in accordance with one aspect of the present invention , a process is provided for eliminating the beany flavor from soybeans in the production of products , such as soymilk and okara which avoids the disadvantages of conventional process , which include thermal and / or chemical processing stages . in accordance with another aspect of the present invention , a process is provided for the extraction of oils from seeds , preferably edible oils . the present invention is also based in part on the discovery that beany flavors and odors from soybean may be eliminated during the production of soy products , such a soymilk and okara . the present invention is based in part on the discovery that seed oils may be produced without off - flavors in the same manner . in more detail , the present invention provides a process for producing soymilk and / or okara which entails first subjecting whole soybeans to a cooled , pressured carbon dioxide in which the soaking water is deaerated . that is , a deaerated water is used for soaking the whole soybeans and sublimated carbon dioxide is sparged into the deaerated water . then , the soaking soybeans are subjected to grinding with deaerated water through which a stream of sublimated carbon dioxide bubbles pass to thereby eliminate a bad or beany flavor , and the ground beans , as slurry , are filtered . then , the filtered slurry is purified using carbon dioxide under the same conditions as in the grinding ( or second ) stage - except that a lower minimum flux ratio may be used - in order to eliminate any remaining bad flavors and odors from the raw soymilk base , which is then cooked . the soymilk produced by the present invention has no beany flavor , no bitter taste and no chalkiness . further , the present process , being non - thermal , does not destroy essential amino acids . additionally , the soymilk produced is white due to reduce chemical browning , and moreover , has a similar flavor to dairy milk and is highly stable . the okara produced has minimal if any , bad odors and , moreover , a high fat content as all process stages of soaking , grinding and purifying are carried out at low temperature . the present invention actually realizes two main objectives : first , the attainment of both high protein yields and virtually no beany flavor and odor . second , these objects are realized in a manner such that the obtained products are both economically feasible and environmentally safe . the process of the present invention employs the use of whole soybeans , and does not require the use de - hulled soybeans . this is important because broken soybeans , even though the soybean coating remains intact , can produce undesirable substances at low levels of humidity and temperature , such as ketones , aldehydes , etc ., which affect the organoleptic qualities of the end - product ( see u . s . pat . no . 4 , 409 , 256 .). in the present process , the whole soybeans are soaked in deaerated water with sublimated carbon dioxide being sparged into the water . this may be achieved by a gas conduit having an effluent part or opening below the surface of the deaerated water in a soaking container . generally , it is most preferred to use a carbon dioxide pressure of about 1 – 5 bar absolute and a soaking water temperature of about 4 ° c . the soaking under these conditions may either be a “ static ” soaking — with no movement in the tank or chamber for soaking — or a “ dynamic ” soaking — using an agitation . the agitation may be provided by any stirring device . the soaking stage is effected either continuously or by batch , that preferably batchwise . further , a membrane contactor may be used to enhance the carborating efficiency in the soaking stage . while a carbon dioxide pressure of 1 – 4 bar absolute is used , it is preferably that about 2 . 5 to 5 bar be used , and most preferably about 3 – 4 . 5 bar absolute . generally , the ph of the deaerated water in the soaking stage is in the range of from less than 5 . 8 to greater than 4 . 6 . however , the soybean - deaerated water - carbon dioxide system should never reach a ph of 4 . 2 – 4 . 6 , which is the isoeletric region for soybean proteins . thus , preferably the ph should be from about 4 . 7 or 4 . 8 to about 5 . 8 , i . e . higher than the isoelectric region for soybean proteins . as noted above , carbon dioxide has been found to be effective in extracting beany flavors and odors from soybeans . additionally , the used of carbon dioxide provides a mildly acid medium which does not leave remaining substances , such as organic ( other than carbonic acid ) and / or inorganic acids in the medium . thus , products and by - products of the present invention are chemical - free , i . e . free of chemical additives . thus , as used herein the term “ chemical free ” means free of — or containing no chemical additives or chemical processing aids , such as sodium bicarbonate . then , the soybeans are washed with ordinary tap water and soaked with deaerated water for about 6 to 18 hours , preferably about 8 to 14 hours , and most preferably about 12 hours at about 1 – 5 bar absolute of pressure and about 0 to 10 ° c ., and preferably about 2 to 8 ° c ., most preferably about 4 ° c ., using an atmosphere of carbon dioxide . preferably , about 2 . 