MXPA96001735A

MXPA96001735A - Procedure to extract ace

Info

Publication number: MXPA96001735A
Application number: MXPA/A/1996/001735A
Authority: MX
Inventors: M Hebert Roland; J Stonicher Robert; T Tucker Robert
Original assignee: Agritech International Llc
Filing date: 1996-05-09
Publication date: 1998-07-03

Abstract

The invention relates to a process for extracting oil from a plant material containing oil, with the use of a suitable solvent to dissolve the oil in the plant material. The ground plant material is deposited in a reactor vessel, and vacuum is created in the reactor vessel. The liquid solvent is introduced into the reactor vessel and allowed to contact the plant material for a sufficient time to dissolve oil from the plant material, while the temperature in the reactor vessel is maintained at a level that prevents denaturation of the constituent components of the reactor. oil of plants and plant materials. Additional solvent vapors are introduced into the bottom of the reactor to cause mixing of the plant material and the solvent and to separate fine particle matter from the heavier particles. Vapors of pressurized solvents are introduced into the upper part of the reactor vessel, while the solvent combination of liquid and oil is removed from the bottom of the reactor vessel through filters. To avoid clogging of the filters at the bottom of the reactor vessel, solvent vapors under pressure are forced through the filters to the bottom of the reactor vessel. The solvent and oil combination is transferred to the separator vessel, where the solvent is evaporated and removed for recycling, while the oil is removed in a holding tank.

Description

PROCEDURE FOR EXTRACTING OIL CROSS REFERENCE TO RELATED APPLICATION This application corresponds to a continuation-in-part of the patent application of the U.S.A. Serial No. 07 / 873,783, recently pending in the Patent Office, of which priority is claimed. BACKGROUND OF THE INVENTION 1. Field of the Invention This invention relates to a method for extracting oil from parts of plants containing oil, such as seeds, fruits, nuts, leaves, germ, bran, barks and roots and more particularly to a method to extract these organic oils at sufficiently low temperatures, lower than 71.1 ° C (160 ° F) to not denaturalize proteins, vitamins and minerals, resulting in two useful substances and distributable in the market, oil and defatted flour. 2. Background When harvested, unpolished rice, also called paddy or paddy rice, consists of a core of rice with starch surrounded by a firmly adhering brown coating of bran and circumscribed with a loose outer shell or bark. In commercial practice, the palay first dries and then grinds. In a mechanical milling process, the husk and bran are removed to obtain white rice. The grinding sub-products are rice husks and rice bran. The husks of rice are primarily celluloses, lignin and minerals, with no food value or significant food. For the most part, husks that average approximately 20% of the weight of the rice are discarded as waste material or used as a low-value soil conditioner, fuel or raw abrasive. Rice bran, on the other hand, is rich in protein (13 to 16%) and food energy and contains high levels of natural vitamins and trace minerals, essential. These qualities have led to a high demand for rice bran as an animal feed ingredient, and it is used extensively for this purpose all over the world. The bran represents in weight 4 to 9 percent of the rice, varying with the location of the crop and the degree of milling. Under normal conditions, when the raw rice is milled in white rice, the oil in the bran (16 to 22%) and a potent lipase, also in the bran, come into contact with each other. This results in rapid degradation of the oil in glycerol and free fatty acids. In this way the bran produced is unpleasant to the palate and is not used as a food. On the contrary, it is used as animal feed. Hexane is conventionally employed as a solvent for extracting oil from rice bran. The use of hexane presents potential air pollution problems. More importantly, extraction with hexane solvent requires high operating temperatures (greater than or equal to approximately 71.1 ° C (160 ° F)) that denature or degrade the functional and nutritional properties of rice bran and rice bran oil. . Thus, some means of extracting oil from rice bran that does not denature or degrade the functional and nutritive properties of rice bran and its oil, will be convenient. More specifically, solvent extraction is desired which does not require high operating temperatures (about 71.1 ° C (160 ° F)) which results in the denaturing of rice bran and its oil. Other solvents, such as propane, ethane, carbon dioxide, dinitrogen oxide, butane and isobutane, have been used to extract oil from plant material that contains it, but at operating temperatures not low enough to avoid denaturation of proteins, vitamins and minerals or otherwise using separate containers to perform the dissolution and extraction stages, or both. Conventionally, there are various methods for extracting oils from organic material, including the