the instant invention provides methods for selectively removing and recovering oleuropein aglycon from ovw . in one embodiment , the method involves the following steps : obtaining raw ovw comprising oleuropein , oleuropein aglycon , and conversion enzymes ; adding pomace oil to the raw ovw to concentrate oleuropein aglycon in a collection of floating solids ; adding citric acid and heat to form precipitated solids ; adding treated water to raw ovw to form additional precipitated solids and to increase oleuropein aglycon concentration ; adding a solvent mixture ( e . g ., hexane and acetone ) to extract the oleuropeins and further concentrate oleuropein aglycon ; and adding treated water during a final evaporation stage to facilitate oil separation , solvent removal , and further increase the total level of oleuropeins extracted . the resulting ovw can be used for direct irrigation , or further treatment by conventional waste water processes . for purposes of the present invention , the term “ raw ovw ” refers to an aqueous mixture containing a mixture of oleuropein , oleuropein aglycon , and any of the naturally occurring enzymes capable of hydrolyzing oleuropein to oleuropein aglycon ( i . e ., conversion enzymes ). in preferred embodiments , the raw ovw will be the product derived from a water wash of olive vegetation matter as in the manufacture of olive oil . in such embodiments , raw ovw will comprise the water from a washing step as well as endogenous water removed from the olive vegetation matter . the term “ treated water ” refers to raw ovw that has been processed to remove at least a portion of oleuropeins and oleuropein aglycon . preferably , treated water will retain a substantial quantity of conversion enzymes . the term “ floating solids ” refers to an oleuropein aglycon - rich collection of water - immiscible constituents that are less dense than water and tend to form or migrate to the surface of the ovw . the floating solids are often manifested as a foam on the surface of the ovw . the term “ precipitated solids ” refers to water - immiscible constituents that are at least as dense as water . the precipitated solids will commonly comprise oleuropein and various sugars . in at least one embodiment of the present invention , those constituents are removed by filtration or centrifugation . the initial step to recover the polyphenolics , oleuropein aglycon and it &# 39 ; s related compounds is to break the complex emulsion of the water . the initial step is to hold the olive vegetation water for 48 hours upon immediate production as a by - product of the olive oil or to by pass this holding phase and heat the water to 40 ° c . for 30 minutes in a vertical cylindrical steel vessel , preferably by steam . during this heating step the oleuropein is hydrolyzed to the aglycon ( oa ) by natural enzymes present in the olive vegetation water . the oa rises to the surface as a constituent of a water immiscible foam that can be continually removed by surface skimming or other conventional methods . the quantity of oleuropein aglycon can be increased in the floating foam by adding citric acid , olive pomace oil , and heat . preferably , about 0 . 01 % to about 1 . 0 % citric acid is added ; and more preferably , about 0 . 1 % citric acid . unless stated otherwise , all percentages are by weight . the olive pomace oil is preferably added in a quantity of about 2 % about 20 % of the raw ovw ; and more preferably to a volume equal to about 10 % of the volume of raw ovw . heat can also be exploited to increase the quantity of oa in the foam . in preferred embodiments , the temperature is increased to about 100 ° c . for about one hour . lower temperatures can be used for correspondingly longer periods to achieve substantially the same effect . during this heating step , additional solids precipitate and are suspended in the aqueous layer . the precipitated , or suspended , solids are high in oleuropeins , sugars , and other components . although not wishing to be bound by any theory , we believe that the higher level of oleuropeins gained from the addition of the olive pomace oil is due to the drying of the foam as it passes through the hot oil and because the oleuropein aglycon is more oil soluble than the other forms . the floating solids on the top layer of the foam are removed by filtration or skimming , and the precipitated solids in the aqueous bottom layer can be removed by filtration or centrifugation . in a preferred embodiment approximately half of the resulting water is added to a second batch of raw olive vegetation water , and the extraction / treatment described above is repeated . the final water from this second process is cleaner and more environmentally benign , and can be discharged as irrigation water or it can be disposed of by conventional water treatment methods . during this second treatment process , a higher percentage of solids can be recovered thereby increasing the yield since a greater percentage of conversion enzymes accumulate . this process of keeping half of the volume of treated water and adding the other half of the volume from fresh olive vegetation water can be repeated as necessary or until all of the water produced is treated . the recovered solids can be dried , e . g ., by heat or vacuum . in the second phase , the floating solids from the first phase are extracted by a mixture of solvents . preferably , the collected floating solids are first dried before the extraction step is performed . drying can take palce by air drying , under vacuum , with heat , or combinations thereof . suitable solvents are non - polar organic solvents or mixtures of solvents . non - polar organic solvents refers to organic solvents that are substantially immiscible with water , or those that are miscible with other organic solvents that are substantially immiscible with water . exemplary solvents are alkanes ( whether straight chain , branched , or cyclic ), ethers , petroleum ethers , aromatic solvents and substituted aromatic solvents ( e . g ., benzene , toluene , xylene ), polyols , and the like . preferred solvents include pentane , hexane , heptane , acetone , ethyl acetate , diethyl ether , dimethyl furan , and mixtures thereof . it is further preferred that the solvent or solvent mixture has a boiling point lower than that of water ( i . e ., & lt ; 100 ° c .). especially preferred solvents include a mixture of hexane and acetone . preferably , the hexane / acetone mixture is from about 40 / 60 (% by volume ) to about 60 / 40 ; and more preferably about 50 / 50 . in preferred embodiments , there are two additional steps in the extraction process . first , the non - polar solvent or solvent mixture is contacted with the recovered solids . the vertical cylindrical steel vessel , used as the heating equipment in the first step , can be used in this step . in a preferred embodiment , the solvent is pumped into a tank , pumped out of the bottom , and then re - circulated through the top until the desired concentration of oleuropein to oleuropein aglycon is obtained . preferably , the volume of solvent used is about one to three liters of solvent per kilogram solids , and more preferably , about two to one ( l / kg ). in a second step , the solvent is removed . solvent removal can be performed under vacuum , heat , or a combination thereof . preferably , solvent removal is performed by transferring the oleuropein aglycon product of the above extraction step to a second vessel . the second vessel is preferably a stainless evaporation / vacuum vessel , but can be any vessel suitable for removing solvent from a mixture or solution . generally , the solvent vapors coming off the mixture are routed through a loop and are cooled by water or an air cooler such that the condensed vapors are collected in a storage or collection vessel remotely from the oleuropein aglycon - rich mixture . this step of solvent removal is continued until the volume in the evaporation vessel is about one tenth the original volume . at this time , previously treated water is added to the vessel as necessary to precipitate oil and facilitate the total removal of solvent . the vessel is reheated to boiling with the solvent traveling through the same condenser loop to the solvent storage until the vapor temperature exceeds the boiling point of the solvent . the condensate is then directed back to the holding tank for the raw treatment of water until the consistency of the residue in the evaporation tank is a slurry or a pumpable mud . the slurry residue , which does not contain any solvent , is then pumped into pans for drying by the same means as in the first stage . the resulting product is about 40 % oleuropein aglycon as determined by hplc . remaining solids are natural olive solids . the other remaining end products also have potential uses . for example , the solid residue from the extraction step is high in sugar and is a suitable supplement for animal feed or alcohol fermentation . ( see fig . ii : olive water treatment - phase ii ; and fig . iii : phase ii )
the present invention provides economical methods for collecting oleuropein aglycon from olive vegetation water , a routine byproduct in the manufacture of olive oil . the methods have the advantage of facilitating the collection of other valuable constituents of olive vegetation water , and furthermore render the olive vegetation water environmentally benign , and thus suitable for routine disposal .