5 to 5 bar , and most preferably 3 – 4 bar absolute of pressure in used . importantly , the present invention has been based , in part , up on the discovery that carbon dioxide contributes to the dissolution of proteolytic enzymes due to the soaking acid medium , which causes the breaking of proteins in the soaked soybean , and moreover retards non - desirable enzymatic processes . as used herein , the term “ deaerated ” means water which has the dissolved air including oxygen removed therefrom . for purposes of the present invention , any conventional methodology may be used to prepare deaerated water . for example , deaerated water may be industrially produced by the use of scrubbing deaeration systems , vacuum deaeration systems and even a vacuum filtration or inert gas methodologies in the laboratory . see dissolution technologies , “ comparison of the effectiveness of various deaeration techniques ”, degenhardt , o . et al ., february 2004 . according to this article , a helium gas sparge methodology affords , perhaps , the best results . see also usp ( 2002 ). generally , it is preferred that the deaerated water used have a dissolved oxygen content of less than 10 ppm , preferably less than 5 ppm . the carbon dioxide is then bubble through in the soaking step into the deaerated water . this sublimated gas will have a temperature of about − 78 ° c ., and will be at an extra - atmospheric pressure of up to about 10 bar absolute pressure . a carbon dioxide loop cycle which is typically used in the present invention is depicted in fig1 . fig1 depicts a suitable co 2 loop cycle which may be used in the present invention . the overall loop cycle entails the inclusion of the components shown in fluid and operable connection are : strangulation values ( k - 222 , k - 223 , and k - 224 ), pressurized storage tanks ( f - 210 , f - 220 , f - 230 , and f - 240 ), pressurized soaking vessel ( d - 110 ), extracting and wet grinding vessel ( d - 120 ), purification tower ( d - 130 ), recycle storage tank ( f - 250 ), separator co 2 - water ( h - 251 ), compressor ( g - 252 ), cooler ( e - 253 ), activated carbon and molecular sieve filters ( h - 255 a / b ), and refrigeration system ( p - 254 ). the following is a more detailed description of a soymilk processing plant with a production of 10 , 000 liters of soymilk per 8 - hour day , equivalent to 1 , 250 liters per hour or a mass flow of 1 , 269 kg of soymilk per hour ( density = 1 . 015 grams per milliliter ). the required soy bean mass flow is 292 kg of soy beans per hour ( at 13 % humidity and 65 % process yield ). water requirement for producing soymilk is 1 , 698 kg / hour ( including process yield ). during the static soaking stage consumption of deaerated water is 1 , 750 kg / hour , in which the replaced soaking water is equal to the water absorbed during soaking , equivalent to 277 kg / hour . during an 8 - hour soaking period the batch volume is 14 m 3 . carbon dioxide consumption during soaking is 108 kg per batch ( at a pressure of 4 atmospheres , 4 ° c . solubility is 0 . 263 mole co 2 per liters of water ). carbon dioxide consumption during the grinding stage is 267 kg / hour and co 2 consumption during purification is 73 . 88 kg / hour . 4 , 253 kg of co 2 are required for one and a half days ( 12 hours ) of production . for a total mass flow co 2 of 354 kg / hour a 25 hp compressor working within a range of 1 to 18 atmospheres in a loop cycle is required . the compressed co 2 reaches a temperature of 110 ° c ., which needs to be cooled down to 20 ° c . using a cooler , with a heat elimination of 29 , 800 kj / hour . in order to be liquidized the co 2 should be cooled to a temperature of − 37 ° c . if the pressure is at 10 atmospheres the heat elimination will be 57 , 420 kj / hour . heat elimination from the soaking water is 81 , 200 kj / hour to reach a temperature of 4 ° c . in the main storage tank ( f - 210 ) the co 2 is in a liquid state of 4 , 253 kg . the tank is connected to three secondary storage tanks ( f - 220 , f - 230 , and f - 240 ) by stainless steel aisi 304 ( food grade ) piping . the conditions of the co 2 in the main tank and secondary tanks are approximately the same (− 37 ° c . and 10 atmospheres ). the flow of the liquid co 2 from the main tank to the secondary tanks is carried out by stainless steel pumps . the co 2 is then set and distributed from the secondary tanks to where it is