Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/41—Preparation of salts of carboxylic acids
  • C07C51/412—Preparation of salts of carboxylic acids by conversion of the acids, their salts, esters or anhydrides with the same carboxylic acid part
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/42—Separation; Purification; Stabilisation; Use of additives
  • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation

Definitions

• the present invention relates to a method for the preparation of a new aluminum trilactate powdery product and to the product itself. Further, the invention is directed to product applications in which said aluminum lactate product may be applied.
• a method for the preparation of aluminum trilactate powder is described in an article from 1962 by A. K. Rai, R. K. Mehrotra and R. C. Mehrotra (Journal furdorfen Chemie, 4 (20 ⁇ , pages 105-112 ⁇ .
• This article describes the formation of aluminum trilactate by precipitation due to the reaction of aluminum chloride or aluminum isopropoxide with lactic acid. In both reactions the precipitate is washed with ether and dried at about 60-70 °C/1.0 mm. Hg.
• Japanese patent application 61- 060631 by Sunahara (1986) describes a production method for aluminum trilactate wherein metallic aluminum reacts directly with a lactic acid solution in presence of a catalyst.
• the resulting aqueous solution, sometimes containing partly precipitated aluminum lactate, is optionally further concentrated, filtered and dried.
• Basic aluminum lactate is not aluminum trilactate but comprises aluminum hydroxide lactate compounds as known to the person skilled in the art.
• the basic aluminum lactate in this Japanese patent application is said to have a lactic acid/aluminum oxide molar ratio of 0.5-5 up.
• lactic acid is added until aluminum trilactate is formed by crystallization having a molar ratio of 5.8-6.2 of lactic acid/aluminum oxide.
• Aluminum trilactate corresponds with a molar ratio of 6 when expressed as ratio of lactic acid to aluminum oxide.
• the basic aluminum lactate solution i.e. aluminum hydroxide lactate solution may be spray-dried. It further describes that the resulting aluminium trilactate crystals may be dried using various techniques such as mold drying, fluidized bed drying, drum or conveyor drying etceteras. Spray-drying is not mentioned as possible drying technique.
• aluminum trilactate is a completely different chemical product than aluminum hydroxide lactate.
• Aluminum hydroxide lactate is an amorf product and is for instance at least twice as more soluble than aluminum trilactate.
• Aluminum trilactate is a crystalline product and has therefore the risk of degradation at high temperatures.
• the present invention provides a new method for the preparation of aluminum trilactate.
• the new method has various advantages in comparison to above-mentioned production methods.
• the new production method is very efficient, has a high product yield, has minimal product losses and low production costs and does not generate waste byproducts in contrast to precipitation/crystallization processes. This latter type of process always generates a byproduct in the form of a "mother liquor" comprising non-crystallized product. This mother liquor remains behind after filtration of the crystallized/precipitated product.
• the new production method is not complex and easy to (automatically) control and as a consequence a product of constant and controlled quality is achieved unlike the product that is obtained via crystallization.
• the aluminum trilactate product obtainable via the method according to the present invention can accordingly be controlled with respect to or be provided with a certain particle size, a certain moisture content, and in relation hereto with a certain degree of dustiness, stickiness, flowability and the like, and the product can therefore be made suitable for a specific product application.
• the present invention further provides a new aluminum trilactate powdery product that is easy to handle and transport unlike the present commercially available aluminum trilactate powder.
• Commercially available aluminum trilactate powder is relatively dusty and sticky and the flowability is not satisfactory. These unfavorable powder properties often lead to practical and safety problems in handling and transporting the powdery product. Further, the stickiness of the product results in high product losses and low yields. It further requires intensive, time consuming and costly cleaning of the used equipment and pipelines. These problems are overcome with the product of the present invention.
• the present invention is directed to a method for the preparation of aluminum trilactate comprising a spray drying process wherein a solution comprising aluminum trilactate and/or an aluminum trilactate slurry is atomized and the atomized droplets are contacted with heated gas resulting in the formation of solid aluminum trilactate particles, followed by the separation of the solid particles from the gas.
