Field of the Invention * The present invention relates to methods for selectiv extraction of desired compounds from carbonaceous materials, an more particularly to a solvent extraction process for the remova 5. of selected compounds from carbonaceous materials. Background of the Invention

In many instances the characteristics of a particula carbonaceous material can be altered by the removal of certai compounds from the material. Examples of some compounds which i 0 may be desirable to remove would include: phospholipids, fats fatty acids, alcohols, waxes, gums, stearols, oil soluble proteins flavonol, mineral oils, essential oils, and PCB's.

More particularly, oils derived from plant materials, such a oil-seeds, cereal brans, fruits, beans, and nuts, are the source o J> raw material for many important commercial products. For example such oils from such plant materials are extensively used i cooking, low fat and fat free cooked food, in cosmetics pharmaceuticals as carriers for insecticides and fungicides, i lubricants, and in myriad other useful products. Consequently much work has been done over the years in developing improve processes for extracting oil from such materials.

One of the most widely used processes for removing oil fro oil-bearing materials is solvent extraction. In solven extraction, the oil-bearing material is treated with a suitabl % solvent, usually the lower carbon alkanes such as hexane, a

elevated temperatures and low pressures, to extract the oil fr the oil-bearing material. The resulting solvent/oil mixture then fractionated to separate the valuable oil from the solven which is recycled. Most solvent extraction processes in commerci use today employ hexane as the solvent. While hexane extraction i the most widely used today, there are also teachings in the art i which normally gaseous solvents are used at both supercritical an subcritical conditions.

One such teaching is found in U.S. Patent No. 1,802,53 to Reid, wherein a normally gaseous solvent, preferably butane o isobutane, is liquefied by decreasing the temperature and/o increasing the pressure, then passing the solvent through a bed o the oil-bearing material in an extraction vessel. The solvent an extracted oil are then passed to a still where the solvent i separated from the oil. The extracted material must then be place in another still where it is heated to remove solvent whic remained entrained in the extracted material. There is n suggestion of obtaining a substantially solvent-free, dry extracted material without an additional treatment step afte extraction.

Another extraction process is taught in U.S. Patent No 2,548,434 to Leaders wherein an oil-bearing material is introduce into the top of an extraction tower and passed counter-current t a liquefied normally gaseous solvent, such as propane, which i introduced at the bottom of the extraction tower. The tower i operated near critical conditions so that the solvent selectivel

rejects undesired color bodies, phosphatide, gums, etc. Th resulting solvent/oil mixture can then be flashed to separate th solvent from the oil. In another embodiment, the solvent/oi * mixture is first subjected to a liquid/liquid separation resultin 5_ in one fraction containing solvent and a less saturated fatt material, and another fraction containing solvent and a mor saturated fatty material. The solvent is then flashed from bot fractions. The extracted material remaining in the tower is draw off and subjected to a vacuum flashing operation to remov 0 entrained solvent.

U.S.Patent No. 4,331,695 to Zosel teaches a process fo extracting fats and oils from oil-bearing animal and vegetabl materials. The material is contacted with a solvent, such a propane, in the liquid phase and at a temperature below th 5 critical temperature of the solvent to extract fat or oil from th material. The resulting solvent/oil mixture is treated t precipitate the extracted fat or oil from the solvent by heatin the solvent to above the critical temperature of the solven without taking up heat of vaporization. The extracted residu 0 (shreds) is then treated to remove any entrained solvent, either b blowing it directly with steam, or by indirect heating followed b direct steaming.