required in other stages . the whole soybeans are introduced using any type of conveyor , which could be from the silo using a worm ( screw conveyor ) to the soaking vessel ( d - 110 ), in which the beans are washed with tap water using an agitation system that can be a mechanical agitator from which air has been extracted using a normal vacuum system . the f - 220 tank feeds the soaking recipient , reaching an internal pressure of 4 atmospheres . soaking time is 8 hours . then the soaking tank is depressurized and all the co 2 is sent to the recycling storage tank ( f - 250 ) and the soaked soybeans are then washed again . all the liquid co 2 storage tanks are thermically insulated with commercial units that use polyurethane or vacuum system . from the f - 230 tank the liquid co 2 is transferred to the grinding container and extracted by a pump with a mass flow of 267 kg / hour that produces a change of state from 10 atmospheres at − 37 ° c . to & gt ; 1 atmosphere at approximately − 78 ° c . using a distributor which changes the isenthalpic state . the co 2 is bubbled by the distributor under a slightly greater pressure in order to ensure mass transfer and an adequate residence time while the soaked soybeans and the grinding water are fed continuously within the container where the soybeans are ground using some type of mechanical device and the used co 2 is also extracted continuously through the top of the vessel , whereby the beany soy odors are extracted from the slurry being grounded ( soybean , co 2 and water ). during the grinding stage the co 2 in the stage of sublimation is bubbled and mixed with the ground slurry ( water and soybean ), in which the co 2 absorbs the medium &# 39 ; s ( no phase change ) heat as it passes to the gas state . this results in internal cooling down to 4 ° c . and so external refrigeration is not necessary . the co 2 gas also contains traces if water and is stored or enters the recycling storage tank where it is fed to the compressor ( g - 252 ) after the water from this flow has been extracted using a separator ( h - 251 ). during food - grade stainless steel reciprocating pump with a volumetric flow or capacity of 1 , 250 liters per hour ( 21 liters per minute ), whose pumping discharge pressure should be such as to ensure the separation of the okara from the raw soymilk extract though filtering using a rotary vacuum filter . a pump is used to feed the extract from the purification tower ( d - 130 ) with a mass flow of 1 . 269 kg / hour . the tower has a distributor through which the co 2 is fed in the sublimation state in the same way as in the grinding stage with a mass flow of 73 . 88 kg / hour . internally , the tower can use various types of packing such as rasching ring , slotted ring , and cross partition rings or perforated plates to significantly increase the transfer of the mass . in this way the last traces of unwanted substances in the raw soymilk are eliminated . the purification tower works continuously in which the temperature should be 4 ° c . with an internal pressure of 1 atmosphere ( the container is thermically insulated and has a refrigerated system that keeps temperatures at 4 ° c .). the used co 2 leaves through the head / top of the tower and goes to the recycling storage tank from where it goes on to the closed cycle . the purified extract leaves from the bottom of the tower and is pumped to cooking tank in which the soy &# 39 ; s non - nutritional substances are destroyed . the cooking tank has an agitation system and a heating system usually using a steam jacket . the soymilk is then pasteurized and sterilized using any of the commercial means available such as plate pasteurizer and / or uht sterilizer . all the water used in the process can be recycled by installing a water treatment plant for this purpose , depending on budgetary considerations . it should be noted that the plant &# 39 ; s final design will depend mainly on the process &# 39 ; s economic factors , such as co 2 and electricity consumption for liquefying refrigeration , etc . the co 2 atmosphere should produce a ph of less than about 6 . 5 preferably less than about 6 . 0 , and most preferably about 5 . 8 within the soaking chamber and medium , which is deaerated water . it is known that the solubility of soybean proteins in water is strongly affected by ph . close to 80 % of the protein in raw seeds or unheated meal can be extracted at neutral or alkaline ph ( see berk ; zeki . technology of production no . 97 , 1992 . p . 8 ). however , the present process uses a weak acid medium without the risk that soybean - water — co 2 system will ever reach a ph 4 . 2 to 4 . 