EP0351937A1 - Detergent compositions and process for preparing them - Google Patents
Detergent compositions and process for preparing them Download PDFInfo
- Publication number
- EP0351937A1 EP0351937A1 EP19890304210 EP89304210A EP0351937A1 EP 0351937 A1 EP0351937 A1 EP 0351937A1 EP 19890304210 EP19890304210 EP 19890304210 EP 89304210 A EP89304210 A EP 89304210A EP 0351937 A1 EP0351937 A1 EP 0351937A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- sodium
- starting material
- rpm
- detergent
- granulation
- Prior art date
- Legal status (The legal status 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 status listed.)
- Granted
Links
- 239000000203 mixture Substances 0.000 title claims abstract description 27
- 239000003599 detergent Substances 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 28
- 150000003839 salts Chemical class 0.000 claims abstract description 25
- 235000019832 sodium triphosphate Nutrition 0.000 claims abstract description 25
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 14
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 12
- 239000000344 soap Substances 0.000 claims abstract description 12
- 239000007858 starting material Substances 0.000 claims abstract description 12
- 239000011149 active material Substances 0.000 claims abstract description 7
- 125000000129 anionic group Chemical group 0.000 claims abstract 2
- 239000000843 powder Substances 0.000 claims description 61
- 238000000034 method Methods 0.000 claims description 46
- 238000005469 granulation Methods 0.000 claims description 42
- 230000003179 granulation Effects 0.000 claims description 42
- 239000002245 particle Substances 0.000 claims description 26
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 18
- 239000008187 granular material Substances 0.000 claims description 17
- 229910000503 Na-aluminosilicate Inorganic materials 0.000 claims description 12
- 235000012217 sodium aluminium silicate Nutrition 0.000 claims description 12
- 239000000429 sodium aluminium silicate Substances 0.000 claims description 11
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 11
- 235000017550 sodium carbonate Nutrition 0.000 claims description 11
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 9
- 235000011152 sodium sulphate Nutrition 0.000 claims description 9
- 229910021538 borax Inorganic materials 0.000 claims description 7
- 239000004328 sodium tetraborate Substances 0.000 claims description 7
- 235000010339 sodium tetraborate Nutrition 0.000 claims description 7
- 238000000280 densification Methods 0.000 claims description 6
- 239000004115 Sodium Silicate Substances 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052911 sodium silicate Inorganic materials 0.000 claims description 3
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims description 2
- VTIIJXUACCWYHX-UHFFFAOYSA-L disodium;carboxylatooxy carbonate Chemical compound [Na+].[Na+].[O-]C(=O)OOC([O-])=O VTIIJXUACCWYHX-UHFFFAOYSA-L 0.000 claims description 2
- 229940001593 sodium carbonate Drugs 0.000 claims description 2
- 239000001509 sodium citrate Substances 0.000 claims description 2
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 claims description 2
- 229960001790 sodium citrate Drugs 0.000 claims description 2
- DZCAZXAJPZCSCU-UHFFFAOYSA-K sodium nitrilotriacetate Chemical compound [Na+].[Na+].[Na+].[O-]C(=O)CN(CC([O-])=O)CC([O-])=O DZCAZXAJPZCSCU-UHFFFAOYSA-K 0.000 claims description 2
- 229960001922 sodium perborate Drugs 0.000 claims description 2
- 229940045872 sodium percarbonate Drugs 0.000 claims description 2
- 235000019794 sodium silicate Nutrition 0.000 claims description 2
- 229940074404 sodium succinate Drugs 0.000 claims description 2
- ZDQYSKICYIVCPN-UHFFFAOYSA-L sodium succinate (anhydrous) Chemical compound [Na+].[Na+].[O-]C(=O)CCC([O-])=O ZDQYSKICYIVCPN-UHFFFAOYSA-L 0.000 claims description 2
- YKLJGMBLPUQQOI-UHFFFAOYSA-M sodium;oxidooxy(oxo)borane Chemical compound [Na+].[O-]OB=O YKLJGMBLPUQQOI-UHFFFAOYSA-M 0.000 claims description 2
- 238000003756 stirring Methods 0.000 abstract description 7
- 238000005520 cutting process Methods 0.000 abstract description 6
- 239000011236 particulate material Substances 0.000 abstract description 3
- 239000011230 binding agent Substances 0.000 description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 238000010298 pulverizing process Methods 0.000 description 13
- 239000000463 material Substances 0.000 description 12
- 238000001694 spray drying Methods 0.000 description 12
- 239000004094 surface-active agent Substances 0.000 description 10
- 238000009472 formulation Methods 0.000 description 9
- 239000002002 slurry Substances 0.000 description 8
- 239000003945 anionic surfactant Substances 0.000 description 7
- 239000004615 ingredient Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 239000012467 final product Substances 0.000 description 6
- -1 for example Inorganic materials 0.000 description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 5