use of liquid hydrocarbons, for example, U.S. Patents. us. 4,331,695; 2,560,935; 183,097; 183,098; 2,485,916; 2,571,948; 2,727,914; 3,261,690; 3,271,160; 3,492,326; 3,542,559; 3,852,504; 4,457,869; 4,486,353; 2,548,434; and 1,802,533. Patent No. 4,334,695 issued to Zosel, describes propane and other hydrocarbons as solvents; however Zosel uses extremely high pressures (approximately 42 atmospheres), the extraction is carried out at high temperatures (80 ° C to 176 ° C) which would denature the proteins and seems to require constant pressure with a potential temperature oscillation of 0 ° C at 100 ° C. Patent X935 describes propane as a high temperature solvent (substantially above 60 ° C (140 ° F)) in a two stage extraction process. Patents * 097 and? 098 introduce water to the process. Patent x916 describes a pre-extraction process involving alcohols and soap at a temperature between 10.6 and 100 UC (51 and 212 ° F) followed by heating to almost the boiling point of the solvent. Patent v948 describes steam distillation. The Patent 914 describes cooking rice bran before extraction with solvent, at temperatures above 76.7 ° C (170 ° F). Patent * 690, uses over-heated steam to extract the oil from the solvent. Patent 160 describes processing safflower seed residues after the oil is extracted. Patent v326 describes extraction with liquid hydrocarbon solvent so as not to extract more than 10% by weight of rice bran rice oil at entry temperature using hexane between 49 and 71.1 ° C (120 and 160 ° F) to subject the rice without polish at a temperature between 51.7 to 54.4 ° C (125 to 130 ° F).

Patent? 559 describes hexane or liquid hydrocarbons between 46.1 and 49 ° C (115 and 12 ° F). Patent 281 describes extraction at both high temperatures and high pressures. Patent * 869 describes high temperature extraction using solvents based on isopropyl and isopropanol. Patent v353 uses ethanol at 70 ° C (158 ° F) and above. Patent * 434 describes gaseous hydrocarbons at high pressure and at high temperature (55.6 to 93.3 ° C (150 to 200 ° F)). Patent * 533 describes butane, propane and other hydrocarbons at 26.7 ° C (80 ° F) and 2,109 Kg / cm2 man. (30 psig) or and 15.6 ° C (60 ° F) and 1.05 Kg / cm2 man. (15 psig), but the flour is placed in a distiller or separate still, where it is heated to remove the solvent. CQMPENPIQ PE? INVENTION The present invention provides a method for extracting rice bran oil, the method is characterized in that it includes the steps of: 1) Placing rice bran containing oil in a reactor vessel; 2) removing air from the reactor vessel by applying a partial vacuum, introducing an inert gas under pressure into the reactor vessel to disperse additional air and applying a second partial vacuum; 3) Introduce to the reactor vessel a liquid solvent having a solvent power for rice bran oil (i.e. capable of dissolving rice bran oil), the liquid solvent is maintained at a temperature between about 20 ° and 51.7 ° C ( 68 ° and 125 ° F), preferably between 20 ° and 22 ° C (68 ° and 72 ° F); 4) Allow the liquid solvent to contact the rice bran for a sufficient time to dissolve a substantial portion of the rice oil; 5) Introduce gaseous solvent to the bottom of the reactor vessel to mix the rice bran in the mixture of liquid solvent and oil; and 6) Remove the combination of solvent and rice bran oil from the reactor vessel. Preferably, the combination of solvent and rice bran oil is removed from the reactor vessel while additional liquid solvent is introduced into the reactor vessel, thereby washing the rice bran, until less than 1% by weight of the bran oil of rice remains in the rice bran. Preferably, the separation of the solvent and oil combination and the introduction of additional liquid solvent is carried out simultaneously to maintain a relatively constant liquid level in the reactor vessel. The temperature of the solvent is critical for a successful practice of the invention. If the solvent is too hot (more than about 51.7 ° C (125 ° F)), then the oil will not be well washed from the bran, possibly because the bran will not absorb the solvent well. If the solvent is too cold, then the bran will absorb the solvent but the bran will not easily release the solvent and oil combination, and thereby increase the process performance time in this unusual manner. Additionally, it is convenient to separate the residue of rice bran particles in various sizes. More generally, the solvent extraction method at low temperature is useful to extract oil from the parts of plants that contain oil without denaturing the vitamins, proteins and minerals contained therein. It is therefore an object of this invention to provide a process for extracting rice bran oil from rice bran and more generally to extract oil from plant parts containing oil. A more specific objective of the invention is to provide a method that includes contacting rice bran containing oil with a suitable solvent, the combination of solvent and rice bran is maintained at a temperature below about 71.1 ° C (160 ° F) which does not denature the constituent components of the rice bran oil and the rice bran.