• the solution or slurry can comprise between 10 to 70 wt% of aluminum trilactate.
• the spray drying process can take place in the various well-known commercially available spray-drying equipment and apparatus in which the heated gas and the aluminum trilactate solution flow co-currently, counter-currently, as a mixed flow in the dryer, etceteras.
• the heated gas for example air at reduced pressure (e.g. vacuum of 0.5 to 5 mbar ⁇ , is used for the evaporation or the drying of the sprayed droplets.
• the drying process may be performed in one stage, meaning in one pass through the dryer, or in multiple stages.
• the nozzles through which the solution is pumped and atomized, may be located at the top, at the bottom or sideways in the dryer. Different types of nozzles are possible. In a preferred embodiment of the present invention, the nozzles are located at the top and the heated air is introduced mainly from above to flow co-currently with the spray of droplets.
• the atomization may be performed by using rotary atomizers, high pressure nozzles or two-fluid nozzles or combinations hereof. It was found that low concentrated aluminum trilactate solutions (including slurry's) are preferably atomized with two-fluid nozzles and the use of compressed air or steam. The concentrations are in the order of 10-25 wt% of aluminum trilactate. Higher concentrated aluminum trilactate slurry's, with concentrations of about 25-70 wt% and in particular 40-55 wt% aluminum trilactate may also be atomized with two-fluid nozzles and the use of compressed air or steam but are preferably atomized by means of high pressure.
• the aluminum trilactate solution or slurry that is used as feed for the spray drying process may be obtained by various means such as for example by means of reaction or crystallization/precipitation .
• the aluminum lactate feed solution is obtained via reaction of an aqueous lactic acid solution with aluminum hydroxide powder in the presence of water in a molar ratio of 3 to 1 (lactic acid : aluminum trihydroxide) .
• the sprayed droplets are falling down while being dried by the heated air.
• the particles may be taken through a second drying stage that may be integrated in the bottom section of the spray tower. Said bottom section then comprises an integrated bed through which heated air flows for further drying of the particles. This drying step may also be performed externally in separate drying equipment.
• the particles are after the first and/or second drying step subsequently further transported via a shaking or vibrating bed. This shaking or vibrating bed serves for further conditioning as e.g. cooling down of the particles.
• the particles then may be taken through a classification system comprising sieves and mills if more fine-tuning of the particle size is required. The fines after milling may be recycled back to the spray section of the spray tower.
• the method yields a product that is free-flowing, not significantly dusty or sticky and which comprises nicely almost round shaped or spherical particles in contrast to the commercially available aluminum trilactate products.
• These latter products comprise particles with many edges looking more like cubical and pyramid shaped blocks or of a form in between. These rod- or cubical-shaped particles are an indication that said particles are made via crystallization processes.
• the nicely spherical-shaped aluminum trilactate particles of the present invention have a much narrower particle size distribution compared to commercially available aluminum trilactate. Particles sizes between 50 and a 1000 micrometer and more in particular between 100 and 500 or even between 100 and 300 micrometer are easy achievable.
• the aluminum trilactate powder of the present invention includes these particles up to a 1000 micrometer in particle size.
• the powder of the present invention has further a very high flowability and is visibly less dusty than commercially available aluminum trilactate powder.
• the powder of the present invention can be controlled to have a Hausner ratio (a well-known parameter to express or indicate the degree of flowability with) of below 1.15. This means that it is easier to transport and to handle and the caking tendency is less than with commercially available aluminum trilactate.
• a Hausner ratio of higher than 1.4 means that the powder is cohesive and thus more difficult or even not suited for proper handling and transport.
• the new product obtained via the method according to the present invention can be provided with a very high dynamic flow rate of 50 ml/s and higher (e.g.
• the aluminum trilactate powder obtained via the present invention was found to be very suitable for various product applications such as cosmetic and personal care applications, dental or oral care applications and technical applications.
