WO2011062234A1 - 洗剤粒子群の製造方法 - Google Patents
洗剤粒子群の製造方法 Download PDFInfo
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- WO2011062234A1 WO2011062234A1 PCT/JP2010/070593 JP2010070593W WO2011062234A1 WO 2011062234 A1 WO2011062234 A1 WO 2011062234A1 JP 2010070593 W JP2010070593 W JP 2010070593W WO 2011062234 A1 WO2011062234 A1 WO 2011062234A1
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- Prior art keywords
- detergent
- weight
- mixer
- stirring
- particle size
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Classifications
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
- C11D1/00—Detergent compositions based essentially on surface-active compounds; Use of these compounds as a detergent
- C11D1/02—Anionic compounds
- C11D1/12—Sulfonic acids or sulfuric acid esters; Salts thereof
- C11D1/22—Sulfonic acids or sulfuric acid esters; Salts thereof derived from aromatic compounds
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- 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 ; Methods for using cleaning compositions
- C11D11/0082—Special methods for preparing compositions containing mixtures of detergents ; Methods for using cleaning compositions one or more of the detergent ingredients being in a liquefied state, e.g. slurry, paste or melt, and the process resulting in solid detergent particles such as granules, powders or beads
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
- C11D17/00—Detergent materials or soaps characterised by their shape or physical properties
- C11D17/06—Powder; Flakes; Free-flowing mixtures; Sheets
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
- 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
-
- 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
Definitions
- the present invention relates to a method for producing detergent particles using a container rotating mixer.
- Patent Document 1 a method for producing a detergent composition granulated by adding a liquid binder
- Patent Document 2 A method for producing a detergent composition that is granulated by adding a liquid binder after dry neutralization at a temperature of °C or higher (Patent Document 2), followed by dry neutralization with a continuous high-speed mixer, followed by high bulk density with a medium-speed mixer, followed by cooling
- Patent Document 3 the manufacturing method of the detergent composition granulated by drying
- solubility in the conventional method as described above, there are relatively many agglomerated particles of the starting material generated by using the non-soap anionic surfactant as a binder. Therefore, it is not easy to improve the solubility.
- the method by dry neutralization is a method suitable for easily producing a detergent particle group mainly composed of an anionic surfactant, but it is possible to granulate while agglomerating raw materials.
- Basic In such a method, when the anionic surfactant is blended in a high amount, due to its strong binder force, aggregation proceeds, making it difficult to reduce the particle size and reducing the granulation yield. Even if a relatively small particle size range is obtained by crushing, it is difficult to obtain a detergent particle group having a sharp particle size distribution and excellent solubility in high yield.
- Patent Document 4 describes a method for producing a granular material by distributing a liquid component between a mixer / granulator and a fluid bed granulator.
- a continuous free-fall mixer In a drum with a baffle, an example is disclosed in which alkylbenzene sulfonic acid is dry-neutralized with sodium carbonate or the like.
- this method uses a continuous free-fall mixer, the aggregates are not crushed and the shearing force applied to the particles is suppressed, but the type of nozzle and spray droplet diameter when spraying alkylbenzenesulfonic acid are suppressed. There is no suggestion about the problem, and problems remain regarding sharpening of the particle size distribution, yield, and solubility.
- the gist of the present invention is a method for producing a detergent particle group including a step of dry neutralizing an acid precursor of a non-soap anionic surfactant with an alkaline powder raw material.
- the present invention relates to a method for producing a detergent particle group, characterized in that a mixer is used and the acid precursor is supplied with an average droplet diameter of 200 ⁇ m or less.
- the present invention is a method for producing a detergent particle group comprising a step of dry neutralizing an acid precursor with an alkaline powder raw material, wherein the detergent particle group having a sharp particle size distribution and excellent solubility is obtained with high yield. It relates to a manufacturing method that can
- the production method of the detergent particle group of the present invention produces an effect that the detergent particle group having a sharp particle size distribution and excellent solubility can be obtained with high yield.
- the method for producing a detergent particle group of the present invention is a method for producing a detergent particle group comprising a step of dry neutralizing an acid precursor of a non-soap anionic surfactant with an alkaline powder raw material.
- the acid precursor is supplied using a multi-fluid nozzle using a container rotating mixer.
- an acid precursor of a non-soap anionic surfactant exhibits adhesiveness when it is dry-neutralized by contact with an alkaline powder raw material. Such an acid precursor is used in a container-rotating mixer.
- supplying with a one-fluid nozzle or pipe which is a general supply method it is difficult to uniformly disperse the supplied liquid component in the mixer, and coarse particles are likely to be formed due to large liquid mass generated locally. I understood.
- the acid precursor that expresses tackiness when sprayed with a powder using a multi-fluid nozzle such as a two-fluid nozzle is sprayed and supplied into the container rotary mixer, it is surprisingly coarse. It was found that uniform granulation was possible while suppressing the formation of particles. This is presumably because high dispersion can be achieved by making the acid precursor into fine droplets in advance using a multi-fluid nozzle, and a large liquid mass forming coarse particles is not generated. Therefore, it is also one of the features of the present invention that the acid precursor that exhibits adhesiveness when it comes into contact with the powder is added to the container rotating mixer using a multi-fluid nozzle.
- the hypothesis of the mechanism for improving the solubility is that voids are generated in the particles by a non-consolidated granulation method using a dissolving rotary mixer, and droplets are made finer and highly dispersed by a multi-fluid nozzle. Therefore, it is thought to be due to a synergistic effect of suppressing the formation of a continuous layer of surfactant in the particles.
- a container rotating type mixer is used, and the acid precursor is sprayed using a multi-fluid nozzle to be supplied to the alkaline powder raw material in the mixer, and further mixed
- dry neutralization is achieved by stirring (mixing) the components in the machine.
- Acid precursor of non-soap anionic surfactant is a precursor of non-soap anionic surfactant, An acid form, which is liquid at room temperature, forms a salt by a neutralization reaction. Therefore, the acid precursor is not particularly limited as long as it is a precursor of a known non-soap anionic surfactant and has the above-mentioned properties.
- linear alkylbenzene sulfonic acid (LAS), ⁇ -olefin sulfone is not particularly limited.
- Examples include acid (AOS), alkyl sulfuric acid (AS), internal olefin sulfonic acid, fatty acid ester sulfonic acid, alkyl ether sulfuric acid, and dialkyl sulfosuccinic acid.