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- 229910017053 inorganic salt Inorganic materials 0.000 description 5
- 239000011734 sodium Substances 0.000 description 5
- 229910052708 sodium Inorganic materials 0.000 description 5
- 239000002736 nonionic surfactant Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- 229910000632 Alusil Inorganic materials 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 229910021653 sulphate ion Inorganic materials 0.000 description 3
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 235000010724 Wisteria floribunda Nutrition 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- 229910000323 aluminium silicate Inorganic materials 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000007580 dry-mixing Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 150000003138 primary alcohols Chemical class 0.000 description 2
- 150000003333 secondary alcohols Chemical class 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 235000019351 sodium silicates Nutrition 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000011282 treatment Methods 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- 229910021532 Calcite Inorganic materials 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N Na2O Inorganic materials [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- ULUAUXLGCMPNKK-UHFFFAOYSA-N Sulfobutanedioic acid Chemical class OC(=O)CC(C(O)=O)S(O)(=O)=O ULUAUXLGCMPNKK-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 239000000872 buffer Substances 0.000 description 1
- 239000000378 calcium silicate Substances 0.000 description 1
- 229910052918 calcium silicate Inorganic materials 0.000 description 1
- OYACROKNLOSFPA-UHFFFAOYSA-N calcium;dioxido(oxo)silane Chemical compound [Ca+2].[O-][Si]([O-])=O OYACROKNLOSFPA-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 235000011180 diphosphates Nutrition 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 229920000058 polyacrylate Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 150000004760 silicates Chemical class 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000019795 sodium metasilicate Nutrition 0.000 description 1
- FTZNYGSHSMZEIA-UHFFFAOYSA-M sodium;hydrogen carbonate;sulfuric acid Chemical compound [Na+].OC([O-])=O.OS(O)(=O)=O FTZNYGSHSMZEIA-UHFFFAOYSA-M 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- POWFTOSLLWLEBN-UHFFFAOYSA-N tetrasodium;silicate Chemical compound [Na+].[Na+].[Na+].[Na+].[O-][Si]([O-])([O-])[O-] POWFTOSLLWLEBN-UHFFFAOYSA-N 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000004711 α-olefin Substances 0.000 description 1
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
-
- 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
-
- 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
- C11D3/04—Water-soluble compounds
- C11D3/10—Carbonates ; Bicarbonates
Definitions
- 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.
- EP 219 328A 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.
- JP 61 069897A 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" 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.
- EP 229 671A 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.
- a crystalline alkaline inorganic salt for example, sodium carbonate
- GB 1 517 713 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 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.
- 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.
- an inorganic builder sodium tripolyphosphate, or sodium aluminosilicate and sodium carbonate
- EP 158 419A 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.
- 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:
- 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.
- 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.
- 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.
- the starting powder contains a total of from 15 to 70 wt% of water-soluble crystalline inorganic salts.
- examples of such salts include sodium sulphate, sodium ortho- and pyrophosphates, and crystalline sodium silicates, that is to say, sodium silicates having a ratio (SiO2 to Na2O) ⁇ 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.
- the starting powder contains from 15 to 50 wt%, more preferably 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 wt%, 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 12 to 70% figure for the surfactant content quoted previously.
- 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.
- 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.
- the percentages and ratios specified above should be based on the total material introduced into the high-speed mixer/granulator, including the added salt.
- 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.
- any component other than a finely divided particulate solid having a particle size of less than 100 microns may be added to the high-speed mixer/granulator prior to granulation.