Another object of the invention is to provide a method for separating different sizes of rice bran particles within the reactor vessel during the process of extracting oil from the rice bran. Further objects and advantages are set forth in part in the following description and in part are evident from the description or can be learned by practice of the invention. The objects and advantages of the invention can be achieved and obtained by the articles and apparatuses particularly indicated in the appended claims. BRIEF DESCRIPTION OF THE DRAWINGS Reference will now be made to the drawings, in which similar parts are designated by similar numbers and where the Figure 1 is a schematic illustration of a system for extracting oil from a plant material containing oil according to the present invention. Figure 2 is an exploded partial sectional view of a filter adapted for use in a reactor vessel according to the present invention. DETAILED DESCRIPTION OF THE INVENTION Now with reference to the drawings in more detail, the Figure 1 illustrates in a schematic form, a system for extracting oil from a plant material containing oil according to the present invention. As can be seen in the drawing, the system comprises a reactor vessel 2 designed to receive a plant material containing oil, for example rice bran. The reactor vessel 12 is charged with rice bran through an opening in the upper part by a pneumatic charging system 4. The reactor 2 can include a material level meter 6 to indicate when the reactor 2 is filled with bran from raw wheat to a desired level. The level 6 pressure gauge can automatically cause an interruption of the pneumatic load system 4, when a desired filling level has been reached. The rice bran will accumulate and clog if left to settle in the automatic loading system. This crude rice bran will begin to accumulate free fatty acid and will result in an acceleration of rancidity. The pneumatic load system 4 should be kept as free as practical between loading operations. The valve 8 in the upper part of the reactor 2 is closed after the pneumatic load lines are blown off. Using the vacuum pump 10, preferably a compressor without oil or alternatively 2 compressors, establish a vacuum of 30.48 to 38.1 cm (12 to 15") of mercury (8.5 to 8.8 psia) in the reactor. preferably nitrogen, then introduced from tank 12 to reactor 2, thereby pressurizing the reactor to a positive value of 1045 to 1758 kg / cm 2 (15 to 25 psig) /2,109 to 2,812 kg / absolute cm2 (30 -40 psia) Then a second vacuum of 30.48 to 38.1 cm of mercury (12 to 15") of mercury (8.5 to 8.8 psia) is established inside the reactor and inside the evacuation line 12. The system is then released. vacuum and the reactor is ready to fill it with liquid solvent. The liquid solvent, preferably propane, at a temperature between 20 and 51.7 ° C (68 and 125 ° F) is pumped by a pump 14 from tank 16 to reactor 2 through an opening 18 in the upper part of the container reactor. When the gauge pressure in the reactor 2 is increased to 0.3115 Kg / cm 2 gauge (5 psig) / 1,406 Kg / cm 2 absolute (20 psia) below the gauge pressure in the solvent storage vessel 16, the bypass line 20 it is opened to allow the vapors that are collected in the reactor 2, to move to the vapor section of the solvent storage container (16), thus allowing a constant and continuous movement of liquid solvent to the reactor 2. To a Pre-determined level of liquid in the reactor, preferably when the rice bran inside the reactor is covered by liquid solvent, the bypass line 20 is closed and the final movement of the liquid solvent to the reactor 2 is carried out. Bypass line 20 is closed before a complete filling with liquid, to prevent the material from flowing back to the steam lines. The filling system with a solvent is then released. The liquid solvent is constantly maintained by the heat exchanger 22 within the temperature range 20 to 51.7 ° C (68 to 125 ° F), preferably 20 to 22.2 ° C (68 to 72 ° F) before and during filling of liquid from reactor 2, in order to cause the liquid solvent to dissolve the rice oil from the bran in reactor 2, at a pre-determined speed and time. As the solvent temperature increases beyond 22.2 ° C (72 ° F), the color of the rice bran oil becomes darker. Within 20 to 22.2 ° C (68 to 72 ° F), the rice bran oil remains clear in color. Before removing the liquid solvent containing dissolved oil from the reactor 2 to the separator 24, additional solvent vapors from the solvent storage container 16 are introduced from 703 to 1,406 Kg / cm 2 (10 to 20 psig), 1,768 to 2.46 Kg. / cm2 absolute (25 to 35 psia) on the pressure of the