In U.S. Patent No. 5,041,245 to Benado a continuous solven extraction method utilizing propane is disclosed to remove oil from vegetable matter, particularly rice bran. According to thi method a sufficient amount of liquid sealing medium is firs

injected into the vegetable matter in a feeding zone to form dough-like plastic mass which is compacted and transported by conveyor assembly to an extraction zone to form a bed. Propane then introduced into the bed of the extraction zone being operat at 102°-122°F. and 125-250 psi to react with the bed material. T miscella of extracted oil and solvent resulting from this from t reaction of propane and bed material is then separated from t remaining solid residue of the bed material. The propane is th separated from the extracted oil by evaporation or volatizati methods. The preferred separation method is to first subject th miscella to near its critical pressure (600 psi for propane/ric bran oil mixture) and significantly elevated temperatures (190° 200°F. for propane/rice bran oil mixture) which can also be nea critical. This yields a high solvent light phase (98% solvent, 2 bran oil) and an oil-enriched heavy phase (60% solvent, 40% bra oil) . The oil enriched heavy phase under reduced pressure is the delivered to a heater-evaporator and further treated to orm a mor oil-enriched heavy phase (10% solvent, 90% bran oil) . This phas is then de-pressurized to about one atmosphere, and further treate in a second combined heater-evaporator stage to produce an oi stream having not more than 1-2% propane. Further simila treatment of this oil stream could be accomplished to remov additional propane if desired.

Other references whichteach solvent extraction of oil-bearin materials, with normally gaseous solvents, include U.S. Patent Nos.

2,682,551 to Miller; and 2,560,935 to Dickinson. In each of thes

processes, the extracted material must be further processed t remove entrained solvent.

While prior art extraction methods, particularly hexan

_* extraction, have met with various degrees of commercial success j> there still remains a need in the art for an improved solven extraction method which is more energy and cost efficient, whic can effectively remove the solvent from the extracted compounds t meet government regulations, which is especially suitable for th processing of certain troublesome oil-bearing materials, as well a 0 which allows greater selectivity of the compounds removed from th carbonaceous material and which results in the recovery of de-oile products having superior nutrient and health characteristics.

In solvent extraction of oil from carbonaceous materials, suc as vegetable material, one problem has been fluidization problem 5 in the bed formed by the material in the extraction vessel. Thi has lead to the need to pre-pelletize or compact the materia before placing the material in the extraction vessel to increas the material bed permeability and allow the solvent to penetrat and flow through all portions of the material bed. This proble 0 is particularly acute in those situations where a significan amount of the vegetable material are of small particle size, e.g. 100 to 400 mesh.

When the carbonaceous material contains significant amounts o

* oil, current solvent extraction methods have been inefficient fo 5 removing most or all of the oil. Examples of such material woul include jojoba, cocoa, rape seed, and canola which are 30% - 60% b

weight oil. In these instances it has been necessary to fir press the material to remove a majority of the oil before usi solvent extraction methods to remove the remaining amounts of oi Alternatively, the material could be first mechanically ground o pulverized to render the oil more accessible to reaction with th solvent. This latter method is difficult if the material has high oil content.

In many of the instances where the material must first b pressed it is necessary to subject the material to hig temperatures (200°-360°F) to effectively remove the oil. In foo material such high temperatures can result in deleterious effect to the desirable characteristics of the material, such as protei denaturing, vitamin destruction, and creation of carbonic acid which effect the aromatic odor of food material such as spices an herbs.

One particularly troublesome material is rice bran, one of th most plentiful and nutritious food sources known to man, but whic is greatly under utilized. This is primarily because immediatel following the milling step, a lipolytic enzyme in the bran i activated which catalyzes the hydrolysis of the glyceryl esters o the free fatty acids (FFA) present in the lipids. This is measure by FFA increase, which is rapid at typical atmospheric storag conditions. This starts fatty acid formation and bran rancidity i a matter of minutes after milling, and eventually renders i inedible to humans after several days of storage. Consequently, rice bran, as a source of oil and food, is under utilized,

particularly in less developed countries. While the food industr struggles to find ways to obtain a rice bran, and rice bran oil free of these undesirable characteristics, more and more beneficia uses and nutritive values are being discovered for these products

5. For example, it has recently been reported that rice bran fiber i effective for lowering cholesterol in humans. As a result, tremendous demand has been created for a process which ca stabilize the rice bran after milling, or a process which wil allow for the extraction of oil while at the same time stabilizin 0 the oil and bran against further fatty acid formation.