6 where the isoelectric region resides and where protein precipitation is imminent . after the soaking stage of the present process , the swelled soybeans weigh about twice their original weight . they are washed again with ordinary water to eliminate oligosaccharides , and ripening enzymes . it is believed that the use of carbon dioxide helps to dissolved oligosaccharides in the aqueous soaking medium . oligosaccharides are part of the soybean carbohydrates . according to the conventional wisdom , oligosaccharides are not broken down by the enzymes of the digestive tract but are fermented by microorganisms present in the intestine with the formation of intestinal gas , i . e . flatulence , an inconvenience associated with the ingestion of beans in general . this is a factor which the present invention takes into account ( berk ; zeki . technology of production of edible fours and protein products from soybeans , fao agricultural service bulletin no . 97 , 1992 . p . 12 ). the wet soybeans and the deaerated water are fed into a carbon dioxide atmospheric grinding stage . the saturated carbon dioxide is bubbled in a sublimated ( solid ) state at a temperature of − 78 ° c ., while the water - soybean system is at about atmospheric pressure , a temperature of preferably 4 ° c ., and ph is 5 . 8 . in the grinding stage , a minimum flux ratio of 0 . 15 ( co 2 gas / grinding liquid ratio ) is used . in this invention , it has been surprisingly discovered that saturated carbon dioxide in the above - mentioned sublimated state easily extracts undesirable substances such as beany flavor , odor and enzymes from the slurry without adversely affecting other organoleptic qualities thereof . in a following stage , the slurry is filtered and raw okara and soymilk are obtained . both intermediate products present a minimal bad odor and whitefish color . it should be noted that chemical browning is indicative of protein and amino acid destruction ( u . s . pat . no . 4 , 409 , 256 ). in accordance with the present invention it is believed that some enzymes from soybean catalyze chemical browning , which can be minimized by soaking and the above - mentioned extraction stage , thus the soaking stage is as important as the extraction stages in the present invention . the soymilk produced by the present process does not present a chalky mouthfeel due to oligosaccharides . other insoluble substances such as protein of high molecular weight and cellulose are easily separated by both soaking and filtration and as a result all fiber is eliminated from the raw soymilk . two consequences of soybean processing at a low temperature may be noted . first , okara yields a high level of lipids ( 87 . 19 %) of the whole soybean or a content of 18 % of its total solids , while total soymilk solids contain just 1 . 33 % of lipids . thus , this product can be called de - fated soymilk or light soymilk . additionally , light soy oil can be extracted from okara , thus the present invention increases the raw soybean resource with little waste . it should be noted that the ash yield regarding the total soybean solids is only 16 %, which is a favorable factor in obtaining soy oil accordingly to u . s . pat . no . 5 , 278 , 325 . secondly , raw soymilk extract yields a high level of protein of at least 75 % of the whole soybean ( less water ). further , because these stages are carried out at low temperatures there is no denaturation of proteins caused by heating . the raw soymilk extract is then purified to ensure the quality of the end product using the same conditions of saturated carbon dioxide which is bubbled in a sublimated state at a temperature of − 78 ° c . at atmospheric pressure inside the purification tower at most preferably 4 ° c . and a ph of 5 . 8 . the flux ratio is lower than in the grinding stage because most of the undesirable substances have already been eliminated . in the purification stage the minimum flux ratio is 0 . 043 ( co 2 gas / raw soymilk liquid ratio ). the raw soymilk is then cooked for about 15 to 60 , preferably about 30 minutes , at atmospheric pressure to eliminate anti - nutritional factors , such as trypsin inhibitor substances , and to lightly deodorize the remaining bad odors , after which it passes through a pasteurization or sterilization stage and is then cooled to about 2 to 8 ° c ., preferably about 4 ° c ., ready for packing . this process does not require vacuum deodorization and homogenization . in industrial use of the present invention , the carbon dioxide can be recycled but beforehand it should be purified using an activated carbon filter and a molecular sieve to eliminate undesirable substances . the co 2 is then fed back to be used again for the next soaking , grinding and purification stages , known as a loop cycle . moreover , the co 2 loop cycle operates under soft conditions such as a maximum pressure of 10 bar absolute and a minimum temperature of − 78 ° c . okara can be dried using any suitable chemical engineering method for subsequent processing . further , the present process can be conducted either batch wise or continuously . the soymilk has a yield of at least 73 . 