- 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 microns 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.
- 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.
- borax and sodium bicarbonate are buffers giving mild products of low in-wash pH.
- granulation is effected by means of a high-speed mixer/granulator having both a stirring action and a cutting action.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- a 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.
- 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.
- a finely divided particulate flow aid may be admixed with the granular material after granulation is complete.
- 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.
- 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.
- 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.
- the flow aid is a finely divided particulate material.
- the preferred average particle size is 0.1 to 20 microns, more preferably 1 to 10 microns.
- the flow aid is finely divided amorphous sodium aluminosilicate, as described and claimed in our copending application of even date (Case C.3236).
- 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.
- 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%.
- 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%.
- both crystalline and amorphous sodium aluminosilicates may be used, together or sequentially, as flow aids.
- 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 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.
- 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.
- 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.
- 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.
- 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)
- Example 2 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.
- the powder was initially subjected to a 2-3 minute warming up period, at a low stirrer speed (50 rpm) 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.
- 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.
- Table 3 Example 3 4 5 LAS 48.6 25.3 26.4 NI - 2.4 2.6 NSD (a) 48.6 27.7 29.0 STP 26.7 42.5 45.9 Salts (b) 26.7 42.5 45.9 Silicate 15.5 11.0 10.0 Minors 1.5 2.9 2.9 Water 7.7 15.9 12.2 (b):(a) 0.55 1.5 1.6
- Powders containing sodium tripolyphosphate, sodium carbonate and sodium sulphate were prepared to the formulations (weight %) shown in Table 6.
- Table 6 Example 6 7 8 LAS 28.0 15.0 15.5 NI - 3.0 1.5 NSD (a) 28.0 18.0 17.0 STP 27.0 30.0 26.0 Carbonate 5.0 10.0 18.9 Sulphate 15.0 15.0 17.2 Salts (b) 47.0 55.0 62.1 Soap - 6.0 - Silicate 8.0 9.0 9.0 Calcite 5.0 - - Minors 1.0 1.0 1.4 Water 11.0 11.0 9.8 (b):(a) 1.7 3.0 3.7
- 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.
- 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.
- a powder containing sodium tripolyphosphate, sodium sulphate and borax was prepared to the formulation (weight %) shown in Table 11.
- Table 11 LAS 28.0 NSD (a) 28.0 STP 27.0 Sulphate 19.7 Borax 10.0 Salts (b) 56.7 Polyacrylate polymer 4.5 Minors 0.8 Water 10.0 (b):(a) 2.03
- 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.
- the properties of the densified granulate were as follows: Yield ⁇ 1700 ⁇ m (wt %) 82.1 Average particle size ( ⁇ m) 583 Bulk density (g/litre) 887 Dynamic flow rate (ml/s) 140 Compressibility (%v/v) 4.7 Particle porosity ⁇ 0.20
- the product was a mild detergent powder giving a pH (1 wt% aqueous solution) of 9.2.
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Abstract
Description
- 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.
- 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.
- 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" 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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 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.
- 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.
- 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.
- 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 (SiO₂ to Na₂O) ≦ 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.
- 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.
- 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 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.
- 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 C₁₂-C₁₅ primary and secondary alcohols ethoxylated with an average of from 3 to 20 moles of ethylene oxide per mole of alcohol.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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 of less than 100 microns may be added to the high-speed mixer/granulator prior to granulation.
- 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 microns 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- 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.
- The flow aid is a finely divided particulate material. The preferred average particle size is 0.1 to 20 microns, more preferably 1 to 10 microns.
- 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 (Case C.3236). 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.
- 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%.
- 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%.
- If desired, both crystalline and amorphous sodium aluminosilicates may be used, together or sequentially, as flow aids.
- 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 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.
- 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.
- 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.
- 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.
- The invention is further illustrated by the following non-limiting Examples, in which parts and percentages are by weight unless otherwise stated.
- 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) - Powders containing sodium tripolyphosphate and sodium sulphate were prepared by spray-drying aqueous slurries to the formulations (weight %) shown in Table 1.