Other problems are encountered with different food products

For example, in eggs it is desirable to remove the cholesterol fro the yoke, yet have the eggs retain their natural proteins no denatured, texture, and taste when cooked. This has not bee 5 possible with the present known methods of solvent extraction.

As another example, in many commercially available seasoning and food coating products one problem has been the inability t remove certain fats while retaining the flavoring of the products

Still another problem has been to create seasoned o 0 unseasoned food coatings that have dielectric characteristics whic increase the ability of the coating to adhere to the food produc during handling and cooking. A further problem with food coating occurs when the food product is mircowaved. The moisture in th

_* food product permeates the coating during the cooking proces 5 resulting in a soggy, unappetizing-looking crust.

Still other problems occur when trying to remove oils and fat

from fried products such as potato chips and french fries. Current methods result in undesirable flavor or texture change because of the inability of these methods to selectively remov only the undesired compounds. 5. The treatment of animal products by present solvent extractio processes to remove fats and cholesterol have not been commerciall successful because of the dilatory effect on the taste, color o texture characteristics of the cooked animal products. Summary of the Invention Therefore one object of this invention is to provide a solven extraction process for selectively extracting substances fro carbonaceous materials.

Another object of this invention is to provide a solven process for the selective removal of various oils from foo products that allows for cost effective removal of the solvent fro the extracted oils and de-oiled products which meet curren governmental regulations for low fat and fat free claims.

Still another object of this invention is to provide a solvent process for the selective removal of undesirable substances from food products which does not destroy the flavor, texture and/or coior characteristics of the food product.

A further object of this invention is to provide a solvent process for the selective removal of undesirable substances from food coatings which also increases their dielectric characteristics.

A still further object of this invention is to provide a

solvent process for the selective removal of undesirable substance from food coatings which also effects better sealing of moisture i the food product during cooking resulting in crisper, mor ■« appetizing products.

5 _. Another object of this invention is to provide novel oils an other substances having more desirable food consumptio characteristics.

Another object of this invention is to provide a novel ric bran oil and de-oiled rice bran. 0 A further object of this invention is to provide a novel mea product.

A still further object of this invention is to provide a nove food coating product.

Other objects and advantages of this invention will becom apparent from the ensuing descriptions of the invention.

Accordingly, a method for removal of selected substances fro carbonaceous material by use of a solvent is provided comprising

(a) introducing the carbonaceous material containing the selecte substances into an extraction zone to form a bed; (b) introducin a gas which at a given pressure liquifies at a higher temperatur than the solvent, the introduction being made under a pressure an at a temperature to cause the temperature and pressure of th extraction zone to be sufficient to cause the solvent to liquif

^* when the solvent is introduced to the extraction zone; (c) introducing into the extraction zone the solvent capable o extracting the selected substance; (d) passing the solvent throug

- ro - the bed of carbonaceous material to extract the substances from t material; (e) removing the resulting substance/solvent mixture fro the extraction zone to a separation zone under conditions whic will maintain the solvent in liquid form as it is passed throug the bed of carbonaceous material and out of the extraction zone t the separation zone; and (f) separating the solvent from th substances in the separation zone.

In a preferred embodiment of the present invention, th compound/solvent mixture is removed by introducing a secon compound, such as nitrogen, methane, or CO,, having dissimilar an greater vaporization conditions from the solvent which is used t not only purge the extracced compound/solvent mixture from th extraction zone, but to maintain the temperature and pressure s that the first introduced solvent is maintained in liquid for during the purging and movement to the separation zone.

In another preferred embodiment of the present invention, th material in the extraction zone is stressed by increasing for shor periods of time the pressure differential between the top an bottom of the extraction zone bed. Brief Description of the Fiσures

Figure 1 is a simplified schematic drawing of a preferre solvent extraction process of the present invention.