- AOS acid
- AS alkyl sulfuric acid
- AS internal olefin sulfonic acid
- fatty acid ester sulfonic acid fatty acid ester sulfonic acid
- alkyl ether sulfuric acid alkyl ether sulfuric acid
- dialkyl sulfosuccinic acid dialkyl sulfosuccinic acid.
- Such an acid precursor may use only one component, and may use it in combination of 2 or more components.
- linear alkylbenzene sulfonic acid (LAS) is preferable from the viewpoints of economy, storage stability and foaming.
- a predetermined amount of an inorganic acid such as sulfuric acid may be mixed in advance with the acid precursor.
- the amount of the non-soap anionic surfactant in the obtained detergent particle group is preferably 10 to 45% by weight, preferably 13 to 35% by weight in the detergent particle group from the viewpoints of detergency and granulation properties. Is more preferable.
- the temperature of the acid precursor at the time of supply is not particularly limited.
- 10 to 80 ° C. is preferable, and 20 to 70 ° C. is more preferable.
- alkaline powder raw material examples include those usually used as alkaline agents in detergent compositions, such as sodium carbonate, sodium hydrogen carbonate, sodium silicate, potassium carbonate, calcium carbonate and the like. . These may be used alone or in combination of two or more. Among alkaline powder raw materials, sodium carbonate is mentioned as a preferred embodiment.
- the average particle size of the alkaline powder raw material is preferably 1 to 500 ⁇ m, more preferably 3 to 450 ⁇ m, further preferably 5 to 350 ⁇ m, and still more preferably 5 to 250 ⁇ m, from the viewpoint of granulation.
- either light soda ash (light ash) or heavy soda ash (dense ash) can be used, but it is preferable to use light ash from the viewpoint of reactivity with the acid precursor.
- dense ash it is more preferable to use light ash having a particle size of 1 to 50 ⁇ m. This enables detergent particles with high bulk density while maintaining reactivity with the acid precursor. Groups can be manufactured.
- the alkaline powder raw material can function as a detergent builder and an alkaline agent in the final composition. Therefore, the addition amount of the alkaline powder raw material is preferably an amount obtained by adding the alkaline powder raw material for exhibiting the above function to the amount necessary for neutralization of the acid precursor (neutralization equivalent). That is, the amount of the alkaline powder material added is preferably substantially larger than the neutralization equivalent, for example, preferably 1 to 35 times the neutralization equivalent, more preferably 2 to 30 times, still more preferably. 3 to 25 times. When an inorganic acid is used in combination with an acid precursor, the neutralization equivalent further adds an amount necessary for neutralization of the inorganic acid.
- the average particle diameter of the alkaline powder raw material is not particularly limited, but when a surfactant is highly blended, it may be pulverized to 1 to 50 ⁇ m from the viewpoint of improving the yield.
- the average particle size of the alkaline powder raw material is calculated on a volume basis, and is a value measured using, for example, a laser diffraction particle size distribution analyzer: LA-920 (manufactured by Horiba, Ltd.). is there.
- Container rotation type mixer As the container rotation type mixer, a drum type mixer or a pan type mixer is preferable.
- the drum-type mixer is not particularly limited as long as the drum-shaped cylinder rotates and performs processing.
- the conical drum-type granulator is used. (Mixer), multi-stage conical drum granulator (mixer), etc. can also be used. These apparatuses can be used in both batch and continuous processes.
- baffle plates baffles ( ) May be attached. This makes it possible to cause the particle group to perform an upward movement, and improves the powder mixing property and the solid-liquid mixing property.
- the operating condition of the container rotating mixer is not particularly limited as long as the components in the mixer can be stirred, but the operating condition is that the fluid number defined by the following formula is 0.005 to 1.0. An operating condition of 0.01 to 0.6 is more preferable.
- Fluid number: Fr V 2 / (R ⁇ g)
- V Circumferential speed [m / s]
- R Radius from the center of rotation to the circumference of the rotating object [m]
- g Gravity acceleration [m / s 2 ]
- Such materials include tripolyphosphates, crystalline or amorphous alkali metal aluminosilicates (zeolites), crystalline silicates, fluorescent agents, pigments, recontamination inhibitors (polycarboxylate polymers, sodium carboxymethylcellulose, etc.) , Particulate surfactant (fatty acid or salt thereof, linear alkylbenzene sulfonate, alkyl sulfate, etc.), spray dried powder, silica, diatomaceous earth, calcite, kaolin, bentonite, sodium sulfate, sodium sulfite, etc. .
- Such a substance is arbitrarily used depending on its application.
- the average particle size of tripolyphosphate and sodium sulfate is preferably 1 ⁇ m or more. From the viewpoint of suppressing particle aggregation, it is preferably 50 ⁇ m or less.
- the average particle size of tripolyphosphate or sodium sulfate is calculated on a volume basis, and is measured using, for example, a laser diffraction particle size distribution analyzer: LA-920 (manufactured by Horiba, Ltd.). Value.
- alkali metal aluminosilicate (zeolite) when alkali metal aluminosilicate (zeolite) is used, the content of alkali metal aluminosilicate (zeolite) in the detergent particle group improves fluidity, suppresses smudge and caking, and cleans. From the viewpoint of improving the strength, 0.1% by weight or more is preferable, 0.5% by weight or more is more preferable, 1% by weight or more is more preferable, and from the viewpoint of rinsing properties and solubility, 20% by weight or less is preferable, 15% by weight % Or less is more preferable, 10% by weight or less is more preferable, and 5% by weight or less is more preferable.
- the above substances may be added together with the alkaline powder raw material before adding the acid precursor, or may be added after adding the acid precursor, but alkali metal aluminosilicate, silica, When adding diatomaceous earth and calcite, it is possible to improve fluidity and storage stability by using these as surface modifiers. preferable.
- Multi-fluid nozzle it is preferable to supply an acid precursor using a multi-fluid nozzle.
- a multi-fluid nozzle is a nozzle that mixes and atomizes a liquid and atomizing gas (air, nitrogen, etc.) through an independent flow path to the vicinity of the nozzle tip.
- a fluid nozzle or the like can be used.