Table 1 Example 1 2 LAS 12.2 9.7 NI 8.1 2.8 NSD (a) 20.3 12.5 STP 42.7 42.5 Sulphate 10.2 14.8 Salts (b) 52.9 57.3 Soap - 4.9 Silicate 10.2 10.0 Minors 2.4 2.8 Water 14.2 12.5 (b):(a) 2.6 4.6 - 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 rpm) 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.
Table 2 1 2(a) 2(b) Pulverisation: Time (min) 4 0.5 0.5 Stirrer speed (rpm) 180 180 180 Cutter speed (rpm) 3000 1000 1000 Binder (water): Amount (wt %) 4 0.5 0.5 Addition time (min) 1 0.5 0.5 Stirrer speed (rpm) 100 100 100 Cutter speed (rpm) 3000 3000 3000 Granulation: Time (min) 15 7 6 Stirrer speed (rpm) 140 140 140 Cutter speed (rpm) 2700 3000 3000 Flow aid: Zeo or Alu Alu Alu Zeo Amount (wt %) 2 1.5 5 Addition time (min) 1 1 1 Stirrer speed (rpm) 90 90 90 Cutter speed (rpm) 300 300 300 Yield <1700 µm (wt %) 95 93 97 Average particle size (µm) 689 555 480 Bulk density (g/litre) 854 840 780 Dynamic flow rate (ml/s) 109 92 61 Compressibility (%v/v) 7.6 7 12 Particle porosity <0.20 <0.20 <0.20 Comparison of Examples 2(a) and 2(b) shows the greater weight-effectiveness of Alusil as flow aid. - 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.
Table 3 Example 3 4 5 LAS 48.6 25.3 26.4 NI - 2.4 2.6 NSD (a) 48.6 27.7 29.0 STP 26.7 42.5 45.9 Salts (b) 26.7 42.5 45.9 Silicate 15.5 11.0 10.0 Minors 1.5 2.9 2.9 Water 7.7 15.9 12.2 (b):(a) 0.55 1.5 1.6 - 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.
Table 4 3 5(a) 5(b) Pulverisation: Time (min) 3 0.5 0.5 Stirrer speed (rpm) 300 180 180 Cutter speed (rpm) 3000 3000 3000 Binder (water): Amount (wt %) 2 none none Addition time (min) 1 - - Stirrer speed (rpm) 100 - - Cutter speed (rpm) 3000 - - Granulation: Time (min) 5 5 6 Stirrer speed (rpm) 275 140 140 Cutter speed (rpm) 3000 2700 2700 Flow aid: Zeo. or Alu. Alu Alu Zeo Amount (wt %) 1 1.5 5 Addition time (min) 1 1 1 Stirrer speed (rpm) 90 90 90 Cutter speed (rpm) 0 300 300 Yield <1700 µm (wt %) 80 94 93 Average particle size (µm) 693 528 389 Bulk density (g/litre) 673 720 820 Dynamic flow rate (ml/s) 134 83 96 Compressibility (%v/v) 3.5 14 11 Particle porosity <0.20 <0.20 <0.20 Table 5 4(a) 4(b) Pulverisation: Time (min) 0.5 0.5 Stirrer speed (rpm) 180 180 Cutter speed (rpm) 3000 3000 Binder (water): Amount (wt %) 1 0.5 Addition time (min) 0.5 0.5 Stirrer speed (rpm) 100 100 Cutter speed (rpm) 3000 3000 Granulation: Time (min) 4 4 Stirrer speed (rpm) 140 140 Cutter speed (rpm) 2700 2700 Flow aid: Zeo. or Alu. Alu Alu Amount (wt %) 2.5 2.5 Addition time (min) 1 1 Stirrer speed (rpm) 90 90 Cutter speed (rpm) 300 300 Yield <1700 µm (wt %) 95 96 Average particle size (µm) 501 608 Bulk density (g/litre) 830 770 Dynamic flow rate (ml/s) 86 89 Compressibility (%v/v) 9 11 Particle porosity <0.20 <0.20 - Powders containing sodium tripolyphosphate, sodium carbonate and sodium sulphate were prepared to the formulations (weight %) shown in Table 6.