reactor inside the bottom of reactor 2, to mix the rice bran in the combination of liquid solvent and oil, thus starting a first stage in a pre-classification of material in the reactor. This pre-sorting mixing procedure causes the heavier rice bran particles to settle to the bottom of the reactor, with the finer particles also referred to as fines that float to the top of reactor 2. After allowing the contents of the reactor are sedimented, usually 10 to 15 minutes, the combination of liquid solvent and oil is then transferred from the bottom of reactor 2 to the top of separator 24. The combination of liquid solvent and oil is pumped by pump 28 beyond of indicator 30, which measures the severity of the combination of liquid solvent and oil, to determine the percentage of oil in the solvent. While the indicator 30 records more than 1 percent oil in the combination of liquid solvent and oil, the pump 14 is activated to pump fresh liquid solvent from the storage vessel 16, through the valve 18, and into the reactor 2. , to maintain a constant level of liquid in the reactor 2. When the indicator 30 registers less than 1% oil in the combination of liquid solvent and oil, the pump 14 is turned off. As the combination of liquid solvent and oil is pumped by the pump 28 from the reactor 12 to the separator 24, fresh solvent vapors from the storage vessel 16 are added to the reactor 2 via the compressor 10 through the heat exchanger 32, forcing in this manner vapors of hot solvent to the upper part of the reactor 2 through the line 34 and pushing the combination of remaining liquid solvent and oil through the rice bran in the reactor 2, through the filter system 36 to the bottom from reactor 2 and separator 24. Fresh solvent vapors are added until a pre-determined liquid level shows that approximately 100% of the combination of liquid solvent and oil remain in reactor 2. Either a peephole 38 or an indicator automated allow the level of liquid to be checked. The transfer of liquid from the reactor to the separator is then stopped by turning off the pump 28. Additional heated solvent vapors are introduced to the reactor 2 from the storage vessel 16 by the compressor 10 through the heating coil 32, to increase the pressure between 1.758 to 2.46 Kg / cm2 gauge (25 and 35 psig), 2.812 to 3.15 Kg / cm2 absolute (40 to 50 psia). After waiting for approximately 6 to 10 minutes after reaching the desired pressure, the liquid transfer system is re-opened when coupling the pump 28, thereby allowing transfer of liquid to the separator 24. After 2 to 3 minutes of pumping, detaching or uncoupling the liquid transfer system. The repeated interruption of heated vapors of solvent at high pressure in the upper part of the reactor 2, acts to force out from the bottom part of the reactor 2, the remaining combination of the liquid solvent and oil. Preferably, heated vapors of solvent at elevated pressure are introduced into reactor 2, three separate times. The repeated force of the heated solvent vapors to reactor 2 acts as a vapor plug to squeeze out from the rice bran, the combination of the remaining liquid solvent and oil. Preferably, the filter system 36 at the bottom of the reactor 2, includes filters dispersed through the bottom of the reactor 2, to accelerate the recovery of the solvent and also to prevent channeling of the combination of liquid solvent and oil in the reactor. This channeling would result in an inefficient discharge of the combination of liquid solvent and oil. Preferably, the filters are removable cartridges using an outer cover with 60 mesh screen, with a polyester fiber material located within the 60 mesh screen. As illustrated in Figure 2, the filter system 32 comprises the filter cartridge 100, reinforcement body 110, inlet body 120, also mesh filter 130, perforated plate 140 and polyester fibers 150. Filter cartridge 100 has discharge nozzle 102 disposed at one end, central portion 104 and portion upper body 106. Upper body portion 106 contains internal threads 108 and projects upwardly from central body portion 104. Upper body portion 106 is adapted to be connected by internal threads 108 to external threads 112 of reinforcing body 110 and external threads 122 of the inlet body 120. The reinforcing body 110 and the inlet body 120 are substantially cylindrical. The reinforcing body 110 is housed within the input body 120, with the filter screen 130 disposed between the reinforcing portion 114 of the reinforcing body 110 and the reinforcing portion 124 of the input body 120. The input body 120 contains the perforated cover 126 around the periphery of reinforcement portion 124.

