractérisé en ce que l'agent d'assistance
à l'écoulement est l'aluminosilicate amorphe de sodium et on l'ajoute à raison de
0,2 à 5,0% en poids par rapport à la composition totale.
13. Procédé selon la revendication 11, caractérisé en ce que l'agent d'assistance
à l'écoulement est un aluminosilicate de sodium cristallin finement divisé et on l'ajoute
à raison de 3,0 à 12,0% par rapport au poids de la composition totale.
14. Procédé selon l'une quelconque des revendications précédentes, dans lequel la
composition ou composent détergent préparé par le procédé présente une porosité de
particules inférieure à 0,25.
15. Procédé selon la revendication 14, dans lequel la porosité des particules de la
composition ou composent détergent est inférieure à 0,20.