14 % of the usable soybean ( less fiber and water ) or 65 % of the whole soybean ( less water ). the soymilk can be used to make excellent soy - products such as yogurt , ice cream , tofu , etc . it may also be used as an intermediate product to produce protein concentrates . further , product work - up is now described . depending on the condition of the invention &# 39 ; s process pure soy extract or soymilk can be obtained . the soy milk or a protein extract obtained from the invention &# 39 ; s process ( the raw material ) passes through an acidification stage in the iso - electric region in which the protein precipitation is produced as in cheese making . in the so - called acid wash any food grade acid , such as citric acid , can be used . it is also believed that the co 2 can be used in a sublimation state , preferably in similar condition with the help of latest - generation contactors . all this leads to ph in the iso - electric region ( 4 . 2 – 4 . 6 ) where precipitation is imminent . thus two products are obtained : ( 1 ) precipitated protein in higher concentration known as soy curd and ( 2 ) soy whey that contains carbohydrates and slats in greater quantities . separating these two flows / fluids are carried out by centrifugation or filtration , whichever is most suitable . the curd then goes through a de - acidification stage in which the suspension is recovered by ph variation . this is relatively easy as a neutralization agent ( alkali ) is not needed in order to go back to the initial ph given that if one works with co 2 acidity is simply eliminated by de - pressurization and / or vacuum in which the extracted co 2 gas can go to a recycle tank . then , after being purified with an activated carbon filter , it is fed back into the new acid washing stage . the stable suspension of protein should have a solid concentration of at least 30 %. after this stage the suspension again goes through a centrifugation stage in which the extract is concentrated to 75 % protein . finally , the protein extract is dried by spray drying to obtain protein powder with a maximum humidity of 8 % so as not to undergo deterioration during storage . some stages of this process can be adapted or developed to improve other already known processes such as soy oil processing . these adaptations can replace the balancing stage or stages ( using sodium bicarbonate or other chemicals ) with other extraction stage that use carbon dioxide , which have advantages such as , minimizing bad odors and flavors , and improved yields . additionally , as noted above , the present invention may be used to produce seed oil . any seeds , particularly edible seeds or nuts , such as sunflower seeds , walnuts , peanuts , pecans , may be used to produce oils having reduced or eliminated off - flavors . generally , the apparatus of the present invention may be used to produce the seed oils , and the released oils may be separated by extraction from the aqueous medium by a suitable solvent such as hexane , with the solvent being removed by subsequent distillation and vacuum treatment if desired . the present process overcomes the principal above - mentioned problems found in traditional soymilk , and some modern commercial soymilks such as beany odor and flavor , chalky mouthfeel , chemical browning , instability , low protein yields , flatulence , and the soymilk is chemical free . moreover , the soymilk produced by the present invention has a similar appearance to dairy soymilk . the present process or part of it may be used to produce protein concentrates . further , some stages of this process may be used to improve known processes already known such as soy oil process , protein isolates , etc . the object is the extraction or elimination of lypoxygenase and other enzymes which cause bad taste flavors from the soybean by sublimated carbon dioxide . these enzymes in the bean cause a bitter , chalky flavor in the end product . use of carbon dioxide also eliminates chemical browning substances , which are both volatile and non - volatile substances . ( 4 ) as these stages are carried out at a low extracting temperature ( 4 ° c . ), the end product ( soymilk ) has a very low percentage of fat ( 0 . 08 %). as used herein , therefore , the phrase “ low fat ” means less than 0 . 10 % fat by weight based on the total weight of the products soymilk . ( 1 ) total or almost total non - desirable substances are eliminated from the soybean ( milk and okara ). ( 3 ) it does not require any chemical processing ; it does not require a chemical balancing stage . ( 4 ) the soymilk has a yield of at least 73 . 