Figure 2 is a schematic representation of the reaction vesse utilized in experiments described below.

Figure 3 is a graphical representation of the results of test run utilizing the process of this invention in extracting oils fro rice bran. Figure 4 is a graphical representation of the results of test _ run utilizing the process of this invention in extracting oils fro certain commercially available cooked food products.

Figure 5 is a graphical representation of the results of test run utilizing the process of this invention indicating the effec on the flavor, color and shape of certain commercially availabl cooked food products.

Figure 6 is a graphical representation of the results of test run utilizing the process of this invention in extracting butte fat from certain name brand cocoa powders.

Figure 7 is a tabular representation of the characteristics o a rice bran de-oiled in accordance with the process of thi invention. Description of the Preferred Embodiments of the Invention

Any carbonaceous material can be treated to selectivel remove substances by the solvent extraction method of the presen invention. Non-limiting examples of such carbonaceous includ soybeans, cottonseed, linseed, and cereals such as rice bran, whea bran, and corn meal, as well as small particle products such a food coatings, meats. Non-limiting examples of the types o substances which can be removed from such materials includ phospholipids, fats, fatty acids, alcohols, waxes, gums, stearols

oil soluble proteins, flavonol, mineral oils, essential oils, oi from cooked or processed food, and PCB's.

Solvents suitable for use in the present invention are a solvent which is normally a liquid at extraction conditions, and 5. which the compound to be extracted is soluble under the reacti conditions. The selection of the appropriate solvent (o combinations of solvents) can thus be made based on its (their known solubility characteristics. If there is to selectiv removal of substances, then the solubility of those substances mus be considered in the selection of the solvent (or combination o solvents) , as well as the operating conditions used in the process In certain circumstances, such as when treating food products other known characteristics of the solvent may need to be take into account. Without limiting the scope of this invention, the preferre embodiments are described as applied to the treatment of certai food products to remove oils, waxes, gums, fats, and/o cholesterol.

Depending on the particular type substances being remove solvents suitable for use in the present invention would includ any solvent which is normally a liquid at extraction conditions, such as hexane, or which can be converted to a liquid at extractio conditions. Preferred solvents are those which are normall gaseous at typical atmospheric conditions. That is, those whic are a gas at about room temperature (about 70 ^β F) and atmospheri pressure. Non-limiting examples of preferred solvents includ

methane, ethane, propane, butane, ethylene, propylene, butylene sulfur dioxide, carbon dioxide, CHF ₃ , CC1F ₃ , CFBr ₃ , CF ₂ =CH ₂ , CF ₃ -CF ₂ CF ₃ , CF ₄ , CF ₄ , CH ₃ -CF ₃ , CHC1 ₂ , ammonia, nitrogen, dichlorodifluo _* methane, dimethylether, di ethylsufaoxide (DMSO) , acetone, nitriou 5_ oxide, methyl fluoride, and halogenated hydrocarbons o combinations thereof which are normally gaseous as indicated, a well as various alcohols. For removal of oil from rice bran an similar grains preferred solvents are propane, butane, and mixture thereof; and, more preferred is propane. 0 The weight ratio of solvent to oil-bearing material will b from about 1:1 to 2:1, preferably from about 1.2:1 to 1.5:1. A co solvent, such as a Cj to C ₆ alcohol, preferably ethanol, may b used. If a co-solvent is used it may be used in place of at leas about 0.5 to 90 vol.%, preferably about 5 to 50 vol.%, and mor preferably from about 5 to 25 vol.%, of the primary solvent.

