PROCESSING OF OIL-BEARING SEEDS

The invention relates to treatment of oil-bearing seeds, which already have been first of crushed and of which already not higher oil. Such oil seeds will be called here "obezzhirennymi". Preferable seeds for method of by invention are soya beans, seeds canola (also called rape seeds), sunflower seeds, cotton seeds, sesame seeds and seeds of safflower. Especially preferable obezzhirennymimaslichnymi seeds are cake canola, known as "white flakes". Other preferable type of defatted oil seeds is oil cake from soya beans.

Seeds oil-bearing crops usually contain from about 20 percent of oil to about 40 percent of oil, the percentage of oil varies depending on type of seeds. (All percentages content, given in this description, are weight). Seeds squeezed and degreased by a conventional way, such as extraction with organic solvent followed by removal of solvent. Such known process removes from seeds all oil or its greater part and leaves flakes, known as cake oil-bearing seeds. Optionally, such flakes can be tested (are treated by heating) and produced the product known as cake oil-bearing seeds. Cake and meal are obezzhirennymimaslichnymi seeds, which are in volume of this invention. Cake and meal rich protein. In some oil-bearing seeds, in particular, canola, protein has good balance of indispensable amino acids, low molecular weight and is not strongly allergennym for people or animals. Some defatted oil seeds have also high content of fibers, and easily st their removal varies depending on type of seeds. However such protein and fiber not very are widely used in industry from - the presence of non-food substances in defatted oil-bearing seeds. These substances have phytic acid and phytate (which usually is about 3 percent of cake canola and about 1.7 percent of soya cake), and also (in some oil-bearing seeds) polyphenolic compounds. Presence of such non-food substances reduces value of defatted oil seeds as food additive.

Respectively, preferably have method, which should be treated defatted oil seeds for production of row products of different composition, including product, rich fiber, one or more products, protein-rich, and product, rich sugars.

According to the invention, defatted oil seeds is subjected to a number of successive treatments. For ease of description they will be called phases of i-of IV, should be at least understand, that each phase of optionally immediately followed the previous phase, and that phase II and IV is carried out with different intermediate products, and also, that may be inserted or added other additional treatment, if required. In addition, as discussed below, some phase are optional.

In phase 1 are free from solvent defatted oil seeds suspended in water at pH 3 - 9 with preferable values of pH from 7 to 9. defatted oil seeds stirred thoroughly with water. Temperature of mixing is not critical, but preferably it is ambient temperature or above. Particularly preferably some - or way heated mixture to temperature 50 theoretically - 95°с, so as it solubility of some components defatted oil seeds. Usually heating may be accomplished preliminary heating water with its subsequent to addition of fat maslichnym separated seeds. Mixture is mixed, to provide thorough mixing. Period of mixing is not critical, and suitable are, for example, periods of from 5 minutes to 2 hours. After that suspension is filtered for, to separate larger part of solid substances from liquid STI. Usually this may be done squeezing, for example, in belt filter, and, if necessary, with further additional filtration separated liquid STI for removing as can be more insoluble substances. Filtration gives liquid extract and solid residue (known as "cake is"). And squeezing, and additional filtration can be conducted, if required, on several stages, to improve separation of the liquid and solid phases.

Preferably equipment, used for filtration, transmits small solid particles neobolochechnoi part of seeds ("cell material"), that they ingress of droplets in extract. Such cell material rich protein. However this equipment should not have such large holes, to exclude passage of larger part of shell part of seeds and other rich fibers of solid substances, which are present in the defatted oil-bearing seeds. Construction of the small holes are used usually in additional filters. Filters with holes of 25 micron are, preferably, most small used filters, and filters with holes 2500 micron are, preferably, most large used filters. Especially preferable used filters are those, which have holes from 50 micron to 500 micron. Since defatted oil seeds sometimes contain particles of cell material (pulp), having larger dimensions to about 75 microns, the most preferable range of holes filters is range from 100 microns to 250 microns. Said the most preferred filters should allow such pulp particles pass into the extract. Solid substances, which remained during stage additional filtration, is added to solid substances, remained at the stage of squeezing. In this document together called "filtering lepeshkoi".

Filter cake is usually has about 30 - 50% dry substances, contained in initial defatted oil-bearing seeds, at least this amount may vary depending on type of used oil-bearing seeds and methods, used for separating them from extract. Its dried by usual method, for example, ring drying or by spray drying, to produce dry material, which can be used as feed for ruminant (here called product phase i). Product phase i has to increase the nnoe amount of protein (approximately 20 - 40% protein by dry matter, if initial material are cake canola), and it also contains a large portion of polyphenolic compounds and some amount of phytic acid, contained in initial defatted oil-bearing seeds.