Table 6 Example 6 7 8 LAS 28.0 15.0 15.5 NI - 3.0 1.5 NSD (a) 28.0 18.0 17.0 STP 27.0 30.0 26.0 Carbonate 5.0 10.0 18.9 Sulphate 15.0 15.0 17.2 Salts (b) 47.0 55.0 62.1 Soap - 6.0 - Silicate 8.0 9.0 9.0 Calcite 5.0 - - Minors 1.0 1.0 1.4 Water 11.0 11.0 9.8 (b):(a) 1.7 3.0 3.7 - 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.
- 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.
Table 7 6 7 Pulverisation: Time (min) 1 1 Stirrer speed (rpm) 300 300 Cutter speed (rpm) 3000 3000 Binder (water): Amount (wt %) 0.5 1 Addition time (min) 2 1 Stirrer speed (rpm) 100 100 Cutter speed (rpm) 3000 3000 Granulation: Time (min) 4 4 Stirrer speed (rpm) 225 200 Cutter speed (rpm) 3000 3000 Flow aid: Zeo. or Alu. Alu Alu Amount (wt %) 1 1 Addition time (min) 1 1 Stirrer speed (rpm) 90 90 Cutter speed (rpm) 0 0 Yield <1700 µm (wt %) g g Average particle size (µm) 743 582 Bulk density (g/litre) 906 800 Dynamic flow rate (ml/s) 133 120 Compressibility (%v/v) 3.5 7.0 Particle porosity <0.20 <0.20 Table 8 8(a) 8(b) 8(c) Pulverisation: none none none Time (min) - - - Stirrer speed (rpm) - - - Cutter speed (rpm) - - - Binder (water): Amount (wt %) 1.5 1.5 1 Addition time (min) 0.5 0.5 0.5 Stirrer speed (rpm) 100 100 100 Cutter speed (rpm) 3000 3000 3000 Granulation: Time (min) 10 7 7 Stirrer speed (rpm) 140 140 140 Cutter speed (rpm) 2700 2700 2700 Flow aid: Zeo or Alu Alu Alu Alu Amount (wt %) 1.5 1.5 1 Addition time (min) 0.5 0.5 1 Stirrer speed (rpm) 90 90 90 Cutter speed (rpm) 300 300 300 Yield <1700 µm (wt %) 94.5 96 96 Bulk density (g/litre) 920 870 760 Dynamic flow rate (ml/s) g g g Compressibility (%v/v) g g g Particle porosity <0.20 <0.20 <0.20 - 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.
Table 9 Example 9 10 LAS 38.0 22.7 NI - 2.1 NSD (a) 38.0 24.8 STP 21.0 37.1 Carbonate 22.0 17.5 Salts (b) 43.0 54.6 Silicate 12.0 9.3 Minors 1.0 1.0 Water 6.0 10.3 (b):(a) 1.1 2.2 Table 10 9 10 Pulverisation: Time (min) 3 3 Stirrer speed (rpm) 300 300 Cutter speed (rpm) 3000 3000 Binder (water): Amount (wt %) 2 1 Addition time (min) 1 1 Stirrer speed (rpm) 100 100 Cutter speed (rpm) 3000 3000 Granulation: Time (min) 5 5 Stirrer speed (rpm) 275 275 Cutter speed (rpm) 3000 3000 Flow aid: Zeo or Alu Alu Alu Amount (wt %) 1 1 Addition time (min) 1 1 Stirrer speed (rpm) 90 90 Cutter speed (rpm) 0 0 Yield <1700 µm (wt %) 80 90 Average particle size (µm) 810 566 Bulk density (g/litre) 746 801 Dynamic flow rate (ml/s) 137 122 Compressibility (%v/v) 3.0 10 Particle porosity <0.20 <0.20 - A powder containing sodium tripolyphosphate, sodium sulphate and borax was prepared to the formulation (weight %) shown in Table 11.
Table 11 LAS 28.0 NSD (a) 28.0 STP 27.0 Sulphate 19.7 Borax 10.0 Salts (b) 56.7 Polyacrylate polymer 4.5 Minors 0.8 Water 10.0 (b):(a) 2.03 - 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.