The mesh filter screen 130 is disposed between the reinforcing portions 114 and 124 of the reinforcing body 110 and the inlet body 120, respectively. Preferably, the 130 mesh filter screen comprises 60 mesh. Within the middle and upper body portions 104 and 106 of the filter cartridge 100 and within the reinforcing body 110, polyester fibers 150 are contained to filter the bran particles passing through the 60 mesh filter screen. The perforated plate 140 is disposed within the filter cartridge 100 to prevent that 150 polyester fibers migrate downstream. Preferably, the filters are inserted approximately 1.27 cm (one half inch) to the bottom of reactor 2 to relieve channeling and plugging. The purge tank 40 leading to the compressor 10 is filled with solvent vapors from the storage container 16. The outlet of the compressor 10 is directed to the filter system 36 which is inserted in the bottom of the reactor 2. The compressor 10 is operated and the pressure is allowed to build up on line 26 at about 17,575 to 18,981 Kg / cm 2 gauge (250 to 270 psig), 18.63 to 20,034 Kg / cm 2 absolute (265 to 285 psia). A valve at the bottom of the filter then opens allowing the compressed vapors to be forced rapidly through the filter and the reactor 2. Preferably the regulator 42 automatically feeds bursts of solvent vapors at 17,575 to 19,333 Kg / cm 2 (250 to 275 psig), 18.63 to 20.387 Kg / cm2 absolute (265 to 290 psia) ascending through the filter 36 to the reactor 2. This procedure is repeated three times. This procedure is a second stage in the pre-classification of material to the reactor. This second stage of the pre-classification process removes fines that accumulate in the filter during the separation of the combination of liquid solvent and oil and discards the fines inside the reactor. The bottom of the reactor 2 is made common to the discharge tank 40 of the compressor 10 with the outlet of the compressor 10 which is connected by pipe to the condenser 44. The compressor 10 removes steam from the bottom of reactor 2. The solvent vapor is then removed from the reactor. bottom of reactor 2, through compressor 10, then it is sent to condenser 44 and to the tank for storage of solvent 16, until the reactor pressure is approximately 5.976 to 6.327 Kg / cm2 gauge (85 to 90 psig), 7.03 a 7.382 Kg / cra2 absolute (100 to 105 psia). When the reactor pressure is about 5,976 to 6,327 Kg / cm 2 gauge (85 to 90 psig), 7.03 to 7,382 Kg / cm 2 absolute (100 to 105 psia), this solvent vapor from the reactor is sent to the heat exchanger 32, where it is heated between 26.67 ° and 65.56 ° C (80 and 150 ° F) and then it is directed to the upper part of the reactor through line 34 and circulates through the material in reactor 2, heating in this way and vaporizing Any traces of liquid solvent that may be trapped in the material. As the remaining liquid solvent in the material in the reactor 2 evaporates, the pressure in the reactor rises, the solvent vapors accumulate and are removed and sent to the condenser 44 to maintain the pressure range from 5,624 to 7.03 Kg / cm2 gauge (80 to 100 psig), 8.08 Kg / cm2 absolute (115 psia) in reactor 2. At the start of this recirculation of solvent vapors, the material in the upper section of the reactor is between 26.67 and 65.56 ° C (80 and 150 ° F) and the material in reactor form is between 10 and 26.67 ° C (50 and 80 ° F). The heater 46 around the circumference of the bottom half of the reactor 2, are also placed in service at this time. Hot water of 65.56 to 82.2 ° C (150 to 18? "F), is circulated through heater 46. Heater 46 acts as a barrier to maintain the heat generated by the recirculation of hot solvent vapors inside the reactor during This step of heating the material to eject the remaining traces of the liquid solvent Alternately, the reactor vessel 2 can be insulated to retain heat inside the vessel Re-circulated hot solvent vapors move down through the material in the reactor 2, heating and evaporating