- the mixing portion of the acid precursor and atomizing gas may be either an internal mixing type that mixes in the nozzle tip portion or an external mixing type that mixes outside the nozzle tip portion.
- an internal mixed type two-fluid nozzle such as manufactured by Spraying Systems Japan Co., Ltd., manufactured by Kyoritsu Alloy Manufacturing Co., Ltd., or manufactured by Ikeuchi Co., Ltd., manufactured by Spraying Systems Japan Co., Ltd.
- an external mixing type two-fluid nozzle manufactured by Kyoritsu Alloy Mfg. Co., Ltd. and Atmax Co., Ltd. an external mixing type four-fluid nozzle manufactured by Fujisaki Electric Co., Ltd., and the like.
- the droplet diameter of the acid precursor droplet can be adjusted by changing the balance between the flow rate of the acid precursor and the flow rate of the atomizing gas. That is, as the flow rate of the atomizing gas is increased with respect to an acid precursor having a certain flow rate, the droplet diameter becomes smaller. Furthermore, the droplet diameter becomes smaller as the flow rate of the acid precursor is decreased with respect to the atomizing gas at a certain flow rate.
- the acid precursor when a two-fluid nozzle is used, for example, it is preferable to supply the acid precursor under the following conditions. Adjustment of the atomizing gas flow rate is easy by adjusting the atomizing gas spray pressure. From the viewpoint of liquid dispersion, the atomizing gas atomizing pressure is preferably 0.1 MPa or more, and the equipment load From the viewpoint of 1.0 MPa, 1.0 MPa or less is preferable.
- the spray pressure of the acid precursor is not particularly limited, but is preferably 1.0 MPa or less, for example, from the viewpoint of equipment load.
- the average particle size of the acid precursor droplet size should be 200 ⁇ m or less. From 1 to 200 ⁇ m, more preferably from 3 to 150 ⁇ m, even more preferably from 10 to 58 ⁇ m.
- the smaller the droplet diameter the more reliably the aggregation during dry neutralization can be suppressed.
- reducing the flow rate of the acid precursor increases the addition time and decreases the production capacity. Therefore, for example, by using a plurality of multi-fluid nozzles and reducing the flow rate per nozzle, it is effective to increase the addition speed while maintaining the fineness of the droplets.
- the addition rate [% / min] which is a value obtained by dividing the liquid powder ratio ((weight of acid precursor / weight of charged powder) ⁇ 100) [%] by addition time [min]
- the addition is preferably in the range of 0.1 to 15% / min, and more preferably in the range of 0.5 to 10% / min.
- the average particle diameter of the droplet diameter of the acid precursor is calculated on a volume basis, and is, for example, a value measured using a laser diffraction particle size distribution analyzer: Spray Tech (manufactured by Malvern). is there.
- a detergent particle group may be produced by further adding other liquid components.
- the other liquid component to be added can be appropriately selected according to the composition of the detergent particle group to be obtained, and a desired liquid component can be used.
- the addition timing of the liquid component is not particularly limited.
- the liquid component may be added before, during or after the dry neutralization of the acid precursor and the alkaline powder raw material. When added, it is preferable to add the surface modifier.
- a liquid component When a liquid component is added after the dry neutralization step, it may be added to the container rotary mixer used for dry neutralization, or the detergent particles obtained by the production method of the present invention may be mixed in the container rotary mixer. After discharging from the machine, it may be added using another mixer / granulator.
- liquid component examples include any liquid component used in ordinary detergent compositions such as nonionic surfactants, water-soluble polymers (polyethylene glycol, sodium polyacrylate, maleic acrylate copolymer, etc.) and fatty acids. .
- the liquid component only one component may be used, or two or more components may be used in combination.
- the component may be added as a liquid, or may be added in the form of an aqueous solution or a dispersion.
- the amount of the net liquid component excluding the medium is preferably 15% by weight or less, more preferably 10% by weight or less, of the final product detergent particle group from the viewpoint of suppressing aggregation of the detergent particle group.
- the nonionic surfactant used as the liquid component is not particularly limited, but from the viewpoint of detergency, for example, a polyoxyalkylene alkyl obtained by adding 6 to 22 moles of alkylene oxide to an alcohol having 10 to 14 carbon atoms. Ether is preferred.
- spraying can be performed with any nozzle, not depending on the multi-fluid nozzle described in the present invention.
- Detergent composition and its manufacturing method A detergent composition can be manufactured by adding a desired component further to the detergent particle group manufactured as mentioned above. That is, the detergent composition of the present invention comprises a detergent particle group obtained by the production method of the present invention.
- the added component examples include enzymes, fragrances, bleaching agents, pigments and the like. Such components may be added to the container rotary mixer after dry neutralization, or the detergent particles obtained by the production method of the present invention are discharged from the container rotary mixer and then mixed separately. You may add using a machine.
- the bulk density of the detergent particles is preferably 400 to 1000 g / L.
- the average particle size of the detergent particle group is preferably 200 to 800 ⁇ m, more preferably 200 to 600 ⁇ m, still more preferably 260 to 600 ⁇ m.
- the fluidity of the detergent particles is preferably 4 to 10 seconds, and more preferably 4 to 7 seconds.
- the detergent yield is preferably closer to 100%, for example, 80 to 100% is preferable, and 90 to 100% is more preferable.
- Average Particle Size For the average particle size, the median diameter is calculated from the weight fraction according to the size of the mesh after vibrating for 5 minutes using a standard sieve of JIS Z 8801 (aperture 2000 to 45 ⁇ m). More specifically, using a 12-stage sieve having a mesh size of 45 ⁇ m, 63 ⁇ m, 90 ⁇ m, 125 ⁇ m, 180 ⁇ m, 250 ⁇ m, 355 ⁇ m, 500 ⁇ m, 710 ⁇ m, 1000 ⁇ m, 1410 ⁇ m, and 2000 ⁇ m, a small sieve with a mesh on the saucer.
- Stack in order add 100 g of particles from the top of the top 2000 ⁇ m sieve, cover and attach to a low-tap sieve shaker (made by HEIKO, tapping 156 times / minute, rolling: 290 times / minute) After vibrating for 5 minutes, the weight of the particles remaining on each sieve and the saucer is measured, and the weight ratio (%) of the particles on each sieve is calculated.
- the average particle size is determined by accumulating the weight ratio of the particles on the sieve having a small mesh size in order from the saucer, and the total particle size becomes 50%.
