the inventive device is explained more detailed in the following by five examples . the embodiment of the device as whole marked with 1 that is shown in the only figure of the drawing has a first chamber 2 , a second chamber 3 as well as a further chamber 4 , whereby an endless conveyor belt 5 is extended from the entrance 6 of the first chamber 2 to the exit 7 of the further chamber 4 . each chamber 2 , 3 and 4 is connected with an outlet 8 , 9 , respectively 10 , whereby the outlets 8 - 10 lead into corresponding tanks that are not shown . the endless conveyor belt 5 is charged with a separation phase 11 at the entrance 6 of the first chamber 2 over an application device that is not shown , whereby the application device not shown is constructed that way that the separation phase 11 is applied in its dry form on the conveyor belt 5 . hereby the layer thickness and the bulk density of the separation phase 11 are adjustable . in the first chamber 2 the solution , dispersion and / or emulsion of the mixture to be separated is sprayed onto the separation phase 11 by corresponding dosing nozzles 13 , whereby the separation phase 11 is transported by the conveyor belt 5 in the sense of direction of the arrow 12 . the dosing nozzles 13 extend across the whole breadth of the separation phase 11 . since the first chamber 2 is set under a vacuum by the outlet 8 , a part of the fluid used for the manufacturing of the solution , dispersion and / or emulsion of the mixture to be separated evaporates . after the transport of the separation phase now charged with the mixture into the second chamber 3 , a suitable eluent is added to the separation phase . herefore chamber 3 has three exemplarily shown nozzle devices 14 that extend diagonally to the transport direction the separation phase 11 and that cause an elution of a single component or a fraction of the mixture . hereby the component found in the eluent , respectively the fraction of the mixture found in the eluent are obtained at the outlet 9 , whereby the component , respectively the fraction can be stored temporarily and correspondingly recovered in the tank not shown . in the further chamber 4 formed as a drying chamber according to the shown embodiment the separation phase 11 is set under a vacuum and heated up which leads to the fact that all the residues of the eluent are removed . at the outlet 7 a separation phase 11 emerges that is still charged with the components , respectively the fractions according to the shown embodiment and that is not meant to be isolated . for that reason this residually charged separation phase can be either regenerated or wasted . however , if also the isolation of these residual components of the mixture is desired , it is only necessary to provide a corresponding number of chambers being formed like the second chamber 3 and being arranged between the second chamber 3 and the further chambers 4 . a solution of the mixture a of 50 % by weight in ethanol was treated in the above described device . hereby aluminium oxide was used as separation phase in a layer thickness of 8 cm , whereby the conveyor belt having a breadth of 1 m was transported with a speed of 10 m / h through the chambers 2 to 4 . in the first chamber 2 700 kg of the solution of the mixture a of 50 % by weight in ethanol / h were sprayed by nozzles onto the separation phase . in the second chamber 3 700 kg ethanol / h were sprayed by nozzles onto the separation phase charged with the mixture a . the eluate hereby emerged and drawn off over the outlet 9 contained a mixture b , whereby the composition of the mixtures a and b is indicated below . the comparison of the above indicated compositions of the mixtures a and b shows clearly that the concentration of unwanted phosphatidic acid was drastically reduced during the treatment . after the elution of the separation phase this separation phase moistened with ethanol was heated up to a temperature of 80 ° c . in the drying chamber 4 under a vacuum . that led to the fact that the ethanol was completely vaporized and that a dry separation phase emerged which was correspondingly wasted . a solution of the mixture c of 20 % by weight in ethanol was treated in the above described device . hereby aluminium oxide was used as separation phase in a layer thickness of 8 cm , whereby the conveyor belt having a breadth of 1 m was transported with a speed of 10 m / h through the chambers 2 to 4 . in the first chamber 2 2250 kg of the solution of the mixture a of 20 % by weight in ethanol / h were sprayed by nozzles onto the separation phase and continuously drawn off . in the second chamber 3 1000 kg of ethanol / h were flushed onto the separation phase charged with the mixture c . the eluate hereby emerged and drawn off over the outlets 8 and 9 contained a mixture d , whereby the composition