the remaining liquid solvent until the temperature of the material at the bottom of the reactor reaches 32.2 to 60 ° C (90 to 140 ° F). It is important to allow complete mixing of hot solvent vapors with materials in reactor 2 to ensure that cooling does not occur as solvent vapors are removed and sent to condenser 44. When the temperature at the bottom of the reactor has reached 32.2 to 60 ° C (90 to 140 ° F), all vapors are removed from the reactor and the temperatures in the top and bottom are equalized between 32.2 and 60 ° C (90 to 140 ° F) .The solvent vapors continue to be extracted from the reactor 2 until the pressure of reactor 2 is 0 Kg / cm2 (0 psig), 1.0545 Kg / cm2 absolute (15 psig) The steam recovery system is released A vacuum of 30.48 to 38.1 cm (12 to 15" ) of Hg, 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia) using a compressor or vacuum pump 10, or alternatively two compressors, reactor 2 is introduced. An inert gas is introduced from tank 12 to the bottom of the reactor 2, at a slow uniform pressure until the reactor is brought back or at 0 Kg / cm2 gauge (0 psig), 1.0545 Kg / cm2 absolute (15 psia). This inert gas is then injected to the bottom of reactor 2 in short strong bursts until positive pressure is reached from 1,406 to 1,758 Kg / cm2 (20 to 25 psig), 2.46 to 2.812 Kg / cm2 absolute (35 to 40 psia) . To reactor 2 again a vacuum of 30.48 is applied to 38. 11 cm (12 to 15") of Hg, 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia) Inert gas or dry compressed air is then introduced to the bottom of the reactor, at this time at a slow uniform pressure until The reactor is brought to 0 Kg / cm2 (0 psig) .This is the third and final stage in the pre-sorting procedure, which again scatters fines from the filter, and which also lays two fines inside the filter. reactor according to the particle size The material classified now is ready to discharge solvent-free Before general discharge of reactor 2, vacuum is introduced to reactor 2 by an upper venturi 48 and an inert gas or dry compressed air enters the bottom of the reactor at a uniform pressure of 1758 to 7.03 Kg / cm2 gauge (25 to 100 psig), 2.812 to 8.085 Kg / cm2 absolute (40 to 115 psia) through it regulator 50, while fines are extracted in the reactor top 2. After the fines are removed, s and interrupts the supply of inert gas or dry compressed air and the remaining material is evacuated from the reactor. Preferably, a venturi will be used on the top and bottom of the reactor vessel. The upper venturi 48 will engage first while introducing an inert gas or dry compressed air from 1,758 to 7,03 kg / cm 2 (25 to 100 psig), 2,812 to 8,085 kg / cm 2 absolute (40 to 115 psia) to the bottom of the reactor to remove the fines. After a pre-determined amount of time, the bottom venturi 52 will be placed in operation leaving the upper venturi 48 operating to capture the fines moving upwards during general discharge. Preferably, all the discharged material is sent to convenient classifiers 54 and 56. After all the material is evacuated from reactor 2, venturi 48 and venturi 52 and classifiers 54 and 56, are turned off. The liquid in the separator 24 contains solvent and oil. The liquid between the separator 24 is heated between 21.1 and 48.9 ° C (70 and 120 ° F) preferably between 21.1 and 37.78 ° C (70 and 100 ° F). This evaporates the solvent. The solvent vapor is removed from the separator 24 by the compressor 62 and liquefied in the condenser 44 and then sent to the storage tank 16. When substantially all the steam has been removed from the separator 24, the oil is then discharged to the holding tank of oil 64. For the process according to the invention, the material must be discarded and / or ground and / or formed into flakes or in the case of fruit (avocado, olives, coconut, etc.), deboned, dehydrated then ground and / or formed into flakes. The particle size for grinding is from a # 40 to # 325 mesh, preferably a # 100 to # 325 mesh, the particle