Referring now to the Figures, oil-bearing material i introduced into extraction zone E via line 10. The extraction zon can be comprised of one or more vessels suitable for the volumes temperatures, and pressures employed. For illustration purposes only one vessel is shown, but in actual practice it would b preferred to use two or more vessels. In this way, while a vesse has undergone extraction and is being unloaded, another vessel ca be loaded with the oil-bearing material to continue the extractio

' process. This would represent a continuous type of operation Unlimiting types of vessels which may be used in the extractio zone include fixed-bed, slurry-bed, moving-bed, as well as reactor

in which the oil-bearing material is fed therethrough on or in bucket, a belt with perforations, or with a screw. It is preferr that the vessel be one in which a limited fixed-bed of oil-beari material can be loaded with a sealing piston. It is preferred evacuate the vessels of the extraction zone prior to t introduction of solvent, especially if the.solvent is propane whi may form an explosive mixture with air. The evacuation can conducted in any suitable manner, such as, by use of a vacuum pu or by merely venting the air as it is displaced by the solven during solvent loading or circulating N ₂ or C0 ₂ through the botto and out the top. Because certain solvents, such as propane, ca become explosive when mixed with air special conditions or step may be needed if such a solvent is selected. Such conditions o steps are well known in the art. Of course any propane whic contaminates the vented air can be separated by pressure o membranes, etc. or burned-off as a heat source during venting.

It is also within the scope of the present invention that th extraction zone be flushed with inert gas prior to introduction o the solvent. That is, by displacing the air in the extraction zon with the inert gas. It is preferred that the inert gas be a elevated temperatures, for example at a temperature from about 80 to 400°F, but which does not heat the material beyond 140°F preferably from about 55° to 120 ^β F, during the heat transfer. Thi hot inert gas flush will act as evacuating the extraction zone o air as well as heating, or drying, the oil-bearing material.

It is preferred that the oil-bearing material be dry befor being contacted with the solvent to mitigate any freezing which ma occur during the process. While the hot inert gas can be used t _ϋ dry the oil-bearing material, it may also be dried by any othe

5. appropriate means, such as by heating it by conventional means including the use of microwaves. Furthermore, after flushing th extraction zone with inert gas, the inert gas can be used t pressurize the extraction zone so that when the normally gaseou solvent is introduced into the extraction zone it is immediatel 0 transformed to the liquid state to prevent referation freezing.

Returning to the Figures, the normally gaseous solvent is fe into the extraction zone via line 12 in the vapor state, whereupo an effective pressure and temperature which will cause the normall gaseous solvent to liquefy. It is also within the scope of thi invention that the normally gaseous solvent be introduced into th extraction zone already in a liquid state. The inert gas can als be used to pressurize the extraction zone so that as the normall gaseous solvent enters the extraction zone, it is converted to it liquid form. Typically, the extraction temperature will be fro about ambient temperature, up to, but not including, th temperature at which degradation, or denaturing, of the proteins o the oil-bearing material is initiated. It is also desirable t protect the vitamins against degradation. This temperature wil typically range from about ambient temperature to about 140°F preferably from about 60°F to 130°F, more preferably from abou 70°F to 120°F, most preferably from about 70 ^β F to about 110°F.

For heat sensitive material such as dried egg yolks it is preferr that the temperature be 60°-90°F. It is within the scope of th invention to operate the extraction zone at a temperature and/ pressure which will selectively remove the oils, but leave a 5. substances such as gums and waxes in the extracted oil-beari material, or to selectively extract the phospholipid gums and wax with the heavier oil fractions. Such a temperature will typical be less than about 80°F at about atmospheric pressure. Of course the temperature may vary somewhat at different pressures. I addition, these temperatures may vary for any given oil-bearin material and solvent combination, and the precise conditions ar within the skill of those in the art given the teaching herein. After the oil has been removed, it is then possible to similarl treat the remaining material, but at slightly elevated temperature and/or pressures conditions to remove the waxes and gums. Th above stated conditions are the preferred conditions when the oil bearing material is rice bran and the solvent is propane. Sinc the de-oiled rice bran is a commercially important product it i preferred that the temperature not be so high that the proteins an vitamins of the rice bran are destroyed during the extractio process. The pressure maintained in the extraction zone will be pressure which is effective for maintaining the solvent as liquid, and to drive the oil/solvent mixture rapidly through th vessel. While this pressure will be dependent on such things a the particular solvent and temperature employed, for propane i will typically range from less than atmospheric pressures to abou

250 psig, preferably from about -15" Hg to 200 psig, mor preferably from about 100 psig to 140 psig.