Table 12 11 Mixing: Time (min) 5 Stirrer speed (rpm) 200 Cutter speed (rpm) 0 Binder (water): Amount (wt %) 1 Addition time (min) 1 Stirrer speed (rpm) 300 Cutter speed (rpm) 3000 Granulation: Time (min) 9 Stirrer speed (rpm) 300 Cutter speed (rpm) 3000 Breakdown of oversize: Time (min) 1.5 Stirrer speed (rpm) 75 Cutter speed (rpm) 3000 Flow aid: Zeo or Alu Alu Amount (wt %) 1 Addition time (min) 0.5 Stirrer speed (rpm) 75 Cutter speed (rpm) 0 Discharge: Time (min) 0.5 Stirrer speed (rpm) 75 Cutter speed (rpm) 0 - During granulation the temperature rose from an initial 20°C to about 40-45°C. It was not necessary to cool the mixer.
- The properties of the densified granulate were as follows:
Yield <1700 µm (wt %) 82.1 Average particle size (µm) 583 Bulk density (g/litre) 887 Dynamic flow rate (ml/s) 140 Compressibility (%v/v) 4.7 Particle porosity <0.20 - The product was a mild detergent powder giving a pH (1 wt% aqueous solution) of 9.2.
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, whereby granulation and densification to a bulk density of at least 650 g/litre are effected.
Claims (16)
(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 independently controllable stirrer and cutter elements, in the absence of a finely divided particulate agent for improving surface properties, whereby granulation and densification to a bulk density of at least 650 g/litre are effected.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB888817386A GB8817386D0 (en) | 1988-07-21 | 1988-07-21 | Detergent compositions & process for preparing them |
GB8817386 | 1988-07-21 |
Publications (3)
Publication Number | Publication Date |
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EP0351937A1 true EP0351937A1 (en) | 1990-01-24 |
EP0351937B1 EP0351937B1 (en) | 1994-02-09 |
EP0351937B2 EP0351937B2 (en) | 2001-12-12 |
Family
ID=10640869
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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EP89304210A Expired - Lifetime EP0351937B2 (en) | 1988-07-21 | 1989-04-27 | Detergent compositions and process for preparing them |
Country Status (15)
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EP (1) | EP0351937B2 (en) |
JP (1) | JP2644038B2 (en) |
KR (2) | KR920004462B1 (en) |
AU (1) | AU611556B2 (en) |
BR (1) | BR8902006A (en) |
CA (1) | CA1322704C (en) |
DE (1) | DE68912983T3 (en) |
ES (1) | ES2049320T5 (en) |
GB (2) | GB8817386D0 (en) |
HK (1) | HK86594A (en) |
IN (2) | IN170472B (en) |
MY (1) | MY105051A (en) |
PH (1) | PH26823A (en) |
TR (1) | TR25923A (en) |
ZA (2) | ZA893186B (en) |
Cited By (13)
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EP0643129A1 (en) * | 1993-09-07 | 1995-03-15 | The Procter & Gamble Company | Process for preparing detergent compositions |
WO1997032005A1 (en) * | 1996-02-26 | 1997-09-04 | Unilever Plc | Anionic detergent particles |
WO1997032003A1 (en) * | 1996-02-29 | 1997-09-04 | The Procter & Gamble Company | Process for manufacture of high density detergent granules |
US5665692A (en) * | 1995-02-13 | 1997-09-09 | The Procter & Gamble Company | Process for producing detergent agglomerates in which particle size is controlled |
WO1998016618A3 (en) * | 1996-10-15 | 1998-08-20 | Procter & Gamble | Process for making a high density detergent composition via post drying mixing/densification |
WO1998054286A1 (en) * | 1997-05-30 | 1998-12-03 | Unilever Plc | Particulate detergent compositions |
WO1999011749A1 (en) * | 1997-08-28 | 1999-03-11 | The Procter & Gamble Company | Agglomeration process for producing a particulate modifier polyamine detergent admix |
US6069124A (en) * | 1997-05-30 | 2000-05-30 | Lever Brothers Company Division Of Conopco, Inc. | Granular detergent compositions and their production |