size or flakes being from .1 mm to .4 mm, preferably .3 mm. This grinding or flaking is done to increase the total surface / volume ratio, the more contact area the particle has with a solvent, the extraction will be better. If in this case the seed of the husk is a small percentage of the total seeds, the dehusking will be omitted (for example naba). This process is also applicable to a pre-press cake. The pre-press cake is a result of a screw press extractor that is used to extract oil from material that is generally at least 20% oil-rich. The screw press, is the most common press in commercial use to extract oil from parts of plants (for example soybeans, naba, cotton seeds, peanuts, flax seed, jojoba, copra, etc). The preparation for extraction of this pre-pressed cake will involve grinding or flaking of material to a # 40 to # 325 mesh, preferably a mesh size of # 100 to # 325, or formed into .1 a. 4 mm preferably .3 mm, EXAMPLE 1 18.16 Kg (40 pounds) of raw rice bran are obtained from commercial rice mill. This raw rice bran has mesh size # 40 to # 325. This raw rice bran is milled to a minimum particle size of # 100 mesh to # 325 mesh. The ground raw rice bran is then charged to the reactor vessel 2. After air is evacuated through a vacuum, purge of inert gas and a second vacuum, the liquid solvent is introduced to the reactor through the opening 18. Additional solvent vapors are introduced to the bottom of reactor 2, to mix the rice bran in the solvent and oil combination. The combination of liquid solvent and oil is then discharged from reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the combination of liquid solvent and oil is removed from the reactor bottom. 2, until there is less than 1% remaining oil in the rice bran. The liquid is removed to reactor 2 and vapors are removed through the method described above. 14.81 kG (33 pounds) 10 ounces of defatted rice bran are removed from reactor 2 and 2.89 kg (6 pounds and 6 ounces) of oil are removed from the separator. EXAMPLE 2 18.16 Kg (40 pounds) of corn are obtained from a commercial gram mill. This corn is then ground to mesh # 100 to # 325. The ground corn is then charged to the reactor vessel 2. After air is evacuated through a vacuum, a purge of inert gas and a second vacuum, the liquid solvent is introduced to the reactor through the opening 18. Additional vapors of solvent is introduced to the bottom of the reactor 2 to mix the corn in the solvent and oil combination. The combination of liquid solvent and oil is then discharged to reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the liquid solvent oil is removed from the top of reactor 2, until There is less than 1% remaining oil in the corn. The liquid is then removed from reactor 2 and the vapors are extracted by the method described above. 16. 57 kg (36 lb. 8 oz.) Of defatted corn were removed from reactor 2 and 1,588 kg (3 lb. 8 oz.) Of oil are removed from the separator. EXAMPLE 18.16 Kg (40 pounds) of naba / canola are obtained from the cooperative extension service of a local university. This naba / canola is then ground to a # 100 to # 325 mesh. The ground naba / canola is then charged to the reactor vessel 2. After air is evacuated through vacuum, a purge of inert gas and a second vacuum, the liquid solvent is introduced to the reactor through the opening 18. Additional vapors of solvent are introduced to the bottom of the reactor 2 to mix the naba / canola in the solvent and oil combination. The combination of liquid solvent and oil is then discharged to reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the liquid solvent oil and oil are removed from the bottom of reactor 2, until that there is less than 1% remaining oil in the naba / canola. The liquid is then removed from reactor 2 and vapors are extracted through the method described above. 13.62 Kg (30 pounds) of defatted naba / canola are removed from reactor 2 and 1,588 Kg (3 pounds and 8 ounces) of oil are removed from the separator.