of the mixtures c and d is indicated below . the comparison of the above indicated compositions of the mixtures c and d shows clearly that the accompanying phospholipides as phosphatidylethanolamine , phosphatidylinositol and phosphatidic acid were removed during the treatment . after the elution of the separation phase this separation phase moistened with ethanol was heated up to a temperature of 80 ° c . in the drying chamber 4 under a vacuum . that led to the fact that the ethanol was completely vaporized out of the separation phase and that a dry separation phase emerged which was correspondingly wasted . a solution of the mixture e of 8 % by weight in ethanol was treated in the above described device . hereby aluminium oxide was used as separation phase in a layer thickness of 8 cm , whereby the conveyor belt having a breadth of 1 m was transported with a speed of 10 m / h through the chambers 2 to 4 . in the first chamber 2 3600 kg of the solution of the mixture e of 8 % by weight in ethanol / h were sprayed by nozzles onto the separation phase . in the second chamber 3 1000 kg of ethanol / h were flushed onto the separation phase charged with the mixture e . the eluate hereby emerged and drawn off over the outlet 9 contained a mixture f , whereby the composition of the mixtures e and f is indicated below . the comparison of the above indicated compositions of the mixtures e and f clearly shows that the concentration of phosphatidylcholine was essentially increased during the treatment . after the elution of the separation phase this separation phase moistened with ethanol was heated up to a temperature of 80 ° c . in the drying chamber 4 under a vacuum . that led to the fact that the ethanol was completely vaporized out of the separation phase and that a dry separation phase emerged which was correspondingly wasted . a solution of the mixture g of 50 % by weight in ethanol was treated on the above described device . hereby silicon dioxide was used as separation phase in a layer thickness of 12 . 5 cm , whereby the conveyor belt having a breadth of 1 m was transported with a speed of 10 m / h through the chambers 2 to 4 . in the first chamber 2 3000 kg of the solution of the mixture g of 30 % by weight in ethanol / h were sprayed by nozzles onto the separation phase . in the second chamber 3 2000 kg of ethanol / h were sprayed by nozzles onto the separation phase charged with the mixture g . in the third chamber 4 the separation phase charged with the mixture was eluted with 7000 kg of ethanol . the eluate hereby emerged and drawn off over the outlet 10 contained a mixture h , whereby the composition of the mixtures g and h are indicated below . the comparison of the above indicated compositions of the mixtures g and h clearly shows that the concentration of the phosphatidylcholine was essentially increased during the treatment . after the elution of the separation phase this separation phase moistened with ethanol was heated up to a temperature of 80 ° c . in the drying chamber 4 under a vacuum . that led to the fact that the ethanol was completely vaporized out of the separation phase and that a dry separation phase emerged which was correspondingly wasted . the separation phase can be used again when it is moistened with ethanol . a solution of a dried extract of 70 % by weight obtained by the extraction of yew needles with methanol was manufactured in butyl acetate and treated in the above described device . hereby silica gel ( compalox ) was used as separation phase in a layer thickness of 10 cm on the conveyor belt , whereby the conveyor belt having a breadth of 1 m was transported with a speed of 5 m / h through the chambers 2 to 4 . in the first chamber 2 100 kg of the above described solution of 70 % by weight in butyl acetate / h was sprayed by nozzles onto the separation phase . in the second chamber 3 300 kg of the ethanol / h was sprayed by nozzles onto the separation phase charged with the mixture . the eluate hereby emerged and drawn off over the outlet 9 was wasted . in the third chamber 4 the separation phase charged with the mixture was eluted with a solvent mixture ( methanol : acetone : acetic ester ; v : v : v ; 70 %: 15 %: 15 %) at a temperature of 30 ° c .± 5 ° c ., whereby this solvent mixture had a flow rate of 500 kg / h . the eluate hereby emerged and drawn out of the chamber 4 over the outlet 10 mainly consisted of 10 - deacetylbaccatin iii ( 10 - dab ) next to the above indicated solvent mixture , whereby the 10 - deacetylbaccatin iii ( 10 - dab ) had a degree of purity of 97 % by weight . according to embodiment 5 the initial solution of the extract of 70 % by weight that was applied in the first chamber and that is meant to be separated had a maximum of between 4 % by weight and 5 % by weight of 10 - deacetylbaccatin iii ( 10 - dab ).