- the bulk density is measured by a method defined by JIS K 3362. The bulk density is measured with the remaining particles obtained by cutting the particles remaining on the 2000 ⁇ m sieve.
- the flow time is defined as the time required for 100 mL of powder to flow out from the bulk density measurement hopper defined by JIS K 3362.
- the flow time is preferably 10 seconds or less, more preferably 8 seconds or less, and even more preferably 7 seconds or less.
- liquidity is measured with the remaining particle
- the detergent yield in the present invention indicates the ratio of particles of 1410 ⁇ m or less in the manufactured detergent particle group.
- ⁇ Quality evaluation method 1. Sharpness of particle size distribution As an index of the particle size distribution, a detergent particle group that has been passed through a 1410 ⁇ m sieve is fitted, and a Rosin-Rammler number (RR number) is calculated and used. The following formula is used to calculate the number of Rosin-Rammlers.
- n is preferably 1.5 or more, more preferably 2.0 or more, from the viewpoint of improving solubility.
- solubility As a solubility index in the present invention, a 60-second dissolution rate of a detergent particle group described below can be used.
- the dissolution rate is preferably 90% or more, and more preferably 95% or more.
- the dissolution rate of the detergent particle group for 60 seconds is calculated by the following method. 1 liter of hard water (Ca / Mg molar ratio 7/3) adjusted to 20 ° C. corresponding to a hardness of 71.2 mg CaCO 3 / liter, 1 liter beaker (inner diameter 105 mm, height 150 mm cylindrical type, for example, manufactured by Iwaki Glass Co., Ltd.) Filled into a 1 liter glass beaker and kept constant at a water temperature of 20 ° C.
- stirrer length 35 mm, diameter 8 mm, for example, model: ADVANTEC, Teflon (registered trademark) SA ( In the round thin type)
- stirring is performed at a rotational speed (800 r / m) at which the depth of the vortex with respect to the water depth is approximately 1/3.
- the detergent particles which have been reduced and weighed so as to be 1.000 ⁇ 0.0010 g, are charged and dispersed in water with stirring, and stirring is continued.
- the detergent particle group dispersion in the beaker is filtered through a standard sieve (diameter: 100 mm) having an opening of 74 ⁇ m as defined in JIS Z 8801, which has a known weight, and the detergent particles in the water state remaining on the sieve are filtered. Collect in an open container with known weight along with sieve. The operation time from the start of filtration until the sieve is collected is 10 ⁇ 2 seconds.
- the collected residue of detergent particles is dried in an electric dryer heated to 105 ° C. for 1 hour, and then cooled in a desiccator (25 ° C.) containing silica gel for 30 minutes. After cooling, the total weight of the dissolved residue of the dried detergent, the sieve, and the collection container is measured, and the dissolution rate (%) of the detergent particle group is calculated by the equation (1).
- Dissolution rate (%) ⁇ 1 ⁇ (T / S) ⁇ ⁇ 100 (1)
- S input weight of detergent particles (g)
- T When the aqueous solution obtained under the above stirring conditions is subjected to the sieve, the dry weight (g) of the residue of the detergent particles remaining on the sieve
- Linear alkylbenzene sulfonic acid (LAS), “Neopelex GS” manufactured by Kao Corporation ⁇ Other raw materials
- Polyoxyethylene alkyl ether (POE) “Emulgen 121” manufactured by Kao Corporation
- Zeolite Average particle size of 3.5 ⁇ m, manufactured by Zeobuilder Co., Ltd.
- Pulverized salt cake An average particle size of 200 ⁇ m pulverized to an average particle size of 10 ⁇ m
- a 75 L drum type mixer ( ⁇ 40 cm ⁇ L60 cm) having a baffle plate was used as a container rotating mixer.
- a two-fluid nozzle (manufactured by Atmax Co., Ltd .: model number BN90) was used.
- Example 1 100 parts by weight of light ash (5.7 kg; 22 times the neutralization equivalent) was stirred in a drum mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 28.4 parts by weight of LAS at 60 ° C. was sprayed with a two-fluid nozzle under a spraying condition of an addition rate of 4.1% / min and an atomizing air spraying pressure of 0.3 MPa. Added for 3 minutes and stirred for 3 minutes after addition. Thereafter, stirring was stopped, 3.9 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the obtained detergent particles were discharged from the mixer. In addition, it was 35 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Example 2 100 parts by weight of light ash (5.5 kg; 18 times the neutralization equivalent) was stirred in a drum-type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 35.4 parts by weight of LAS at 60 ° C. was applied with a two-fluid nozzle under a spraying condition of an addition rate of 4.3% / min and an atomization air pressure of 0.3 MPa for atomization. Added for 3 minutes and stirred for 3 minutes after addition. Thereafter, stirring was stopped, 6.8 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the obtained detergent particles were discharged from the mixer. In addition, it was 35 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Example 3 100 parts by weight of light ash (5.5 kg; 18 times the neutralization equivalent) was stirred in a drum-type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 35.4 parts by weight of LAS at 60 ° C. was sprayed with a two-fluid nozzle under a spraying condition of an addition rate of 8.1% / min and an atomization air spray pressure of 0.44 MPa for atomization. Added for 3 minutes and stirred for 3 minutes after addition. Thereafter, stirring was stopped, 4.1 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the resulting detergent particles were discharged from the mixer. In addition, it was 46 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Example 4 100 parts by weight of light ash (5.5 kg; 18 times the neutralization equivalent) was stirred in a drum-type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 35.4 parts by weight of LAS at 60 ° C. was sprayed with a two-fluid nozzle under a spray condition of an addition rate of 8.1% / min and an atomization air spray pressure of 0.17 MPa. Added for 3 minutes and stirred for 3 minutes after addition. Thereafter, stirring was stopped, 4.1 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the resulting detergent particles were discharged from the mixer. In addition, it was 98 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Example 5 100 parts by weight of light ash (5.5 kg; 18 times the neutralization equivalent) was stirred in a drum-type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 35.4 parts by weight of LAS at 60 ° C. was sprayed with a two-fluid nozzle under a spray condition of an addition rate of 8.1% / min and an atomization air spray pressure of 0.14 MPa. Added for 3 minutes and stirred for 3 minutes after addition. Thereafter, stirring was stopped, 4.1 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions, and the resulting detergent particles were discharged from the mixer. In addition, when the spray droplet diameter (average particle diameter) of LAS under this spray condition was measured, it was 133 ⁇ m.