14 % of the usable soybean ( less fiber ). the objective is the solubilization of proteolytic enzymes in an acidic medium or environment . ( 6 ) the soymilk base can be used making excellent beverages , yogurt , ice cream , tofu , etc . ( 7 ) co 2 is more soluble than o 2 and helps to eliminate the o 2 , which is in the aqueous medium . ( 9 ) this process does not need a homogenization stage due to the soymilk being highly stable and with good properties . as used herein , the term “ bean flavor ” means that the products or byproducts of the present invention have no perceptible bean flavor on the human palate . having describes the present invention , reference will now be made to an example , which is provided solely for purposes of illustration and is not intended to be limitative . 4 . introduce the whole soybeans in a plastic bottle ( 2 liters of capacity ), 5 . put in the bottle 17 grams of dry ice in pieces , 6 . put in the bottle 0 . 5 liters of boiled water ( temp = 20 ° c . approx .) instead of deaerated water , 8 . the bottle put in the fridge ( t = 4 ° c .) the soaking step is made overnight and the pressure must reach to 4 atmospheres approximately , 10 . wash the wet and swelled soybeans strongly with tap water , 13 . while the mixture soybeans and water are blended , 91 grams of dry ice in pieces are introduced in the blender cup ( blending time = 5 minutes approx . ), 14 . the slurry is filtered using a fabric bag filter , raw soymilk extract and okara are separated , 15 . raw soymilk extract goes to the purification step . put the extract in the same blender that has already been washed . while the extract is blended again , 27 grams of dry ice in pieces are introduced in the blender cup ( time = 2 minutes approx . ), 16 . the purified raw soymilk is filtered again and cooked for 35 minutes ( 20 minutes of batch pasteurization ), and as noted from the above table relating to mass balance , the present process affords soymilk ( or extract of protein 50 . 16 % and carbohydrates 42 . 86 %). the precise relative amounts will depend upon the amount of water used in the process . furthermore , if desired , soy oil can be extracted from the okara produced by the present process using any knowing commercial extraction method . however before extraction the okara must be dried to a suitable humidity of about 13 – 30 % ( water content ). thus , the important end products of the present invention included soymilk or ( protein and carbohydrate ) extract , soy oil and fiber since as noted above , the present process may be further modified to include a conventional extraction step . yet , most importantly , all products and by - products of the present invention do not exhibit either a beany flavor or odor . as noted above , in accordance with yet another aspect of the present invention , seed oils , nut oils and even olive oil may be produced . as such , the present invention may be used to extract oil from seeds , particularly edible seeds with the use of the carbon dioxide atmosphere and conditions therewith described herein . however , in this process , an extraction step is used , after an initial wash / bath step , wherein the oil is extracted from the deaerated water with organic solvent . finally , a distillation step is used if desired , vacuum purification may also be used . for example , the sublimated carbon dioxide of the present invention may be used in conjunction with seeds such as sunflower seeds , flax seeds , rape seeds ( canola ), pumpkin seeds , safflower seeds , wheat germ seeds , grape seeds , corn seeds , cottonseed , peanuts , almonds , avocados , coconut , brazil nuts , pecans , pistachios , cashews , macadamias , and olives . the seeds are preferably dehulled in a conventional manner prior to the wash / bath / soak step in deaerated water / sublimated carbon dioxide . generally , when using any type of seed , the seeds are first subjected to the soaking extraction step using sublimated carbon dioxide in deaerated water as described above . then , the released oils are extracted from the deaerated water bath with a suitable organic solvent for the oil , which is preferably hydrophobic . such solvents are well - known and include hexane , for example . the lypoxigenase enzyme is recognized as the main producer of the majority of vegetable proteins in plants such as soybeans , peas and peanuts . oily polysaturated acids are oxidized by lypoxigenase catalytic action and produce bad odors such as aldehides , alcohol , ketones furans , hydroxyacids , etc . lypoxigenase is found in the cotydelons of legumes and many other seeds but the enzyme is inactive due to its limited contact with the oxygen in the substratum held in the cell &# 39 ; s structure . the cell structure &# 39 ; s break - up by grinding or milling leads to oxidization and so lypoxigenase needs to be inactivated in order to control bad flavors . the removal of bad odors in edible oils not only makes the refining process complex but also causes the oil to be degraded ( see u . s . pat . no . 