Preparation of Pharmaceutical or Cosmetic Dispersions

FIG. 1 shows a flow chart for the process according to the invention;

FIG. 2 shows an embodiment of the jet disperser in which the pre-emulsion passes directly from a capillary bore in the sealed end of the feed tube into an outflow tube tightly connected to the feed tube;

FIG. 3 shows an embodiment of the jet disperser in which the pre-emulsion flows through an annular space between a relatively large diameter feed tube and relatively small diameter tubular piece open on one end and having capillary bores opposite one another so that opposed jets of emulsion collide with each other in the tubular piece; and

FIG. 4 shows an embodiment of the jet disperser in which the pre-emulsion flows through opposed jets in a relatively small diameter inner tube into the annular space between a relatively large diameter external tube and the inner tube, and the steams of emulsion issuing from said jets hit the internal wall of the external tube.

According to FIG. 1, the aqueous phase is in a kettle 1 and the oily phase is in a kettle 2. If necessary, the kettle temperatures must be adjusted by heating so that the temperature of the two phases is above the solidification point of any solid constituents present. The two phases are then stirred together in the stirred kettle 3 and pre-emulsified. The pre-emulsion thus prepared is then pumped out of the stirred kettle 3 through the jet disperser 4, in which the homogenisation and fine dispersion characteristic of the end product is effected. Thereafter, the highly concentrated emulsion is adjusted to the desired end concentration by passing the aqueous phase into the storage kettle 5 (Dilution).

The process, which is carried out discontinuously here, can also be carried out by a continuous procedure. In this case, both phases are continuously metered from kettles 1 and 2 into stirred kettle 3, pre-emulsified and then pumped through the jet disperser 4.

In many cases, it is easier to produce a water-in-oil emulsion of high particle fineness than an oil-in-water emulsion. In such cases, the process described above is modified in that phase inversion occurs in the jet disperser 4. The procedure here is to initially introduce the oil phase from kettle 2 into the stirred kettle 3 and then slowly to mix in the aqueous phase. A pre-emulsion in which the oil phase forms the external phase and the aqueous phase forms the internal phase is thereby formed (W/O emulsion). On subsequent dispersion and homogenisation in the jet disperser 4, phase inversion then takes place in a manner such that the external phase becomes the internal phase and the internal phase becomes the external phase. An oil-in-water emulsion (O/W emulsion) is formed. The concentrations of the two phases (proportions), the temperature and the mechanical stress in the jet disperser 4 are decisive for the phase inversion point. The phase inversion point for a given product can be determined empirically, without problems, as a function of the abovementioned process parameters. Furthermore, physical measurement methods, such as, for example, measurement of the electrical conductivity or ultrasonic absorption, can be used to determine the phase inversion point, since these parameters change drastically at the phase inversion point.

Various technical embodiments of the jet disperser 4 are described in the following text. The simplest embodiment of a jet disperser is shown in FIG. 2. It consists of a feed tube 6, the end of which is closed except for a capillary bore 7, and the tube is connected to an outflow tube 8 through this capillary bore. Moreover, the outflow tube 8 is connected tightly to the feed tube 6. The diameter d of the capillary bore is, for example, 0.6 mm, and its length l is 1 mm. Systematic series of experiments have shown that optimum results in respect of particle properties and energy dissipation are obtained if the following dimensions are maintained:

An alternative embodiment of the jet disperser is shown schematically in FIGS. 3 and 4. In this embodiment, a tubular piece 9, open on one side and having a relatively small diameter is inserted in a tube 10, which is also open on one side, having a relatively large diameter. An annular space 11 remains between the internal wall of the external tube 10 and the external wall of the tubular piece 9. In the region of this annular space, the tubular piece 9 is provided with capillary bores 7 opposite one another. As is similarly the case in the embodiment according to FIG. 2, these capillary bores form the only connection between the tubes 10 and 9. According to FIG. 3, the pre-emulsion flows through the tube 10 into the annular space 11, and from there through the capillary bores into the tubular piece 9. Since the jets 7 are opposite one another, the issuing streams of emulsion collide with one another in tube 9. A particularly good dispersion is thereby achieved. The homogenised emulsion leaves the jet disperser through the outflow 12.

The apparatus of the jet disperser according to FIG. 4 is identical to that of the disperser according to FIG. 3. However, from the point of view of flow, it is operated in the reverse direction. In this case, the pre-emulsion is fed through the opening 12 of the inner tube 9 and then flows through the jets 7, which are opposite one another, into the annular space 11 between the internal tube 9 and the external tube 10. The streams of emulsion issuing from the jets 7 hit the internal wall of the tube 10 and flow from there to the drainage opening 13. The internal wall of the tube 10 is thus a baffle for the streams of emulsion. In the embodiment according to FIG. 4, tube 9 is the feed tube and tube 10 is the drainage tube of the jet disperser. In contrast, in the embodiment according to FIG. 3, tube 10 is to be regarded as the feed tube and tube 9 as the drainage tube. The jets or capillary bores 7 are located, uniformly distributed over the circumference, such that their axes intersect at a point on the longitudinal axis of the jet disperser. The above specification applies in respect of their dimensions.