- Example 6 100 parts by weight of pulverized light ash (4.9 kg; 12 times the neutralization equivalent) was stirred in a drum mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 54.5 parts by weight of LAS at 60 ° C. was added with a two-fluid nozzle for 11.0 minutes under a spraying condition of an addition rate of 4.9% / min and an atomization pressure of 0.3 MPa for atomization. And stirred for 3 minutes after the addition. Thereafter, stirring was stopped, 4.7 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the resulting detergent particles were discharged from the mixer. In addition, it was 35 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Example 7 100 parts by weight of pulverized light ash and 100 parts by weight of dense ash (5.8 kg; 24 times the neutralization equivalent) were stirred in a drum-type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 50.3 parts by weight of LAS at 60 ° C. was applied with a two-fluid nozzle for 6.3 minutes under a spray condition of an addition rate of 4.0% / min and an atomization pressure of 0.3 MPa for atomization. And stirred for 3 minutes after the addition. Thereafter, stirring was stopped, 5.0 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the obtained detergent particles were discharged from the mixer. In addition, it was 35 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Example 8 100 parts by weight of light ash (2.4 kg; 9 times the neutralization equivalent) and 133 parts by weight of pulverized mirabilite were stirred in a drum type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 46.7 parts by weight of LAS and 4.7 parts by weight of 98% sulfuric acid were mixed in advance, and the temperature was adjusted to 60 ° C., and the addition rate was 7.2% / min with a two-fluid nozzle. It added in 2.8 minutes on the spray conditions of Air spray pressure 0.3MPa, and stirred for 2 minutes after the addition. Thereafter, 10.0 parts by weight of polyoxyethylene alkyl ether was added in 0.5 minutes, followed by stirring for 2 minutes.
- Example 9 100 parts by weight of light ash (1.9 kg; 7 times the neutralization equivalent) and 213 parts by weight of pulverized mirabilite were stirred in a drum type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 65.2 parts by weight of LAS and 6.5 parts by weight of 98% sulfuric acid were mixed in advance, and then the temperature was adjusted to 60 ° C., and the addition rate was 7.5% / min with a two-fluid nozzle. It added in 2.8 minutes on the spray conditions of Air spray pressure 0.3MPa, and stirred for 2 minutes after the addition. Thereafter, 8.7 parts by weight of polyoxyethylene alkyl ether was added in 0.5 minutes, followed by stirring for 2 minutes.
- Comparative Example 1 100 parts by weight of light ash (5.5 kg; 18 times the neutralization equivalent) was stirred in a drum-type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 30 seconds, 35.4 parts by weight of LAS at 60 ° C. was sprayed using a one-fluid nozzle (manufactured by Spraying Systems Japan Co., Ltd .: Model No. Unijet 8003) at an addition rate of 13.0% / min. In 2.7 minutes, and stirred for 3 minutes after the addition. Thereafter, stirring was stopped, 6.8 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the obtained detergent particles were discharged from the mixer. In addition, it was 860 micrometers when the spraying droplet diameter (average particle diameter) of LAS in this spraying condition was measured.
- Comparative Example 2 100 parts by weight of light ash (26.4 kg; 22 times the neutralization equivalent) was stirred in a Redige mixer FKM-130D (manufactured by Matsubo). After stirring for 30 seconds under the conditions of a stirring blade rotation speed of 130 r / m and a shearing machine rotation speed of 3600 r / m, 28.4 parts by weight of LAS at 60 ° C. was added to a two-fluid nozzle (manufactured by Spraying Systems Japan Co., Ltd. SU29) was added in 7.0 minutes at an addition rate of 4.1% / min and an air spray pressure for atomization of 0.3 MPa, and the mixture was stirred for 3 minutes after the addition.
- a two-fluid nozzle manufactured by Spraying Systems Japan Co., Ltd. SU29
- Comparative Example 3 100 parts by weight of light ash (25.3 kg; 18 times the neutralization equivalent) was stirred in a Redige mixer FKM-130D (manufactured by Matsubo). After stirring for 30 seconds under the conditions of a stirring blade rotation speed of 130 r / m and a shearing machine rotation speed of 3600 r / m, 35.4 parts by weight of LAS at 60 ° C. was made into one fluid nozzle (manufactured by Spraying Systems Japan Co., Ltd. Unijet 8010) was added at a rate of 10.5% / min in 3.4 minutes and stirred for 3 minutes after the addition.
- Comparative Example 4 100 parts by weight (4.93 kg) of light ash was stirred in a drum type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 10 seconds, 35.2 parts by weight of polyoxyethylene lauryl ether (Emulgen 106 manufactured by Kao Corporation) at 60 ° C. was added to a two-fluid nozzle (addition rate 3.7% / min, Air spraying pressure for atomization of 0. 3 MPa) and added in 9.4 minutes. After the addition, granulation was continued by further mixing for 1 minute. Thereafter, stirring was stopped, 6.8 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the obtained detergent particles were discharged from the mixer.
- polyoxyethylene lauryl ether Emulgen 106 manufactured by Kao Corporation
- Comparative Example 5 100 parts by weight (4.93 kg) of light ash was stirred in a drum type mixer (rotation speed 30 r / m, fluid number 0.2). After stirring for 10 seconds, 35.2 parts by weight of polyoxyethylene lauryl ether (Emulgen 106 manufactured by Kao Corporation) at 60 ° C. was added to a two-fluid nozzle (addition rate 3.7% / min, Air spraying pressure for atomization of 0. 3 MPa) and added in 9.4 minutes. After the addition, granulation was continued by further mixing for 1 minute. Thereafter, stirring was stopped, 40.9 parts by weight of zeolite was added, stirring was performed for 1 minute under the same conditions as described above, and the resulting detergent particles were discharged from the mixer.
- polyoxyethylene lauryl ether Emulgen 106 manufactured by Kao Corporation
- composition, conditions, and results of the detergent particle group raw materials in the above examples are shown in the following table.
- the detergent particle groups obtained in Examples 1 to 9 have a detergent yield as high as 80% or more, and the Rosin-Rammler number (RR number in the table), which is an index of particle size distribution, is 1.5 or more. It was found that particles with a sharp distribution were obtained in high yield.