The extraction zone can also be subjected to conditions whic - will repeatedly stress and relax the oil-bearing material and/o j> solvent molecules. This is believed to create a washing effec that enhances the ability of the solvent to extract the oil fro the material. In addition it is believed that such pressur pulsing aids in the separation of the heavier oil from the lighte solvent after the oil has been extracted from the material an 0 while it is flowing toward the bottom of the reactor. Suc stressing and relaxation are effected to create pressur differentials between the top and bottom of the extraction zone o at least 0.25 psig. The pressure differential can be as great a will permit, under the temperature and pressure conditions of th 5 material bed, the solvent passing through the exit port of th reactor to remain as a liquid.

This pressure differential can also be created by actuatin and deactuating a piston or diaphragm in the pressure or solven line. The stressing and relaxation conditions can also be caused b 0 sonification; i.e., by subjecting the ingredients of the extractio zone to sonic energy.

In a particularly preferred method a second solvent or iner gas is introduced to the top surface of the extraction zone t increase the pressure and then briefly open valve in the separatio zone to cause the second solvent or inert gas to displace part o the propane/oil mixture through the bottom filter. In this manne

it acts as a fluid piston. This action allows the bed to comprised of much smaller particles than has generally heretofo be used in solvent extraction processes. There is no need to pr pelletize such particles before treatment. This also allows the utilization of the forces of polarity combination to extract different materials at the same time using pressure from the second gas. By selecting a second solve having a different polarity that solvent can be used to remo different substances, such as cholesterol from egg powders. The period of time that the valve remains open would sufficient to permit at least some of the extracted oil and propa to flow through the bottom filter in the reaction vessel and in the separation zone. The extracted oil and propane can at tha time be separated if desired. After the valve is close additional liquid propane or N ₃ is then added to the bottom of th extraction zone to again raise the pressure and clear the filter i the extraction zone and purge the second solvent or inert gas. I another compound was extracted by the second solvent, then th mixture of the second solvent and this other compound will b forced through the top filter of the extraction zone and into a upper separation zone where the other compound can be recovered b known separation techniques.

In an alternate embodiment the bottom valve can be continuou open, and the top valve of the reactor through which the second ga enters the extraction bed can periodically be opened. This i achieved by setting the pressure at the top valve sufficient highe

than the desired pressure in the extraction bed, and by opening t top valve before the pressure at the bottom valve reaches pressure too low to maintain the extraction bed pressure at t desired level. The pulsing procedure may be repeated as many times as desir and with the proper construction of the reaction vessel utilizi many different solvents. The number of pulsings, as well as t amount of the pressure differential, and the time between pulse depends on the accessibility of the oil in the oil bearing materi for contact by the solvent, as well as the polarity strengths the substances involved; i.e., how strongly bonded the oil is other substances, such as the proteins, in the product.

The extraction can also be accomplished in more than o extractions; i.e.,the oil-bearing material can undergo sever extractions with fresh solvent in order to assure more comple removal of oil. For example, a first extraction may leave as mu as about 1 to 3 vol.% of the oil in the material which weig percent is based on the total weight of the extracted material. substantial amount of this residual oil can then be removed subjecting the oil-bearing material to at least one oth extraction with fresh solvent. It is preferred that less th about 1 wt.%, more preferably less than about 0.1 wt.% of t extracted material represent that residual oil fraction in the d oiled material. Of course, the economics of the process must considered so that the cost of additional extractions does n

exceed the value of the added products from the addition extractions.

