• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    THE METHOD OF PREPARING GRANULATED DETERGENTS in the apparatus, with fluidized bed) 1st layer by spraying liquid detergent substances onto powdered skeletal substances under known conditions with the addition of powdered detergent substances after mixing them for granulating at 10-100 ° C, which is different. As one of the powdered skeletal substances, sodium tripolyphosphate is used with a P content of 90-100% and an apparent density of more than 700 g / l, preferably 900-1000 g / l, with a fine fraction with a grain diameter of and less than 0.2 mm in the amount of 70-100% and when moving and granulating the gas velocity in the working area of the inhomogeneous fluidized bed is set between the velocity of the fluidization point of the largest particles and the ten-fold speed of ablation of the middle particles, with the gas consumption being 8002000 kg / m, solids 3001000 kg / m and liquid substances 60 200 kg / m.
    公开号:SU1081203A1
    申请号:SU797770975
    申请日:1979-12-13
    公开日:1984-03-23
    发明作者:Манфред Миттельстрас；Лотар МЕРЛЬ；Ханс-Йоахим Кюнне；Йоахим Заксе；Эберхард Шмидт；Вольфганг Шультц；Норберт Зиг
    申请人:Феб Вашмиттельверк Гентин (Инопредприятие)；
    IPC主号:
    专利说明:

    I p-d1 L--}. 1 The invention relates to methods for the continuous preparation of granular detergents and cleaning agents in fluidized bed apparatus. A known method of continuous preparation of granular detergent, in which liquid detergents are sprayed onto powdered skeletal substances under known conditions, with the addition of powdered detergents after mixing them for granulation, preferably at 10-100 C. by spraying powdered (skeletal) skeletal substances with liquid detergent substances in pneumatic mixers. At the same time, powdered skeletal substances are either mixed in advance and then fed into the pneumatic mixer, or individually continuously fed into it from the supply tanks. During the pneumatic mixing process, powdered skeletal substances are sprayed with detergents. The water contained in the detergent is bound to the powdered skeletal substances in the form of water of crystallization or is evaporated due to the heated air. The known methods of pneumatic mixing allow the use of powdered skeletal substances accepted in industry, producing detergents, but their physicochemical parameters have special requirements. In order to avoid the heterogeneity of the final products, skeletal substances with approximately the same apparent densities and approximately the same particle size distribution are used, which are mainly obtained by spray drying. The standard detergents according to the description of the invention to the German Patent Application No. 1283427, laid out in an accepted patent application, contain 40-50% pentane sodium triphosphate (sodium tripolyphosphate), which, together with the water used, is hydrated to the hydrochloride in significant amounts. Hexahydrate is formed in the case of sodium tripolyphosphate containing 3 phase II (grain size 0.2 mm 30), but only after leaving the mixture ate, which takes a longer time to mature. At the same time, under the influence of heat generated, thermally unstable components of detergents such as, for example, disintegrate. perborate sodium. This entails a deterioration in whitening ability. In order to avoid these difficulties, it is known that sodium tripolyphosphate with approximately 40- 80% w / w phase 1 and apparent density of 550-700 g / l is used in mixers with vortex air flow. From Austrian patent 297895 it follows that the mixture of individual grains formed as a result of hydration into granules is relatively weak, so that the final products have little mechanical strength. It is also known (s6FW102jR 8/76, pp. 205-208) that the use of pentane sodium triphosphate is possible if the water contained in the liquid raw material is evaporated by hot air. The disadvantage of this method is that when using 40-50% tripolyphosphate with an apparent density of S: 100 g / l, the final product is obtained with apparent densities of 800 g / l. At the same time, this method allows the use of a maximum of 15% liquid detergent. In addition, the use of hot air is associated with relatively high and uneconomical energy consumption. The purpose of the invention is to develop a method for the continuous production of granular detergents and detergents, which, with high-quality detergents and detergents (detergents), require reduced manufacturing costs, especially lower energy costs. The purpose of the invention is to develop a method for the continuous production of granular detergents and cleaning agents in fluidized bed apparatus, which does not have special requirements for the powdered skeletal substances sprayed with detergents with regard to their chemical and physical properties, especially the apparent density. 