(Mpile) treatment phase of II

Extract after treatment phase i (which preferably contains small particles of pulp seeds) is treated with alkaline substance (that referred here by treatment phase of II), to to brought to pH level above 9. preferable level is pH of 10.5 - 11.5.

Treatment with alkali substance helps solubilise some amount of protein, contained in fragments of pulp (cell material) in extract, extracted in treatment of phase Ic, selected alkaline substance may be substance, which will form insoluble crystals phytate, which easily precipitate. For example, if alkaline substance is calcium oxide (CaO) or hydro ksid calcium (Ca (0n)₂ ) g then fitinovaya acid will react with it, forming calcium phytate, which is insoluble and forms large crystals, easily falling into precipitate from the filtrate at pH higher than about 10, and therefore they can be easily are separated from liquid phase extract provided, that used pH of, at least, 10. Similarly, and other alkaline substance with divalent atoms of metal have tendency form large, easily removable crystalline fitaty at pH above 10, and such alkaline substance can also be used, if this no contraindications (for example, from - behind the, that they poisonous). Hydro ksid sodium is less than preferable as alkali substance from - behind the, that crystals of phytate, which it forms (sodium phytate), have tendency be more than small and less tight, crystals than calcium phytate, and therefore their difficult separate.

Treatment usually starts with addition of CaO or Ca (it)₂ until achieved pH about 11. Regulation of pH of extract usually is carried out at room temperature^ then phytate calcium is precipitated from liquid STI. Optionally, liquid st then is heated to 40 - 60 theoretically and shaken. Treatment with alkali substance (treatment phase of II) can continue at any suitable time, required for deposition of most present phytate. If required epilitiform part fitatov, more present in small particles pulp seeds, may require more prolonged time. Therefore, at least duration of treatment phase II and is not critical, is installed, that period treatment of from 5 minutes to 2 hours is suitable.

Preferable upper limit of pH of in treatment of phase II is a pH of 12. good results can be obtained without using more high pH of, since it was to increase the pH of probability of side reactions, which can damage the protein in treated liquid STI. However higher pH of can be used there, where risk of side reactions is permissible.

Solid substances in extract after establishment of desirable pH of (called here "solid substances phase of II") is separated from remaining liquid STI. For separating solid substances can be used any suitable method, such as filtration or centrifugation. Solid substances of phase II of strongly enriched fitatom. If, that preferably, with alkali substance, used for treatment of phase of II, is CaO or Ca (it) g/phytate is will be the calcium phytate. Solid substances of phase of II are new product, containing at least 5% phytate, preferably at least 10% phytate, with considerable amount of protein and some other material, such as fiber. In case of, when solid substances of II obtained from cake canola, solid substances of phase II of usually have more 10% phytate and about 35 - 50% protein. Solid substances of phase of II can be additionally subjected to reaction, as is represented by below for phase of III, for production of additional products.

Then, that remains after removal of solid substances phase of II, is a alkaline liquid st, here called "liquid styu phase of II".

Phase III is optional process for treatment of solid substances phase of II.

Solid substances of phase of II can be, if required, are introduced into reaction with suitable acid (for example, ns1, to lower pH of to approximately 1 - 5, preferably, to 2 - 4. This will be called here "treatment phase of III" and is optional part of a method. Treatment of acid is used for, to solubilise phytate and phytic acid in solid substances phase of II, produce liquid phase, which contains phytate (liquid st phase of III) and solid phase (solid substances of phase of III). They may be separated any by usual method, such as centrifugation or filtration.

Liquid st phase III can be, optionally, treated with enzyme preparation, containing phytase, before or after separation of liquid STI phase iii and solid substances phase of III. Phytase can hydro lizovat the whole phytate or part of phytate, contained in liquid STI phase of III, to produce inozitola - valuable food product.

After separation from liquid STI phase of III, solid substances of phase of III dried. Solid substances of phase III after the drying contain less than about 50% protein (accurate number of depends on initial defatted oil seeds) and have also a certain number of fibers (whose amount also depends on initial defatted oil seeds). In cake canola protein content usually is in the range 40 - 50%. Solid substances of phase of III are a product of, which can successfully be used in feed for animals or in food products for people. It, optionally, can be combined with .25 protein source (such as, for example, other products, obtained in the course of discussion below phase of IV) for to increase the ny its feed or food value.