US6207635B1 (en) | 1995-05-31 | 2001-03-27 | The Procter & Gamble Company | Process for manufacture of high density detergent granules |
US6221831B1 (en) | 1997-05-30 | 2001-04-24 | Lever Brothers Company, Division Of Conopco, Inc. | Free flowing detergent composition containing high levels of surfactant |
US6303558B1 (en) | 1997-05-30 | 2001-10-16 | Lever Brothers Co., Division Of Conopco | Detergent composition containing at least two granular components |
CN1116400C (en) * | 1996-02-29 | 2003-07-30 | 普罗格特-甘布尔公司 | Process for mfg. high density detergent granules |
WO2006021294A1 (en) * | 2004-08-25 | 2006-03-02 | Unilever Plc | A particulate detergent composition, and packaging therefor |
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GB8926718D0 (en) * | 1989-11-27 | 1990-01-17 | Unilever Plc | Process for the preparation of detergent compositions |
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 |
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US5489392A (en) * | 1994-09-20 | 1996-02-06 | The Procter & Gamble Company | Process for making a high density detergent composition in a single mixer/densifier with selected recycle streams for improved agglomerate properties |
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US5569645A (en) * | 1995-04-24 | 1996-10-29 | The Procter & Gamble Company | Low dosage detergent composition containing optimum proportions of agglomerates and spray dried granules for improved flow properties |
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US5665691A (en) * | 1995-10-04 | 1997-09-09 | The Procter & Gamble Company | Process for making a low density detergent composition by agglomeration with a hydrated salt |
US5576285A (en) * | 1995-10-04 | 1996-11-19 | The Procter & Gamble Company | Process for making a low density detergent composition by agglomeration with an inorganic double salt |
KR100394762B1 (en) * | 1996-02-13 | 2003-11-20 | 주식회사 엘지생활건강 | Concentrated powdery detergent composition with excellent long period storage stability |
US5668099A (en) * | 1996-02-14 | 1997-09-16 | The Procter & Gamble Company | Process for making a low density detergent composition by agglomeration with an inorganic double salt |
JP2000501453A (en) * | 1996-08-26 | 2000-02-08 | ザ、プロクター、エンド、ギャンブル、カンパニー | Agglomeration method for producing detergent compositions including premixing of modified polyamine polymer |
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US6610645B2 (en) | 1998-03-06 | 2003-08-26 | Eugene Joseph Pancheri | Selected crystalline calcium carbonate builder for use in detergent compositions |
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GB1517713A (en) * | 1974-10-31 | 1978-07-12 | Unilever Ltd | Preparation of detergent formulations |
JPH0631430B2 (en) * | 1985-05-29 | 1994-04-27 | ライオン株式会社 | Method for producing high bulk density granular detergent composition |
JPH0631431B2 (en) * | 1985-06-27 | 1994-04-27 | ライオン株式会社 | Method for producing cleaning composition |
US4925585A (en) * | 1988-06-29 | 1990-05-15 | The Procter & Gamble Company | Detergent granules from cold dough using fine dispersion granulation |
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1988
- 1988-07-21 GB GB888817386A patent/GB8817386D0/en active Pending
-
1989
- 1989-04-24 CA CA000597591A patent/CA1322704C/en not_active Expired - Fee Related
- 1989-04-27 DE DE68912983T patent/DE68912983T3/en not_active Expired - Lifetime
- 1989-04-27 AU AU33751/89A patent/AU611556B2/en not_active Ceased
- 1989-04-27 EP EP89304210A patent/EP0351937B2/en not_active Expired - Lifetime
- 1989-04-27 ES ES89304210T patent/ES2049320T5/en not_active Expired - Lifetime
- 1989-04-28 KR KR1019890005623A patent/KR920004462B1/en not_active IP Right Cessation
- 1989-04-28 IN IN113/BOM/89A patent/IN170472B/en unknown