4 , 915 , 972 ). one of the ways to avoid the negative effects of lypoxigenase is to use some the stages of this invention and adapt them to commercial methods . in traditional process used to produce soy oil the main residue extract is used for animal feed without taking into account the commercial value of the non - oily by - products as it is difficult or almost impossible to process it profitably . it would be ideal to obtain other products such as protein concentrates for human consumption using this by - product because the commercial value of soy meal is higher than profits from the sale of an equal quantity of oil . however , there is an equal demand for both soy oil and meal and so the meals &# 39 ; quality and soy &# 39 ; s make - up are important factors that need to be taken into account when choosing a processing method and the products one wants to obtain . new ways of processing soy can be found by using parts of the stages and / or the whole of this invention . as mentioned above , raw okara has good organoleptical properties ( it does not have a beany smell ) as well as containing most of lipids from soybeans ( yield is 87 . 19 %). also , as okara is processes under cool / cold conditions the oil content remains intact , and it is not degraded by heat or oxidization due to being processed in a co 2 atmosphere . starting with okara in raw state in which humidity should be 50 % of total weight , and due to this being one of the conditions for ensuring good drying by spray drying , this can be achieved by varying the conditions in which water is fed into the invention &# 39 ; s production process . okara is then dried using this method to a maximum humidity of 10 % of total weight . it is known that excessive humidity in the raw material can lead to problems such as its deterioration on one hand as well as difficulties of extracting oil because an emulsion would result that would be difficult to separate due to the presence of lecithin in the extract &# 39 ; s medium . after the drying stage the okara is cooked usually live vapor at temperature between 90 ° c . and 120 ° c . approximately . cooking in a humid atmosphere for de - naturalization of remaining proteins remaining in the okara and in some degree the coalescence of small droplets of oil . following this stage flakes are produced with the main purpose of increasing the surface contact between the okara &# 39 ; s texture which is mainly made up of 42 . 23 % fibers . 32 . 74 % proteins and 17 . 47 % fats . the high fiber helps in extraction as this increases the interface area and creates higher porousness in the okara flakes because these structures help to diffuse the solvent as well as in percolation . the soy flakes then go through a normal solvent extraction stage using a hexane ( by batch , semi - continuous or continuous ) to obtain two products : the okara waste ( with a minimal quantity of fat ) and the oil - rich soy solvent ( full micelle ). the following operations are aimed at removing and recuperating the solvent of each one of the streams . most of solvent extraction manufactures also offer micelle distillation systems which minimize damage to the raw oil and its components , minimum loss of solvent as well as other important characteristics . means of solvent vaporization include instant vaporation , vacuum distillation and steam stripping . on the other hand the used solvent is recovered from the okara waste using an okara desolventizer in this stage . the resulting soy oil contains certain types of wax which are edible substances that are solid at temperatures below 40 ° c . their presence give the oil a turbid character at low winter temperatures which is why they are eliminated during winterization where the raw oil is chilled at 0 ° c . and in this way the wax is crystallized to be easily eliminated from the oil . after this stage the raw soy oil goes on to be de - gumming in which phospholipids are eliminated . as most of the enzymes have already been eliminated in the inventor &# 39 ; s previous process it is believed that the carbon dioxide in the above - mentioned conditions have also eliminated certain enzymes that reduce the phospholipids &# 39 ; hydrability and in this way , the efficiency of the de - gumming is improved . the soy oil then goes through a neutralization stage in which the free oil acids in the oil are eliminated using an alkali , which may be any suitable inorganic base such as alkali carbonates or hydroxides , such as sodium carbonate or sodium hydroxide . these free oil acids are part of the rancid reactions which produce bad odors . soaps are produced from the neutralization reactions that are easily eliminated . in this way soy oil is obtained . it is assumed that this process does not need de - odorization or bleaching because it begins