(d) treatment phase of IV

Phase of IV represents an optional treatment liquid STI phase of II.

Liquid fraction, obtained in treatment of phase of II, enrich protein and can be treated for extraction of protein. Can be used several optional methods. One suitable method is ultrafiltration, which allows compounds of low molecular weight pass through filter, the passage of the protein. Other suitable method is precipitation of protein. Preferable by method of depositing protein is caused by heating coagulation protein at heating liquid phase to temperature 7 0 - 120 theoretically, preferably to 90 - 110 theoretically, for the time, sufficiently short for, not to destroy proteins (for example, about 6 minutes at 95 theoretically), or isoelectric precipitation at gradual addition of diluted acid to the, until pH of liquid STI approaches the isoelectric point of main proteins in liquid STI, as known in this area for removing protein from solution. If proteins precipitate, more more preferably to use stage of ultrafiltration after deposition of so, so as to remove any more soluble proteins, which do not suffered precipitate.

Precipitated protein then is dehydrated known method (such as filtration or centrifugation) and dried (in ring or spraying drying), to produce new high valuable rich protein concentrate (product 1 phase of IV), which usually contains more than 80% protein, less than 1% phytate and has index of dispersity is less than 5%. As used in this description and in the attached formula of invention, of dispersity index is calculated according to official technique AOSC (the American ECO ChemistsSociety) ba-10 - 65, in revision 1999 g. This method proposes evaluate water-protein in the form of percent of total protein.

Product 1 phase of IV is suitable for use in feed or food products or can combinable with other feed or food products for to increase the ny content protein.

After the, as protein rolled precipitate, rest of liquid st preferably is subjected to ultrafiltration, for example, by means of its passing through membranes molecular sieve. Delayed material (retentate) after such ultrafiltration is a thick liquid st, which can be left in liquid form or any vysushena by usual method for formation of new solid product (product 2 phase of IV). This product also rich protein. Protein content in the product 2 phase of IV varies depending on size used molecular - screening filters and number of passes through such filters and may amounts 50 - 100% protein, but will contain less than 1% phytate and have index of dispersity (as it is defined above) more than 40%. Product 2 phase of IV is suitable for use in feed or food products. It also is suitable for use as ingredient losonov for skin and cosmetic products.

The remaining liquid st (called here product 3 phase of IV) poor protein, but enrich sugars. It is suitable as initial material for ethanol fermentation or can be vysushena any common by methods of extraction of sugars. In especially preferable version, product 3 phase of IV is subjected to nanofiltration, and retantat saved as product 4 phase of IV. Liquid st, which passed through nanofiltration, is a mainly water with some minerals. It may be fused in waste or can be recycle on phase I with addition of vospolnyayushchei water, which is added to fat maslichnym separated seeds in phase I retantat (product 4 phase of IV) contains a large portion of sugars and residual protein, which were in product 3 phase of IV, but is more concentrated and has less than impurities. Product 4 phase of IV can be dried or arris in the form of liquid STI. It is good fermentation medium and can be used as ingredient of feed or food product.

CIRCUIT

Invention will be below additionally described with a reference to the drawings, on which:

Figure 1 - unit - circuit treatment process defatted oil seeds by invention. It corresponds to the, that named in the description by treatment of phase i.

Figure 2 - unit - circuit treatment process liquid STI, obtained in the process by Figure 1. It corresponds to the, that named in the description by treatment phase of II.

Fig. 3 - unit circuit - optional additional treatment process solid product obtained in the process of by Figure 2. It corresponds to the, that named in the description by treatment phase of III.

Figure 4 - unit circuit - optional additional treatment process of liquid product, obtained in the process of by Figure 2. It corresponds to the, that named in the description by treatment of IV phase.

Invention now additionally is described with a reference to the drawings on examples, showing treatment of typical defatted cake canola. The present description relates to preferable in the present time versions of, and are possible modification without output from volume invention.

Turning first to Figure 1, are free from solvent defatted oil seeds 10 mixed with water 11 and, optionally, with recycled water 501 with the last stage of process (Figure 4) in reaction reservoir 14, to produce suspension. Preferably, water is heated before, as added its in reservoir 14. If required, pH of is controlled addition of acid substance (acid 12) or alkali substance (calcium oxide 13) to pH 3 - 8. Suspension is stirred (schematically indicated mixer 15) and, optionally, is heated (schematically indicated heating spiral 16).