The oil-bearing material preferably sits on a filtering mean such as a screen, or membrane filter, or perforated tray (n shown) , wherein the solvent passes there-through with the extracte oil. It is understood that an alternative process feature is on wherein the iltering means is situated between the extraction zon and the separation zone. The solvent is maintained in contact wit the oil-bearing material for an effective period of time. That is for a period of time which will result in the extraction of predetermined amount of oil. Of course, if too much oil stil remains in the oil-bearing material after extraction, it may b subjected to one or more additional extraction cycles or th extraction time extended with pressure pulsing according to th condition of the oil-bearing material feedstock or the desire product to be recovered.

The solvent/oil mixture is passed from the extraction zone vi line 18 to separation zone S under conditions which will maintai the solvent as a liquid. It is important that the pressure b maintained in the extraction zone during removal of the solvent an oil not only to prevent unnecessary evaporation of solvent durin removal which may result in freezing of the extracted material, bu also to not complicate the removal of excess solvent in th material to less than that permitted by government regulations. A preferred method of maintaining the pressure in the extractio zone during removal of solvent and oil is to introduce a gas whic

has dissimilar vaporization condition characteristics from th solvent, more particularly vaporization condition characteristic greater than the solvent so that it can be used to add pressure an heat to the extraction zone during the removal of the oil/solven mixture to prevent freezing of the oil bearing material, th remaining oil/solvent mixture, and the extracted mixture.

Such gases would include an inert gas, such as nitrogen, int the extraction zone to replace the leaving solvent/oil mixture. B "inert gas" is meant a gas which will not cause a deleteriou reaction of the extracted oil or extracted material. Th preferred inert gas is nitrogen, carbon dioxide or methane. Mor preferred is nitrogen. The gas replaces the solvent/oil mixture i the extraction zone and maintains substantially the same pressur throughout the solvent/oil removal step. This prevents freezing o the extracted material. It is preferred that the inert gas whic is introduced into the extraction zone to displace the solvent/oi mixture be heated. That is, that it be at a temperature from abou 60 ^β F to 140°F, preferably at a temperature from about 100°F t 120°F. This heated inert gas can enhance the recovery of an residual oil and solvent left in the extracted material.

It is also preferred that in designing the reactor vessel an in selecting the solvents to be used, the specific gravities of th substances to be removed and the specific gravity of the solvent be as different as possible. This has found to be beneficial i the separation of the oil and solvent from each other, as well a the oil bearing material, during the pulsing stages. For exampl

the large differtial in the weight of propane and oil causes th propane to separate from the oil and move upward in a purified for to contact more oil still bound in the rice bran while th extracted oil rapidly moves toward the separation zone for removal 5. This reduces the amount of solvent needed to remove the oil and/o reduces the amount of separation of solvent from the extracted oil It is also within the scope of this invention that solven vapor be passed through the de-oiled material either in place o the inert gas or following the passage of inert gas. This solven vapor will act to remove at least a portion of the residual oil solvent mixture left in the de-oiled material.

The separation zone is run under conditions which will enhanc the separation of solvent from the oil. It is preferred that som heat be applied preferably from a slightly heated solvent or iner gas, to enhance this separation. Other methods which can b employed for operating the separation zone to enhance solvent/oi separation include distillation, centrifugation, the use o membranes and reduced pressures, and/or cryogenics. The separated solvent is then passed, via line 20, to storage zone ST where it can be recycled via line 22 to the extraction zone. Makeup solvent, if needed, can be added via line 24. At least a portion of the recovered solvent may also be recycled directly to the extraction zone via line 26.

It is also within the scope of the present invention that the separation be conducted in more than one vessel. For example, the solvent/oil mixture (which may also include some of the second

dissimilar gas) may first be subjected to a first separator vesse wherein a liquid/liquid (and gas if the second dissimilar gas i present) separation occurs. That is, the separation vessel i under enough pressure so that the solvent will not vaporize. Th liquid solvent is separated from the oil phase. The liquid solven fraction is then introduced into a second separation vessel wherei a liquid/vapor separation occurs. That is, the solvent i vaporized and collected in a storage vessel and any residual oi fraction is separately collected. This second vessel wil typically be smaller than the first and may include the use of vacuum or other conventional means to aid in the vaporization o the solvent.