from a light raw material ( with no undesirable odors or pigments ) a highly preferred organic solvent for the extraction of oil from soybeans should possess the following properties : good solubility of the oil . poor solubility of non - oil . high volatility ( i . e . low boiling point ), so that complete removal of the solvent from the micella and the meal by evaporation is feasible and easy . yet , the boiling point should not be too low , so that extraction can be carried out at a somewhat high temperature to facilitate mass transfer . low viscosity . low latent heat of evaporation , so that less energy is needed for solvent recovery . low specific heat , so that less energy is needed for keeping the solvent ant the micella warm . the solvent should be chemically inert to oil and other components of the soybean . absolute absence of toxicity and carcinogenicity , for the solvent and its residues . non - inflammable , non - explosive . non - corrosive . commercial availability in large quantities and low cost . preferably , solvents used are low - boiling hydrocarbon fractions obtained from petroleum . generally , solvent having a boiling point range of less than 90 ° c . are preferred . a typical commercial solvent for oil extraction which may be used has a boiling point range ( distillation range ) of 65 to 70 ° c . and contains mainly of six - carbon alkanes , hence the name “ hexane ” by which these solvents are commonly known . “ hexane ” solvents for the extraction of edible oil must comply with strict quality specifications . the quality parameters which make up the specifications usually include : boiling ( distillation ) range , maximum non - volatile residue , flash point , maximum sulphur , maximum cyclic hydrocarbons , color and specific gravity . generally , any lower alkyl , i . e . up to about 15 , preferably up to about 12 carbons , hydrocarbons may be used as the extracting solvent to form a phase separation . for example , in addition to the preferred hexanes , mineral oils may be used . further , a temperature in the range of about 40 ° f . to about 90 ° f . is used for the extraction . preferably , a temperature in the range of about 50 ° f . to 80 ° f . is used . safety considerations , of course , mandate use of special standards for buildings and installations in solvent extraction plants . all the electrical installations must be explosion - proof . the discharge end of all vents must be equipped with refrigerated condensers to minimize escape of solvent vapors to the atmosphere . very strict safety measures must also be taken to prevent the hazard of sparks in and around the plant . all these add to the high cost of erection and operation of solvent extraction plants . thereafter , the oils are isolated by phase separation , and concentrated by distillation to remove all traces of organic solvent , which , of course , will have a much lower boiling point than the oil . finally , the distilled oil may be subjected to a conventional vacuum or reduced pressure treatment in order to further remove even trace amounts of solvent . generally , the same procedures may be used for the washing of seeds as with soybeans . notably , the seeds , which are preferably dehulled in a conventional manner , are contacted with deaerated water under an atmosphere of sublimated carbon dioxide in orders to extract seed oils therefrom . the seeds are then discarded , and the bath water containing the seed oil is subjected to extraction with organic solvent . generally , the bath water is contacted with an amount of extracting solvent which is from about 0 . 25 to 5 × volume of the bath water . preferably , the amount is from 0 . 75 to 2 × the volume of the bath water . thereafter , the organic solvent phase is removed with the seed oil by phase separation in a conventional manner . then , the organic phase may be dried with a desiccant to remove traces of water . thereafter , the solvent is removed y partial vacuum evaporation , such as with a rotary evaporator . thereafter , the isolated seed oil is obtained . having described the present invention , it will be apparent that many changes and modification may be made to the above - described embodiments without departing from the spirit and the scope of the present invention .
a process for preparing a beanless flavor soymilk or okara or a combination thereof , which compares the stages of containing soybeans with deaerated water under an atmosphere of carbon dioxide for a time and a temperature effective to allow said soybeans to soak and swell ; washing said soaked and swollen soybeans with water to remove oligosaccharides and ripening enzymes ; grinding said washed soybeans under an at atmosphere of carbon dioxide by bubbling in carbon dioxide in a sublimated state to form a slurry ; and filtering the slurry to produce raw okara and soymilk .