The apparatuses of the jet dispersers described here are of very simple and compact construction and can therefore be produced inexpensively in any workshop. A pressure of the order of magnitude of 10 to 50 bar is required for their operation. This pressure is substantially lower than the pressure required for operating a highpressure homogeniser. For this reason, simple feed pumps, such as, for example, geared pumps or single-stage or multi-stage eccentric screw pumps, are completely adequate. Instead of producing the operating pressure with the aid of pumps, it is also possible to charge the reservoir kettle with compressed gas. For pressures of up to 15 bar, the throughput per individual jet is about 500 liters per hour, and is about 1,000 liters per hour at 60 bar. A further increase in the throughput can be achieved by increasing the number of jets and/or by connecting several jet dispersers in parallel.

The organic phase (oily phase), consisting of: 200-400 kg of emulsifier, such as cetyl-stearyl alcohol and sodium cetyl-stearyl sulphate, and non-ionic emulsifiers, 1,200-1,600 kg of decyl oleate or liquid hydrocarbons, 0.5-2 kg of antioxidants, 50-200 kg of oilsoluble UV filter substance, such as methyl-phenylbenzoxazole, 5-20 kg of anti-foaming agent and 100-200 kg of perfume oil, is initially introduced in a normal stirred kettle 3 at 60.degree. C., and the cold aqueous phase, consisting of: 300-800 kg of water and 100-300 kg of water-soluble UV filter substance, such as Novantisol-sodium, is added. Brief stirring gives an emulsion concentrate of the W/0 type of about 40.degree. C. This is homogenised under a pressure of 10 bar through the jet disperser 4 into the storage tank 5 containing 6,000-8,000 kg of water, 30-100 kg of buffer substance, such as disodium hydrogen phosphate, and 10-30 kg of preservative. Phase inversion takes place in the jet disperser 4. Whilst the mixture is passed in the storage tank 5 , it is stirred. 10,000 kg of finished, liquid suntan emulsion of the O/W type with a very high degree of dispersivity are thus formed.

The organic phase (oily phase), consisting of: 150-300 kg of an emulsifier mixture of polyoxyethylene stearate and sorbitan fatty acid ester, 400-800 kg of cetyl-stearyl alcohol and 600-1,200 kg of octyldodecanol or liquid hydrocarbons, is melted at 70.degree. C. in a normal kettle 2 and the melt is cooled to 40.degree. C.

The oil-soluble active compounds and 20-40 kg of perfume oil are then added.

20-40 kg of a carboxyvinyl polymer are dispersed in 6,000-8,000 kg of water of 45.degree. C. in another kettle 1, and 300-600 kg of 1,2-propylene glycol are added. After the mixture has been brought to 40.degree. C., the water-soluble active compounds are added.

The aqueous phase is then added to the oily phase in stirred kettle 3, and 100-150 kg of 10% strength sodium hydroxide solution are added to neutralise the mixture.

After brief stirring, the still liquid emulsion is homogenised by the jet disperser 4 under a pressure of 10-15 bar. After homogenisation, the cream solidifies in storage tank 5. 10,000 kg of vanishing cream of the 0/W type with a very high degree of dispersivity are thus formed.

The oily phase of: 1,500-3,000 kg of ointment base consisting of mixtures such as: fatty acid esters and fatty alcohol esters (non-ionic) and mineral fats, 50-150 kg of aluminium tristearate, 200-400 kg of octyldodecanol, 50-150 kg of microcrystalline wax and 600-1,000 kg of hydrocarbons is melted in a normal kettle 2 at 80.degree. C. and the melt is cooled to 75.degree. C.

The aqueous phase, consisting of: 4,500-6,000 kg of demineralised water, 25-75 kg of magnesium sulphate, 200-400 kg of glycerol and 10-40 kg of preservative, is prepared in another kettle 1 and brought to 45.degree. C.

The water-soluble active compounds are added to the aqueous phase.

The aqueous phase is then added to the oily phase in the stirred kettle, while stirring. After the crude emulsion has been cooled to 45.degree.-50.degree. C., the oil-soluble active compounds and 40-80 kg of perfume oil are added. A water-in-oil emulsion (W/O emulsion) is thereby formed. After the perfume oil has been incorporated, the still liquid W/O emulsion is homogenised in the jet disperser 4 under a pressure of 10-15 bar and is filled into the storage tank 5, where it solidifies to the finished cream. The W/0 emulsion is thereby retained, that is to say no phase inversion takes place.

The organic phase (oily phase), consisting of: 100-200 kg of octyldodecanol, 10-35 kg of sorbitan fatty acid esters or liquid paraffins, 20-45 kg of wax mixtures, 80-125 kg of cetyl-stearyl alcohol, 5-25 kg of preservative and 5-20 kg of one or more pharmaceutical active compounds (for example azole, imidazole or triazole derivatives), is melted at 50.degree.-75.degree. C. in a stirred melting kettle 3 and the melt is then cooled again to 35.degree.-45.degree. C. The aqueous phase consisting of: 550-750 kg of sterilised water with a temperature of 38.degree.-45.degree. C., is then emulsified into the oily phase (W/O emulsion). Pharmaceutical active compounds, emulsifiers and thickeners may also be added to the aqueous phase. The pre-emulsion thus prepared is then pumped through the jet disperser 4 under an initial pressure of 10-15 bar and with a substance flow of 1,000-2,000 kg per hour, and is thereby homogenised. The initial W/O emulsion is thereby inverted into the desired O/W emulsion (oil-in-water emulsion). The finished ointment can either be directly filled into tubes, or it can first be cooled in a storage tank 5. Alternatively, cooling can also be effected "in line" by means of a heat exchanger between the jet disperser 4 and the storage tank 5.