- Comparative Example 1 the detergent yield was as low as 67%, the Rosin-Rammler number was 1.0, and it was found that the particle size distribution of the obtained detergent particles was broadened. As for Comparative Example 2, although no decrease in yield was observed, it was found that the Rosin-Rammler number was 1.1, and the particle size distribution of the obtained detergent particles was broadened. In Comparative Example 2, many deposits on the wall surface and the stirring shaft in the mixer were observed. In Comparative Example 4, the obtained detergent particle group was a wet powder, and physical properties could not be measured.
- Comparative Example 5 a detergent particle group capable of measuring physical properties was obtained by increasing the amount of zeolite as compared with Comparative Example 4, and the average particle diameter of the obtained detergent particle group was 138 ⁇ m. Since the average particle diameter of the light ash before granulation was 100 ⁇ m, granulation hardly progressed, and this is because the adhesiveness when contacting with the powder is weak.
- Example 2 Regarding the solubility, from the comparison between Example 2 and Comparative Example 3, the dissolution rate of Example 2 is 97%, while the dissolution rate of Comparative Example 3 is 78%. Despite the large average particle size, the dissolution rate was excellent.
- Example 3 the detergent yield was better in Example 3 in which the average particle diameter of the acid precursor droplet size was made finer.
- a detergent particle group having a sharp particle size distribution and excellent solubility can be produced with high yield.
- Such a detergent particle group can be preferably used as a detergent composition for various uses such as clothing, or as one component of such a detergent composition.
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Abstract
Description
(1)非石鹸性陰イオン界面活性剤の酸前駆体
非石鹸性陰イオン界面活性剤の酸前駆体とは、非石鹸性陰イオン界面活性剤の前駆体であって酸形態を示し、常温で液状のものをいい、中和反応により塩を形成するものである。よって酸前駆体としては、公知の非石鹸性陰イオン界面活性剤の前駆体であって上記の性質を有するものであれば特に限定されないが、直鎖アルキルベンゼンスルホン酸(LAS)、α-オレフィンスルホン酸(AOS)、アルキル硫酸(AS)、内部オレフィンスルホン酸、脂肪酸エステルスルホン酸、アルキルエーテル硫酸、ジアルキルスルホコハク酸等が挙げられる。このような酸前駆体は一成分のみを用いても良く、二成分以上を組み合わせて用いても良い。中でも、経済性、保存安定性及び泡立ちの観点からは直鎖アルキルベンゼンスルホン酸(LAS)が好ましい。
アルカリ性粉体原料としては、通常洗剤組成物においてアルカリ剤として用いられるものが挙げられ、炭酸ナトリウム、炭酸水素ナトリウム、ケイ酸ナトリウム、炭酸カリウム、炭酸カルシウム等が例示される。これらは単独で用いても良く、二種以上を混合して用いても良い。アルカリ性粉体原料の中でも、好ましい実施態様として炭酸ナトリウムが挙げられる。
容器回転型混合機としては、ドラム型混合機或いはパン型混合機が好ましい。ドラム型混合機としては、ドラム状の円筒が回転して処理を行うものであれば特に限定されるものではなく、水平又はわずかに傾斜させたドラム型混合機の他に円錐ドラム型造粒機(混合機)、多段円錐ドラム型造粒機(混合機)等も使用可能である。これらの装置はバッチ式、連続式いずれの方法においても用いることができる。
フルード数:Fr=V2/(R×g)
V:周速[m/s]
R:回転中心から回転物の円周までの半径[m]
g:重力加速度[m/s2]
容器回転型混合機には、一般に洗剤組成物の分野に用いられる公知の物質を合わせて添加してもよい。
本発明においては、酸前駆体を多流体ノズルを用いて供給することが好ましい。かかるノズルを用いることにより、その液滴を微細化して分散させることができる。多流体ノズルとは、液体と微粒化用気体(エアー、窒素等)を独立の流路を通してノズル先端部近傍まで流通させて混合・微粒化するノズルであり、2流体ノズルや3流体ノズル、4流体ノズル等を用いることができる。また、酸前駆体と微粒化用気体の混合部は、ノズル先端部内で混合する内部混合型、或いはノズル先端部外で混合する外部混合型のいずれであっても良い。
本発明においては、さらにその他の液体成分を添加して洗剤粒子群を製造してもよい。添加されるその他の液体成分としては、得ようとする洗剤粒子群の組成に応じて適宜選択することができ、所望の液体成分を用いることができる。液体成分の添加時期は特に限定されるものではなく、例えば、酸前駆体とアルカリ性粉体原料とを乾式中和する工程の前又はその途中、或いは後に行ってもよいが、表面改質剤を添加する場合には、表面改質剤の添加前が好ましい。
上記のようにして製造される洗剤粒子群に、さらに所望の成分を添加することによって洗剤組成物を製造することができる。即ち、本発明の洗剤組成物は、本発明の製造方法によって得られる洗剤粒子群を含有してなるものである。
本発明により得られる洗剤粒子群等の物性の指標としは、嵩密度や平均粒径、及び流動性が挙げられる。また生産性の指標として洗剤収率が挙げられる。洗剤粒子群の嵩密度としては、400~1000g/Lが好ましい。洗剤粒子群の平均粒径としては、200~800μmが好ましく、200~600μmがより好ましく、260~600μmが更に好ましい。洗剤粒子群の流動性としては、4~10秒が好ましく、4~7秒がより好ましい。洗剤収率としては、100%に近ければ近い程好ましく、例えば、80~100%が好ましく、90~100%がより好ましい。