3 granulometric cocrasfa and water content. When using water-containing substances, there should be no need for special technological costs. The target product must have a high mechanical strength. V.). The goal is achieved in that according to the method for producing granulated detergent in a fluidized bed apparatus by spraying liquid detergent substances on powdered skeletal substances under known conditions with powdered detergents added after mixing to granulate at 10-100 ° C, as one of the powdered skeletal alloys use sodium tripolyphosphate with a phase content of P of 90-100 and an apparent density of more than 700 g / l, preferably 900-1000 g / m, with a content of fine fractions Cuts with a grain diameter of less than 0.2 mm in an amount of 70-100% and with stirring and granulating the gas velocity in the working area of the non-homogeneous fluidized bed establish between the velocity of the fluidization point of the largest particles and the ten-fold velocity of ablation of medium particles, and the gas consumption 800-2000 kg / m; solids 300-1000 kg / m; and liquid substances 60200 kg / m. The drawing is a diagram, implementing the proposed method. Powdered skeletal substances from the system of hoppers 1 are fed to the weights 3 via the respective conveyors 2. From the weights, weighed powder and different skeletal substances are fed in batches directly into a known mechanical mixer 4 and mixed. During the mixing process, a dosage pump 5 adds 0-10%, preferably -57 liquid detergents and / or mixtures of several detergents, mainly non-ionic compounds, fed from a supply and mixing tank system 6. Mixed powdered skeletal substances from the mixer 4 through the respective conveyors enter the intermediate bunker 8, and from it through the cell drum sluice gate 9 and the metering conveyor scales 10 - into the loading 0J4 funnel of the transporting screw 11 and the drum cell head zovoy the shutter 12. Mixed powdered skeletal substances using a transporting screw is loaded into the pneumatic loading and unloading device 13 and, thus, into the apparatus with a fluidized bed 14. Using the gas flow 15 generated by the blower 16 and controlled by the regulating device 17, powder skeletal substances are kept in suspension above the base of their leakage 15 and vigorously mixed. During the mixing process through one or more known spraying devices 18, 5-30%, preferably 12-17%, of a liquid detergent or a mixture of liquid detergents or their acid form products, mainly alkyl benzene sulphonic acids and fatty acids, or The mixtures supplied from the supply and mixing tank system 6 are sprayed onto the powdered skeletal substances through the constant pressure regulator 20 through the constant pressure regulator 20. During intensive mixing in the vortex chamber 21, powdered skeletal substances are granulated with sprayed liquid detergents. The resulting granules are withdrawn from the fluidized bed apparatus via a pneumatic loading device 12 and a drum cell lock valve 22 and are discharged using suitable conveyors 23. Air flow from the top of the fluidized bed apparatus is fed to one or more cyclones , free from trapped dust particles or release into the atmosphere. Separated in a cyclone 24, particles are pumped through a drum cell sluice gate 25 are fed to the conveyor auger 11 and, with the aid of Gu, together with mixed powdered skeletal substances are reintroduced into the fluidized bed apparatus. Example 1. 85% of a mixture consisting of 40% pentane sodium triphosphate (patriotol polyphosphate) {apparent with a density of 1000 g / l, 80 less than 0.2 mm, phase content 11-95 y, 10%
    soda ash, 25.8% sodium sulfate, 14% sodium perborate. 4% sodium disilicate, 3% magnesium silicate, 1% CMC, 0.2% optical brightener, and 2% non-ionic compounds are continuously fed to the fluidized bed apparatus. This mixture is sprayed with 15% of a mixture consisting of 10 h of dodecylbenzenesulfonic acid and 7 h of fatty acid. The result is a dust free bulk detergent with an apparent density of 530 g / l.
    Example 2: 83% of a mixture consisting of 40% pentane sodium -; rosfat (seemingly density 1000 g / l, 80%: less than 0.2 mm, phase content P 95%), 10% soda ash, 15.3% sodium sulfate, 10% soap powder, 6% sodium silicate, 3% magnesium sulphate, 1% CMC, 0.2% optical bleach and 14% sodium perborate are continuously fed into a fluidized bed apparatus and sprinkled with 17% dodecylbenzenesulfonic acid. A free dust free detergent is obtained with an apparent raft weight of about 580 g / l.
    Example 3. 83% of the mixture consisted of 40% pentane sodium triphosphate (apparent density of 1000 g / l, 80% less than 0.2 mm, phase II content 95% 10% soda ash, 15.3% sodium sulfate, 10% soap powder, 6% sodium disilicate, 3% magnesium sulphate, 1% CMC and 0.2% optical bleach are continuously fed to a fluidized bed apparatus and sprayed with 14% of a mixture consisting of Yuch dodecylbenzenesulfonic acid and 5 hours of fatty acid, and tar: same 3% non-ionic compounds. As a result, a free flowing detergent with an apparent density of 550 g / l is obtained.
    D ime 4. 84% of the mixture, consisting of 35% pentane sodium triphosphate (bulk density 1050 g / l, 75% less than 0.2 mm, phase II content 93%), 15% soda ash, 30% sodium sulfate , 1% carboxymethylcellulose, 0.2% optical bleach, and 18.8% sodium silicate are injected continuously into the fluidized bed apparatus and irrigated with 16% dodecylbenzenesulfonic acid.
    A detergent is obtained with a bulk density of 730 g / l. Area consumption per hour: air 1800 kg / m solids 750 kg / m and liquid 193 kg / m.