After the, as water and oil seeds will be thoroughly intermixed, the obtained suspension then directed along pipeline 111 and is squeezed out on belt filter 17, which shown schematically as having two belts 112 and 113, which move over rolls of 114 and 115, respectively. These tapes are oriented so, that they gradually approach to each other during the suspension from right to left on Figure 1. Extract 116 is separated from suspension and is collected in suitable reservoir 140. Wet filter cake is 120 is pressed out from clearance 121 between belts. Filter cake is 120 may be smeshana with additional water 117 and returned on band filter for additional squeezing (it is shown pointer 130). When committed sufficient pressing out, extract 140 is fed along pipeline 141 in device for mechanical removal of vegetable pulp, shown schematically with position 118. This device has filter 119, on holding solid substances (known as "marc of"). Solid substances after squeezing and additional filtration for removing pulp preferably is directed (as shown pointers 131 and 132, respectively) on dehydration and drying, for example in ring drier 135 for production of solid product 100 (product phase i), which can be used in feed for ruminant. Remaining after removal of pulp extract 150 is collected. If required, additional filtration depulpatsiya can be carried out several times, as shown pointer 122 recirculation, before extract will be is assembled.

Turning now to Figure 2, extract 150 mixed with alkaline substance 20 (for example, with calcium oxide) for achievement of at pH above 9 (preferably, pH of 10.5 - 11.5) and heated in reaction reservoir 21 at stirring (schematically indicated mixer 22) and heating (schematically indicated heating spiral 23). Along pipeline 24 is suitable amount of mixture for placement in the basket 25 or centrifuge 26. Solid and liquid components are separated by centrifugation. Solid substances of 200 (solid substances of phase of II) is extracted. Liquid st 201 (liquid st phase of II) also is extracted.

Turning now to fig. 3, solid substances of 200 mixed with acid 30 and heated in reaction reservoir 31, as schematically shown heating spiral 32. Mixture is mixed, as schematically shown mixer 33. It is possible, is added phytase 34 and mixing is continued. Then mixture is removed along pipeline 35 in centrifuge 36, placing it in basket 37 tsentrifugizatem mixture is centrifuged the, until it does not splits on liquid st 38 and solid substance 39. Solid substances of 39 is withdrawn and, if necessary, dried in ring drier 315 to produce solid product 300, which is used as feed for animals or feed ingredient. Liquid st 38 is along pipeline 310 reservoir 311. If in reaction reservoir 31 1.20 phytase 34, then liquid st will enrich inozitolom. If in reaction reservoir 31 not 1.20 phytase 34, then liquid st will enrich fitatom and may be treated fitazoi by addition of phytase (312) reservoir 311. In any case is obtained product 301, representing the rich inozitolom liquid st. As indicated on circuit diagram, this product is discharged along pipeline 315 in container 316.

Turning now to Figure 4, liquid st 201 is treated for deposition of protein by its heating in reaction reservoir 401 (as schematically shown heater 402) or slow addition of acid 403, results to formation of clotted clot 404 over liquid STI. Then content reservoir 401 filtered or centrifuged, to to isolate svernuvshiisya clot 404, as schematically shown filtering vessel 405;

the svernuvshiisya clot is delayed on filter in the form of solid protein concentrate 406. Solid substances (concentrate) 406 dried, if necessary, as it is shown schematically circular drier 420, product is 4001 (product 1 phase of IV). Liquid st 407, through filter, is subjected to ultrafiltration, indicated schematically on 408, and the retentate 409 from this ultrafiltration is with production of the product 4002 (product 2 phase of IV). Retentate 409 drained as thick liquid st, but, if required, it can be dried in solid product (on circuit is not indicated). Product 4002 rich protein and can be used as feed or food product or as ingredient for cosmetic and therapeutic products. The remaining after ultrafiltration liquid st 410 enrich sugars. Can be extracted directly, as shown is shown 411, in the form of product 4003 (product 3 phase of IV), which (optionally), can be used as fermentation medium. Alternatively, liquid st 410 may be subjected to nanofiltration 412 so, to focus sugar in a retentate 413, which is discharged in collector, to produce product 4004 (product 4 phase of IV), as shown is shown 415.

-filtration is not obligatory, but serves for of preparing product 4004, which is more concentrated, than product 4003, with smaller pollution of minerals (ash). If is nanofiltration, then liquid st 500, passing through filters, includes mainly water and minerals. It may be recycle as part of water, coming into reservoir 14 on Figure 1, or fused in wastes, or its minerals can be extracted.

The invention will be now explained examples, charts showing treatment according to one preferable version of invention for defatted oil cake canola.