1.平均粒径
平均粒径については、JIS Z 8801の標準篩(目開き2000~45μm)を用いて5分間振動させた後、篩目のサイズによる重量分率からメジアン径を算出する。より詳細には、目開き45μm、63μm、90μm、125μm、180μm、250μm、355μm、500μm、710μm、1000μm、1410μm、2000μmの12段の篩と受け皿を用いて、受け皿上に目開きの小さな篩から順に積み重ね、最上部の2000μmの篩の上から100gの粒子を添加し、蓋をしてロータップ型ふるい振とう機(HEIKO製作所製、タッピング156回/分、ローリング:290回/分)に取り付け、5分間振動させたあと、それぞれの篩及び受け皿上に残留した当該粒子の重量を測定し、各篩上の当該粒子の重量割合(%)を算出する。受け皿から順に目開きの小さな篩上の当該粒子の重量割合を積算していき合計が50%となる粒径を平均粒径とする。
嵩密度は、JIS K 3362により規定された方法で測定する。なお、嵩密度は、2000μmの篩上に残留した粒子をカットした残りの粒子にて測定する。
流動時間は、JIS K 3362により規定された嵩密度測定用のホッパーから、100mLの粉末が流出するのに要する時間とする。流動時間として10秒以下が好ましく、8秒以下がより好ましく、7秒以下が更に好ましい。なお、流動性は、2000μmの篩上に残留した粒子をカットした残りの粒子にて測定する。
本発明における洗剤収率とは、製造された洗剤粒子群中の、1410μm以下の粒子の割合を示す。
1.粒度分布のシャープさ
粒度分布の指標としては、1410μmの篩を通過させた洗剤粒子群をフィッティングし、Rosin-Rammler数(R-R数)を算出して用いる。Rosin-Rammler数の算出には以下の式を用いる。
R(Dp):粒径Dpμm以上の粉体の累積率〔%〕
Dp:粒径〔μm〕
n:Rosin-Rammler数
β:粒度特性係数
より詳細には、上記平均粒径の測定と同様の方法により、それぞれの篩及び受け皿上に残留した該粒子の重量を測定し、各篩(目開きDp[μm])上の該粒子の重量割合(累積率R(Dp)[μm])を算出する。そして、各logDpに対するlog(log(100/R(Dp)))をプロットした時の最小2乗近似直線の傾きnを、Rosin-Rammler数とする。
本発明における溶解性の指標としては、以下に説明する洗剤粒子群の60秒間溶解率を用いることができる。溶解率は90%以上が好ましく、95%以上がより好ましい。
硬度が71.2mgCaCO3/リットルに相当する20℃に調整した1リットルの硬水(Ca/Mgモル比7/3)を1リットルビーカー(内径105mm、高さ150mmの円筒型、例えば岩城硝子社製1リットルガラスビーカー)の中に満たし、20℃の水温をウォーターバスにて一定に保った状態で、撹拌子(長さ35mm、直径8mm、例えば型式:ADVANTEC社製、テフロン(登録商標)SA(丸型細型))にて水深に対する渦巻きの深さが略1/3となる回転数(800r/m)で撹拌する。1.0000±0.0010gとなるように縮分・秤量した洗剤粒子群を撹拌下に水中に投入・分散させ撹拌を続ける。投入から60秒後にビーカー中の洗剤粒子群分散液を、重量既知のJIS Z 8801に規定の目開き74μmの標準篩(直径100mm)で濾過し、篩上に残留した含水状態の洗剤粒子群を篩と共に重量既知の開放容器に回収する。なお、濾過開始から篩を回収するまでの操作時間を10±2秒とする。回収した洗剤粒子群の溶残物を105℃に加熱した電気乾燥機にて1時間乾燥し、その後、シリカゲルを入れたデシケーター(25℃)内で30分間保持して冷却する。冷却後、乾燥した洗剤の溶残物と篩と回収容器の合計の重量を測定し、式(1)によって洗剤粒子群の溶解率(%)を算出する。
S:洗剤粒子群の投入重量(g)
T:上記撹拌条件にて得られた水溶液を上記篩に供したときに、篩上の残存する洗剤粒子群の溶残物の乾燥重量(g)
・アルカリ性粉体原料
ライト灰:平均粒径100μm、セントラル硝子(株)製
粉砕ライト灰:平均粒径8μm(上記ライト灰を粉砕したもの)
デンス灰:平均粒径300μm、セントラル硝子(株)製
・非石鹸性陰イオン界面活性剤の酸前駆体
直鎖アルキルベンゼンスルホン酸(LAS)、花王(株)製「ネオペレックスGS」
・他の原料
ポリオキシエチレンアルキルエーテル(POE)、花王(株)製「エマルゲン121」
ゼオライト:平均粒径3.5μm、ゼオビルダー社製
粉砕芒硝:平均粒径200μmのものを平均粒径10μmに粉砕したもの
ライト灰100重量部(5.7kg;中和当量の22倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの28.4重量部を2流体ノズルにて、添加速度4.1%/min、微粒化用Air噴霧圧0.3MPaの噴霧条件にて、6.9分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト3.9重量部を添加して前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、35μmであった。
ライト灰100重量部(5.5kg;中和当量の18倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの35.4重量部を2流体ノズルにて、添加速度4.3%/min、微粒化用Air噴霧圧0.3MPaの噴霧条件にて、8.2分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト6.8重量部を添加して前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、35μmであった。
ライト灰100重量部(5.5kg;中和当量の18倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの35.4重量部を2流体ノズルにて、添加速度8.1%/min、微粒化用Air噴霧圧0.44MPaの噴霧条件にて、4.4分間で添加し、添加後3分間撹拌した。その後撹拌を止めゼオライト4.1重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、46μmであった。
ライト灰100重量部(5.5kg;中和当量の18倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの35.4重量部を2流体ノズルにて、添加速度8.1%/min、微粒化用Air噴霧圧0.17MPaの噴霧条件にて、4.4分間で添加し、添加後3分間撹拌した。その後撹拌を止めゼオライト4.1重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、98μmであった。
ライト灰100重量部(5.5kg;中和当量の18倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの35.4重量部を2流体ノズルにて、添加速度8.1%/min、微粒化用Air噴霧圧0.14MPaの噴霧条件にて、4.4分間で添加し、添加後3分間撹拌した。その後撹拌を止めゼオライト4.1重量部を添加して、同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、133μmであった。
粉砕ライト灰100重量部(4.9kg;中和当量の12倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの54.5重量部を2流体ノズルにて、添加速度4.9%/min、微粒化用Air噴霧圧0.3MPaの噴霧条件にて11.0分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト4.7重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、35μmであった。