• a solution comprising 20 wt% aluminum trilactate by reaction of a solution comprising 88 wt% of lactic acid with -80 wt% dried aluminum hydroxide gel (a white amorphous powder product obtained from Taurus Chemicals®) in the presence of demineralized water.
• the reaction was carried out at an elevated temperature of about 75 to 80 0 C and with a molar ratio of 3 to 1 for lactic acid to aluminum hydroxide.
• the resulting 20wt% solution was fed to a spray-dry tower.
• the solution was fed through two-fluid type nozzles (located at the top of the tower) and atomized by means of application of steam under a pressure of about 8 to 10 bar.
• the spray of droplets was brought in contact with heated air (mainly introduced from above in the spray dry tower) with an inlet temperature of about 235 to 245 0 C.
• the outlet temperature was about 100 to 120 0 C.
• the spray-dried particles were further introduced in a static bed integrated in the lower section of the tower for further drying and were subsequently transported via a shaking bed for cooling down.
• the particles were then taken through a classification system comprising sieves and a mill.
• the degree of flowability of the powder is indicated via the well-known Hausner ratio, which was calculated and measured by measurement of the compressed or tapped bulk density and the untapped (uncompressed) aerated bulk density. The values of the parameters are shown in TABLE I . The experiments were done in duplicate.
• the "Carr class” is a known index or scale (R.I. Carr,
• the flowability can also be expressed by measurement of the dynamic flow rate, which is also a standardized method.
• the dynamic flow rate is measured by measuring the time for 600 ml of powder product to flow through a 2 cm orifice of a tube.
• a dynamic flow rate of or above 50 and preferably of or above 70 or 80 ml/s is acceptable in terms of the powder being suited for the normal handling and transporting activities. The higher the dynamic flow rate, the easier and more efficient, in terms of time and losses of powder that remains behind, the handling and transport of the powder will be.
• the dissolution rate of both powders was measured by measuring the time necessary to dissolve 5 g of aluminum trilactate in 200 ml of Milli-Q water at room temperature.
• the conductivity of the solution was measured in time. When the conductivity is stable, the sample is considered to have dissolved.
• the spray-dried aluminum trilactate powder showed a twofold higher dissolution rate of about 0,25 g/s (or 20 seconds per 5 grams of powder) compared to PURAMEX ⁇ L® with a dissolution rate of about 0.125 g/s (or 40 seconds per 5 grams of powder ⁇ .
• a approximately 53 wt% aluminum lactate-comprising slurry was made by slow and controlled addition of about 16 kg of -80 wt% dried aluminum hydroxide gel ⁇ a white amorphous powder product obtained from Taurus Chemicals®) to about 55.8 kg of lactic acid and about 25.4 kg of demineralized water at an elevated temperature of about 75 to 85 degrees Celsius.
• the aluminum trilactate slurry was kept in a feed tank and was continuously stirred.
• the slurry was fed from the feed tank to a commercially available SLS small-scale pilot spray dryer.
• the slurry was fed through two-fluid type nozzles
• the spray of droplets was brought in contact in co-current flow with heated air with an inlet temperature of about 220 to 230 0 C.
• the outlet temperature was about 120 to 130 0 C.
• the resulting free-flowing aluminum trilactate powder had a moisture content of about 1.1 wt%.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Crystallography & Structural Chemistry (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
• Cosmetics (AREA)
• Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
• Medicinal Preparation (AREA)

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• 2006
  • 2006-12-14 EP EP06126103A patent/EP1932825A1/de not_active Withdrawn
• 2007
  • 2007-12-10 WO PCT/EP2007/063613 patent/WO2008071659A1/en not_active Ceased
  • 2007-12-10 JP JP2009540737A patent/JP5455641B2/ja not_active Expired - Fee Related
  • 2007-12-10 CN CN200780045706.8A patent/CN101610990B/zh not_active Expired - Fee Related
  • 2007-12-10 EP EP07857333A patent/EP2091907A1/de not_active Withdrawn
  • 2007-12-10 BR BRPI0720062-5A patent/BRPI0720062A2/pt not_active Application Discontinuation

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