Example 1

25 kg treated hexane for extraction of oil white flakes canola obtained from commercial a manufacturer of g. Saskatchewan, Canada. Hexane evaporated at ambient temperature to the moment, when hexane not has encountered detector solvent, to produce purified from solvent white flakes. Purified from solvent white flakes were crushed in ball mill, to destroy large komki and to produce homogeneous cake - initial material for extraction. This material smeshivali with 756 kg of water, which preliminarily was heated UP to 50 theoretically, and added to the to mixture of 1.7 l 10% - hydroxide suspension CaO. Material stirring in belt mixer, until achieve homogeneous consistency. Checked the pH of mixture, which reach 8.0. This material then stirring for 10 minutes in belt mixer.

Then the material ambulances through belt press - continuous-action filter firm Frontier the Technology, Inc. belt press filter - otzhimal material between two polypropylene monovoloknistymi belts, passing above some rolls and gradually near-Earth as moving material through press - filter. Poroznost tape has been such, that propuskala air at a rate of 0.15 m³/ s. Material manually 1.20 in hopper press, to provide uniform flow of material between belts. Material shared on liquid extract (referred here liquid styu phase 1) and the rest of "filtering scone" (called here solid substances phase 1) to complete passage through press - filter. Then liquid st phase 1 ambulances through additional filter with 150 mcm holes. The obtained the following extract, which skipped through a sieve, and residual pulp. This procedure is used for, to remove majority of the particles of husk from extract. Then pulp 1.20 in filtering scone (solid substances of phase 1), and extract, obtained at additional filtration added to to liquid STI phase 1.

On optional stage, solid substances of phase 1 (the filtering scone) additionally treated. These substance smeshivali with water at 50 theoretically in belt mixer, until achieve homogeneous consistency. This material ambulances through belt press - filter, as described earlier, to produce additional extract and filtering scone. Extract ambulances through additional filter, as described above. Added to the pulp to filtering lepeshke, and cleaned from it liquid st added to to liquid STI phase 1.

Filtering scone, obtained at the second pass through belt press - filter, smeshivali with 23 l of water at 50 theoretically in belt mixer, until achieve homogeneous consistency. This material ambulances through belt press - filter, as described above, to produce additional extract and filtering scone. Extract ambulances through additional filter, as described above, and added to the pulp to final filtering lepeshke (solid substances of phase 1). Final filtering scone analyzed protein content and dry substances (results are given in the table 1 below). Extract added to the liquid to STI phase 1.

At least passes through press - filter are preferable, and additional filtration improves separation, the invention allows one-passage, if this preferably, and then result one passage will be product 1. phase described in the table liquid st phase 1 and solid substance phase 1 products are three passages, each, through press - filter and additional filter. Data products used in subsequent examples.

Example 2

Concentration fitatov in solid product (treatment phase of II)

Free from pulp extract from three passes through belt press - filter (liquid st phase 1) reburied in 100 l steam boiler and to extract added to the 1.7 l 10% - hydroxide suspension CaO. During the phase of extraction temperature extract decreased to ambient temperature. Value of pH of extract at ambient temperature after addition of CaO of moisture 11.0. Boiler pairs filed, until temperature of not extract enhanced to 50 theoretically. Extract was at 50 theoretically for 3 - minute period.

Then extract tsentrifugirovali at 5000 g for 2 minutes in basket centrifuge. Separated liquid st decanted and collected (liquid st phase of II). Solid particles from centrifuge resuspended in equal volume of water (at ambient temperature) and again tsentrifugirovali at 5000 g for 2 minutes, washed to soluble material, connected with particles. All particles (solid substances of phase of II) bring together and analyzed the protein content, dry substances and phytic acid. Is installed, that dry substances include 14.9% phytic acid and 45.17% protein.

Example 3

Defitinizatsiya solid product (treatment phase of III)

Solid substances of phase of II, obtained in example 1, kept and freeze to days process of working phase of III. However if required, treatment phase III may be be immediately after phase II of.

Ottaivali 150 g specimen held frozen solid substances phase of II. From this sample otdelyali four 10 g of sample and each smeshivali with 15 ml of water at room temperature. To each sample by drops added to the ns1 the, until pH of does not reduce to 3.5. Then temperature of each sample to differenceto to each of four samples added to the different amount of phytase. Amount of these were, respectively, 25, 15, 10 or 5 FTU (fitaznykh units) phytase Naturphos® (firm BASF). One unit of activity of fitaznoi (1 FTU) is determined as-containing enzyme product, which releases 1 micromole inorganic phosphorus per minute from excess phytate sodium 37 theoretically and pH 5.5. After addition of phytase sample was at 50 theoretically at constant stirring. Through 30 minutes, 60 minutes, 90 minutes and 120 minutes after addition of phytase, from each sample were singled by 5 ml and immediately smeshivali with 15 ml of cooled ice 0, 7on ns1 for inactivation of phytase.