粉砕ライト灰100重量部及びデンス灰100重量部(5.8kg;中和当量の24倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの50.3重量部を2流体ノズルにて、添加速度4.0%/min、微粒化用Air噴霧圧0.3MPaの噴霧条件にて6.3分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト5.0重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、35μmであった。
ライト灰100重量部(2.4kg;中和当量の9倍)、粉砕芒硝133重量部をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、LASの46.7重量部及び98%硫酸4.7重量部を予め混合した後、60℃とし、2流体ノズルにて、添加速度7.2%/min、微粒化用Air噴霧圧0.3MPaの噴霧条件にて、2.8分間で添加し、添加後2分間撹拌した。その後、ポリオキシエチレンアルキルエーテル10.0重量部を0.5分間で添加し、添加後2分間撹拌した。その後、ポリアクリル酸ナトリウム2.3重量部を0.5分間で添加し、添加後2分間撹拌した。その後撹拌を止め、ゼオライト6.7重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、58μmであった。
ライト灰100重量部(1.9kg;中和当量の7倍)、粉砕芒硝213重量部をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、LASの65.2重量部及び98%硫酸6.5重量部を予め混合した後、60℃とし、2流体ノズルにて、添加速度7.5%/min、微粒化用Air噴霧圧0.3MPaの噴霧条件にて、2.8分間で添加し、添加後2分間撹拌した。その後、ポリオキシエチレンアルキルエーテル8.7重量部を0.5分間で添加し、添加後2分間撹拌した。その後、ポリアクリル酸ナトリウム2.6重量部を0.5分間で添加し、添加後2分間撹拌した。その後撹拌を止め、ゼオライト21.7重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、58μmであった。
ライト灰100重量部(5.5kg;中和当量の18倍)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。30秒撹拌した後、60℃のLASの35.4重量部を1流体ノズル(スプレーイングシステムスジャパン(株)製:型番Unijet 8003)を用いて、添加速度13.0%/minの噴霧条件にて2.7分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト6.8重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、860μmであった。
ライト灰100重量部(26.4kg;中和当量の22倍)をレディゲミキサーFKM-130D((株)マツボー製)中で撹拌した。撹拌羽根回転数130r/m、剪断機回転数3600r/mの条件で30秒間撹拌した後、60℃のLASの28.4重量部を2流体ノズル(スプレーイングシステムスジャパン(株)製:型番SU29)を用いて4.1%/minの添加速度、微粒化用Air噴霧圧0.3MPaの添加条件にて、7.0分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト6.4重量部を添加して、前記と同条件にて1分間撹拌し、得られた洗剤粒子群をレディゲミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、60μmであった。
ライト灰100重量部(25.3kg;中和当量の18倍)をレディゲミキサーFKM-130D((株)マツボー製)中で撹拌した。撹拌羽根回転数130r/m、剪断機回転数3600r/mの条件で30秒間撹拌した後、60℃のLASの35.4重量部を1流体ノズル(スプレーイングシステムスジャパン(株)製:型番Unijet 8010)を用いて10.5%/minの添加速度にて、3.4分間で添加し、添加後3分間撹拌した。その後撹拌を止め、ゼオライト6.8重量部を添加して、前記と同条件にて1分間撹拌し、得られた洗剤粒子群をレディゲミキサーから排出した。なお、この噴霧条件におけるLASの噴霧液滴径(平均粒径)を測定したところ、510μmであった。
ライト灰100重量部(4.93kg)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。10秒間撹拌した後、60℃のポリオキシエチレンラウリルエーテル(花王(株)製エマルゲン106)35.2重量部を2流体ノズル(添加速度3.7%/min、微粒化用Air噴霧圧0.3MPa)を用いて、9.4分間で添加した。添加後、さらに混合を1分間続けて顆粒化を行った。その後攪拌を止め、ゼオライト6.8重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。
ライト灰100重量部(4.93kg)をドラム型ミキサー(回転数30r/m、フルード数0.2)中で撹拌した。10秒間撹拌した後、60℃のポリオキシエチレンラウリルエーテル(花王(株)製エマルゲン106)35.2重量部を2流体ノズル(添加速度3.7%/min、微粒化用Air噴霧圧0.3MPa)を用いて、9.4分間で添加した。添加後、さらに混合を1分間続けて顆粒化を行った。その後攪拌を止め、ゼオライト40.9重量部を添加して、前記と同条件にて1分間撹拌を行い、得られた洗剤粒子群をミキサーから排出した。
Claims (8)
- 非石鹸性陰イオン界面活性剤の酸前駆体をアルカリ性粉体原料で乾式中和する工程を含む洗剤粒子群の製造方法であって、乾式中和に容器回転型混合機を使用し、該酸前駆体をその液滴径の平均粒径が200μm以下で供給することを特徴とする、洗剤粒子群の製造方法。
- 非石鹸性陰イオン界面活性剤の酸前駆体の供給を多流体ノズルを用いて行う、請求項1に記載の製造方法。
- 添加されるアルカリ性粉体原料の量が、非石鹸性陰イオン界面活性剤の酸前駆体の中和当量の1~35倍の量である、請求項1又は2に記載の製造方法。
- 得られる洗剤粒子群中に非石鹸性陰イオン界面活性剤が10~45重量%含有される、請求項1~3のいずれか1項に記載の製造方法。
- アルカリ性粉体原料の平均粒径が1~500μmである、請求項1~4のいずれか1項に記載の製造方法。
- 洗剤粒子群の嵩密度が400~1000g/Lである、請求項1~5のいずれか1項に記載の製造方法。
- 洗剤粒子群中にアルカリ金属アルミノ珪酸塩0.1~20重量%を含有する、請求項1~6のいずれか1項に記載の製造方法。
- 請求項1~7のいずれか1項に記載の製造方法によって得られる洗剤粒子群を含有してなる洗剤組成物。
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JP2006509855A (ja) * | 2002-12-12 | 2006-03-23 | ヘンケル・コマンディットゲゼルシャフト・アウフ・アクチエン | 乾式中和法ii |
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JPH06502212A (ja) * | 1990-10-03 | 1994-03-10 | ザ、プロクター、エンド、ギャンブル、カンパニー | 粒状感pH界面活性剤を含有する高密度洗剤組成物の製法 |
JP2006509855A (ja) * | 2002-12-12 | 2006-03-23 | ヘンケル・コマンディットゲゼルシャフト・アウフ・アクチエン | 乾式中和法ii |
JP2005239786A (ja) * | 2004-02-24 | 2005-09-08 | Lion Corp | ノニオン界面活性剤含有粒子及びその製造方法並びに洗剤組成物 |
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