    Example 5. 88% of a mixture composed of 42% pentanate triphosphate (bulk density 800 g / l, 85% less than 0.2 mm, phase II content 99%), 10% soda ash, 10% sodium sulfate, 18% perborate-sodium , 3% magnesium silicate, 1% carboxymethyl cellulose, 0.2% optical brightener and 15.8% sodium disilicate, are injected in a continuous fluidized bed apparatus and irrigate 12% of a mixture consisting of 60% dodecylbenzenesulfonic acid, 30% fat acids and 10% nonionics. A detergent is obtained with a bulk density of 600 g / l. Flow rate per hour: air 1000 kg / m, solids 600 kg / m, liquids 82 kg / m.
    Recognized as an invention according to the results of the examination carried out by the Office for the Invention of Germark: the Democratic Republic
    权利要求:
    Claims (1)
    [1]
    54) METHOD FOR PRODUCING A GRANULATED DETERGENT IN a device with a fluidized bed by spraying liquid detergents on powdered skeletal substances under known conditions with the addition of powdered detergents after mixing them for granulation at 10-100 ° С, characterized in that as one of powdered skeletal substances use sodium tripolyphosphate with a phase content of 90-100% and an apparent density of more than 700 g / l, preferably 900-1000 g / l, with a fine fraction with a grain diameter of less than 0 , 2 mm in the amount of 70-100%, and with stirring and granulation, the gas velocity in the working zone of the inhomogeneous fluidized bed is set between the velocity of the fluidization point of the largest particles and ten times the entrainment rate of medium particles, the gas flow rate being 8002000 kg / m 2 , solids 3001000 kg / m 2 and liquid substances 60 200 kg / m 2 .
    类似技术:
    公开号 | 公开日 | 专利标题
    CA1324745C|1993-11-30|Process for manufacturing particulate detergent composition directly from in situ produced anionic detergent salt
    US3856441A|1974-12-24|Apparatus for pelletizing powdered solid substance in a fluidized bed
    US5308596A|1994-05-03|Process for the production of crystalline sodium disilicate in an externally heated rotary kiln having temperature zones
    US3112274A|1963-11-26|Process for making a bleach composition
    US4427417A|1984-01-24|Process for preparing detergent compositions containing hydrated inorganic salts
    US2768095A|1956-10-23|Process of coating finely divided solid material
    GB1350098A|1974-04-18|Spray drying
    EA002208B1|2002-02-28|Production of detergent granulates
    JPH07100653B2|1995-11-01|Manufacturing method and equipment for effervescent granules and tablets
    SU1081203A1|1984-03-23|Process for producing granulated detergent
    US4968500A|1990-11-06|Continuous method for preparation of granulated sodium perborate
    KR100486408B1|2005-04-29|Method for producing pourable methionine salt based animal food supplement and the granulate thus obtained
    CS245755B2|1986-10-16|Method of continual fluid drying of chemical products
    US4422900A|1983-12-27|Spray drying apparatus for available chlorine-containing compounds
    US20040077518A1|2004-04-22|Granular surfactant and process for producing the same
    US3227790A|1966-01-04|Process for granulation of perborate
    GB1570615A|1980-07-02|Sodium pereborate monohydrate
    JP2008081329A|2008-04-10|Method for manufacturing gypsum dihydrate having large particle size
    US2975142A|1961-03-14|Granular water-soluble perborate-containing salt mixture
    EA001453B1|2001-04-23|Process for the production of a detergent composition
    US3318887A|1967-05-09|Cyanuric acid production
    US3585043A|1971-06-15|Method for preparing a homogenous silage additive
    US3562164A|1971-02-09|Production of free elowing washing powder mixtures
    US4152078A|1979-05-01|Granulating apparatus
    US3328159A|1967-06-27|Production of granular enriched superphosphate
    同族专利:
    公开号 | 公开日
    DD140987A1|1980-04-09|
    DD140987B1|1982-06-30|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    GB8818613D0|1988-08-05|1988-09-07|Paterson Zochonis Uk Ltd|Detergents|
    GB9415904D0|1994-08-05|1994-09-28|Unilever Plc|Process for the production of detergent composition|
    GB9526097D0|1995-12-20|1996-02-21|Unilever Plc|Process|
    GB9712580D0|1997-06-16|1997-08-20|Unilever Plc|Production of detergent granulates|
    GB9712583D0|1997-06-16|1997-08-20|Unilever Plc|Production of detergent granulates|
    EP1187903B1|1999-06-21|2006-03-15|The Procter & Gamble Company|Process for coating detergent granules in a fluidized bed|
    DE10014749B4|2000-03-24|2006-11-09|Thurn-Produkte Adolf Thurn|Process and device for the agglomeration of washing powders|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DD21034079A|DD140987B1|1979-01-05|1979-01-05|CONTINUOUS MANUFACTURING METHOD GRANULATED WASHING AND CLEANING AGENT IN SWIVEL LAYERED APPARATUS|
    [返回顶部]