Phytate benefit from each sample shaking for 3 h at room temperature. Then sample tsentrifugirovali at 16000 g for 10 minutes and from each udalyali separated liquid st. To this liquid STI added to 2.5 ml chloroform and tsentrifugirovali for 10 minutes at 10000 g with to produce two layers. Upper layer were singled and 1.20 in device for liquid chromatography careers high-pressure. Phytate content determined by peak area phytate in comparison with standard curve, obtained with known amounts of phytate.

Phytate content determined in sample of solid substances phase of II, which not subjected treatment fitazoi, as described in the given example. Unprocessed solid substances of phase II of have content of phytate 14.90% by dry matter.

Table 1 shows content of phytate non solid substances and in samples, selected at different moments of time after addition of phytase to samplings. Removal of phytate from solid substances depended from amount of enzyme and duration of reaction. When in reaction mixture 25 FTU, phytate not found through 60 minutes after introduction of phytase. At 15 and 10 FTU, for complete removal of phytate needed more long periods of incubation, and at 5 FTU, residual phytate still has encountered in mixture after 120 minutes after introduction of enzyme.

Table 1 Content of phytate in solid product (weight.% by dry matter) without addition of phytase (time 0) and at different duration of incubation with said amounts of phytase

Example 4

Phase Of IV. Extraction of materials rich in proteins Liquid st, separated during centrifugation of extract in example 2 (liquid st phase of II) defended and reburied in 100 l steam boiler. Steam in boiler filed so, that temperature extract observed 95 theoretically. Temperature 95 theoretically was for 5 minutes and then through jacket steam boiler ambulances cold water. Cold water ambulances for 20 minutes. In upper layer extract during this procedure heating and subsequent cooling attributable protein sediment or clot. Then content steam boiler ambulances through nylon rivet sieve with holes 200 micron (sieve Nitex™ firm the Great the Western Manufacturing will the COMPANY, Inc.). Clot is collected sieve, while liquid st passes through a sieve and met in tray.

Clot is then filmed with sieve and reburied in cheese shape width 305 cm, length 457 cm and height 152 cm. Then mold reburied in cheese press and squeezed for 10 minutes under pressure at 34 kPa, with further squeezing for 10 minutes at 69 kPa, and then with squeezing for 10 minutes at 138 kPa, for 10 minutes at 207 kPa, and, finally, with squeezing for 20 minutes at 276 kPa. Liquid st, separated at that, added to the liquid to STI, obtained at initial draining tube through a sieve. The whole liquid st borrowers together (liquid st phase of IV). Completion of squeezing pressure were thrown down and protein precipitate (clot, - product 1 phase of IV) analyzed content of

protein, dry substances and phytate.

Liquid st, remaining after separation of clot (liquid st phase of IV), ambulances through ultrafiltration membrane with threshold cutoff by molecular mass 10000, until volume of retentate was not to about 20 l. Then retentatu added to 20 l of water, and procedure of ultrafiltration repeated. The whole conducted 6 cycles ultrafiltration for concentration of protein in a retentate. Liquid st, through membrane (permeate), collected and bring together. Final retentate investigated on protein, dry substances and phytate (product 2 phase of IV).

If required, ultrafiltratsionnyi permeate may be assembled as product 3 phase of IV. This however was not is made in the given example. Instead, combined ultrafiltratsionnyi ambulances permeate through membrane nanofiltration, until volume of retentate not decreased to 18 l. Retentate (product 4 phase of IV) analyzed protein content, dry substances and phytate. Results are given in table 2 below.

Table 2 shows also in graph " % extraction of" percentage of protein, extracted in different products, from amount of protein, prisutstvovavshego in initial defatted oil-bearing seeds.

Table 2 Content of dry substances, protein and phytate in fractions, in processing white flakes canola (content of phytate and protein is presented in % from dry substance) Fraction % dry matter protein

Index of dispersity protein (as it is defined above) for the product 1 phase of IV reach 3.32, and for product 2 phase of IV 52.46.

Understandable, that predecesser description is described only for coded, and that versions of this method will be evident for specialists, remaining in the same time in volume of the formula of invention.