- 1989-04-28 PH PH38585A patent/PH26823A/en unknown
- 1989-04-28 BR BR898902006A patent/BR8902006A/en not_active IP Right Cessation
- 1989-04-28 MY MYPI89000581A patent/MY105051A/en unknown
- 1989-04-28 JP JP1111946A patent/JP2644038B2/en not_active Expired - Fee Related
- 1989-04-28 TR TR89/0322A patent/TR25923A/en unknown
- 1989-04-28 ZA ZA893186A patent/ZA893186B/en unknown
- 1989-04-28 IN IN114/BOM/89A patent/IN169824B/en unknown
- 1989-05-03 GB GB898910087A patent/GB8910087D0/en active Pending
- 1989-07-21 ZA ZA895578A patent/ZA895578B/en unknown
- 1989-07-21 KR KR1019890010340A patent/KR920000114B1/en not_active IP Right Cessation
-
1994
- 1994-08-25 HK HK86594A patent/HK86594A/en not_active IP Right Cessation
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Cited By (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0643129A1 (en) * | 1993-09-07 | 1995-03-15 | The Procter & Gamble Company | Process for preparing detergent compositions |
US5665692A (en) * | 1995-02-13 | 1997-09-09 | The Procter & Gamble Company | Process for producing detergent agglomerates in which particle size is controlled |
US6207635B1 (en) | 1995-05-31 | 2001-03-27 | The Procter & Gamble Company | Process for manufacture of high density detergent granules |
WO1997032005A1 (en) * | 1996-02-26 | 1997-09-04 | Unilever Plc | Anionic detergent particles |
WO1997032003A1 (en) * | 1996-02-29 | 1997-09-04 | The Procter & Gamble Company | Process for manufacture of high density detergent granules |
CN1116400C (en) * | 1996-02-29 | 2003-07-30 | 普罗格特-甘布尔公司 | Process for mfg. high density detergent granules |
WO1998016618A3 (en) * | 1996-10-15 | 1998-08-20 | Procter & Gamble | Process for making a high density detergent composition via post drying mixing/densification |
WO1998054286A1 (en) * | 1997-05-30 | 1998-12-03 | Unilever Plc | Particulate detergent compositions |
US6069124A (en) * | 1997-05-30 | 2000-05-30 | Lever Brothers Company Division Of Conopco, Inc. | Granular detergent compositions and their production |
US6191095B1 (en) | 1997-05-30 | 2001-02-20 | Lever Brothers Company, A Division Of Conopco, Inc. | Detergent compositions |
US6221831B1 (en) | 1997-05-30 | 2001-04-24 | Lever Brothers Company, Division Of Conopco, Inc. | Free flowing detergent composition containing high levels of surfactant |
US6303558B1 (en) | 1997-05-30 | 2001-10-16 | Lever Brothers Co., Division Of Conopco | Detergent composition containing at least two granular components |
WO1999011749A1 (en) * | 1997-08-28 | 1999-03-11 | The Procter & Gamble Company | Agglomeration process for producing a particulate modifier polyamine detergent admix |
WO2006021294A1 (en) * | 2004-08-25 | 2006-03-02 | Unilever Plc | A particulate detergent composition, and packaging therefor |
Also Published As
Publication number | Publication date |
---|---|
JP2644038B2 (en) | 1997-08-25 |
EP0351937B2 (en) | 2001-12-12 |
KR920000114B1 (en) | 1992-01-09 |
DE68912983T2 (en) | 1994-06-01 |
EP0351937B1 (en) | 1994-02-09 |
KR900001836A (en) | 1990-02-27 |
AU3375189A (en) | 1990-01-25 |
TR25923A (en) | 1993-09-17 |
ES2049320T5 (en) | 2002-05-16 |
MY105051A (en) | 1994-07-30 |
DE68912983T3 (en) | 2002-04-04 |
DE68912983D1 (en) | 1994-03-24 |
ZA893186B (en) | 1990-12-28 |
BR8902006A (en) | 1990-04-10 |
IN169824B (en) | 1991-12-28 |
JPH0241399A (en) | 1990-02-09 |
KR900001829A (en) | 1990-02-27 |
ES2049320T3 (en) | 1994-04-16 |
GB8817386D0 (en) | 1988-08-24 |
HK86594A (en) | 1994-09-02 |
CA1322704C (en) | 1993-10-05 |
GB8910087D0 (en) | 1989-06-21 |
AU611556B2 (en) | 1991-06-13 |
KR920004462B1 (en) | 1992-06-05 |
IN170472B (en) | 1992-03-28 |
PH26823A (en) | 1992-11-05 |
ZA895578B (en) | 1991-03-27 |
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