If gums and waxes, or certain oils, are present in th extracted oil fraction, they may be solidified out of the oil b cooling. The cooling can be provided by use of the vaporize solvent which will still be cool owing to the vaporization step.

The substantially solvent-free oil is collected via line 30 The de-oiled oil-bearing material can be collected from th extraction zone by any appropriate means. For purposes o simplification, the de-oiled material is shown in the Figure a being collected via line 32.

In those situations where the oil-bearing material is on which is unstable because of the production of fatty acids, such a rice bran, a stabilizing agent can be added to the extraction zon via line 34. Any appropriate means can be used to add th stabilizing agent. That is, it can be sprayed directly onto th

oil-bearing material prior to the material being introduced in the extraction zone. It can also be introduced into the extracti zone either directly, (as shown in the figure) or in combinatio with the solvent. Rice bran, the preferred oil-bearing material upon milling, activates lipolytic enzymes which catalyze th production of free fatty acids. These free fatty acids cause th bran to become rancid. Non-limiting examples of stabilizers whic can be used to stabilize rice bran include an inert gas such a nitrogen, food grade acids and alcohols, preferably ethanol ercaptans, and enzyme inhibitors, protein, and/or peptides Preferred are food grade acids and alcohols, non-limiting example of which include citric acid, ascorbic acid, lactic acid, gluconi acid, malic acid, ethanol and the like. More preferred are citri acid and ascorbic acid, with ascorbic acid being most preferred. The rice bran which results from the preferred embodiment o the present invention is unique in the industry in commercia quantities. That is, not only are the fatty acids stabilized, bu deleterious ingredients which contribute to poor taste are als absent. Furthermore, the rice bran of the present invention als contains more vitamin B's and even protects the cyanocobalami (vitamin B-12) than an identical bran which has been extracted b use of a conventional hexane extraction process. Consequently, th rice bran produced in accordance with the present invention fill a long felt need in the art. Utilizing the reactor vessel 100 schematically illustrated i

Figure 2 the experiments results of which are described in Figures

3 - 7 were conducted as follows. The rice bran or other mater was introduced to the extraction zone 101 of the reactor 100 line 102. Valve 103 operatively attached to line 102 was clos Nitrogen was then introduced into the bottom of extraction z 5. 101 via line 104 in sufficient quantity to purge the air f extraction zone 101 into upper separation zone 105. The air then purged from upper separation zone 105 through line 106 i the atmosphere. The pressure in extraction zone 101 was t adjusted and maintained at 90 psi. Propane was then introdu 0 through line 104 into extraction zone 101 in quantities suffici to purge the nitrogen from the reactor 100 through line 106 and increase the pressure within extraction zone 101 to 127 psi.

Nitrogen was then reintroduced through line 107 in quantiti sufficient to create a pressure differential between the top a bottom of extraction zone 101 of 1-50 psi. Valve 106 was th cracked open until the pressure differential has been dissipated which time valve 106 is closed. This procedure is repeated f about ten minutes by re-introducing nitrogen through line 107.

Nitrogen was then used to purge extracted oil/propane mixtu from the evaporation zone 101 and from reactor 100 through li 109. At all times during the procedure to this phase, the pressu and temperature was maintained at levels to prevent the propa from vaporizing while the oil/propane mixture was forced throu the 400 mesh bottom filter 108. Vacuum to 15" Hg is completed and nitrogen at 80°F. was t circulated through the evaporation zone 101 to remove all tra

amounts of propane which remained in the de-oiled rice bran whic was removed from reactor 100 through line 106.

Upper 200 mesh filter 110 is removed and the de-oiled ric bran was removed from reactor 100. The extracted N ₂ /oil/propan mixture removed from reactor 100 were separated by alternatel cooling and heating, and use of pressure in a separate vessel 20 by well known means.

The de-oiled rice bran or other material was then analyzed. The results are summarized in Figures 3 through 7.