EXAMPLE 4 18.16 Kg (40 pounds) of soybeans are obtained from a commercial grain mill. This soy is then ground to # 100 mesh to # 325. The ground soybeans are then charged to the reactor vessel 2. After air is evacuated through a vacuum, a purge of inert gas and a second vacuum, the liquid solvent is introduced into the reactor through the opening 18. Additional vapors solvent is introduced to the bottom of the reactor 2, to mix the soy in the solvent and oil combination. The liquid solvent and oil combination is then discharged from reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the liquid solvent oil is removed, from the bottom of reactor 2, to that there is less than 1% of oil remaining in the soybeans. The liquid is then removed from reactor 2 and the vapors are extracted by the method described above. 15.06 Kg (33 pounds and 3 ounces) of defatted soy were removed from reactor 2 and 3.09 Kg (6 pounds and 13 ounces) of oil are removed from the separator. EXAMPLE 5 18.16 Kg (40 pounds) of a cardamom are obtained from a commercial gram mill. This cardamom is then ground to mesh # 100 to # 325. The ground cardamom is then charged to the reactor vessel 2. After air is evacuated through a vacuum, an inert gas purge and a second vacuum the liquid solvent is introduced to the reactor through the opening 18. Additional solvent vapors they are introduced to the bottom of the reactor 2, to mix the cardamon in the combination of solvent and oil. The combination of liquid solvent and oil is then discharged to reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the liquid solvent oil is removed from the bottom of reactor 2, until less than 1% remaining oil in the cardamon. The liquid is then removed from reactor 2 and the vapors are extracted by the method described above. 14.89 Kg (32 pounds 13 ounces) of defatted cardamom were removed from reactor 2 and 3.26 Kg (7 pounds 3 ounces) of oil are removed from the separator. EXAMPLE 6 18.16 Kg (40 pounds) of pre-pressed jojoba cake are obtained from a commercial spindle type extractor. This jojoba cake is then ground to # 100 mesh to # 325. The ground jojoba cake is then charged to the reactor vessel 2. After air is evacuated through a vacuum, an inert gas purge and a second vacuum, the liquid solvent is introduced to the reactor through the opening 18. Additional solvent vapors are introduced to the bottom of reactor 2, to mix the jojoba in the solvent and oil combination. The combination of liquid solvent and oil is then discharged from reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while removing the liquid solvent oil from the bottom of reactor 2, until there is less than 1% remaining oil in the jojoba. The liquid is then removed from reactor 2 and vapors are removed through the method described above. 16.25 Kg (35 pounds and 13 ounces) of defatted jojoba cake were removed from reactor 2 and 1.9 Kg (4 pounds and 3 ounces) of oil are removed from the separator. EXAMPLE 7 18.16 Kg (40 pounds) of pre-pressed peanut cake are obtained from a commercial spindle type extractor. This peanut cake is then ground to a # 100 to # 325 mesh. The ground peanut cake is then charged to the reactor vessel 2. After air is evacuated through a vacuum, an inert gas purge and a second vacuum, the liquid solvent is introduced to the reactor through the opening 18. Additional solvent vapors are introduced to the bottom of reactor 2, to mix the peanut cake in the combination of solvent and oil. The combination of liquid solvent and oil is then discharged from reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the liquid solvent and oil are removed from the bottom of reactor 2, until There is less than 1% remaining oil in the peanut cake. The liquid is then removed from reactor 2 and the vapors are extracted by the method described above. 16. 71 kg (36 lbs. And 13 oz.) Of defatted peanut cake were removed from reactor 2 and 1.44 kg (3 lbs. And 3 oz.) Of oil are removed from the separator. EXAMPLE 8 18.16 Kg (40 pounds) of Kenaf seed (variety of hemp) are obtained from a manufacturer of absorbers using Kenaf fibers. This kenaf is then ground to mesh # 100 to # 325. He Ground kleef is then charged to the reactor vessel 2. After air is evacuated through a vacuum, a purge of inert gas and a second vacuum the liquid solvent is introduced to the reactor through the opening 18. Additional solvent vapors are added to the reactor. enter the bottom of the reactor 2, to mix the Kenaf in the combination of solvent and oil. The solvent and oil combination is then discharged from reactor 2 and pumped to separator 24. Additional liquid solvent is pumped to the top of reactor 2, while the liquid solvent and oil are removed from the bottom of reactor 2, until There is less than 1% remaining oil in Kenaf. The liquid is then removed from reactor 2 and the vapors are extracted by the method described above. 15.18 Kg (33 pounds and 7 ounces) of defatted Kenaf seed are removed from reactor 2 and 2.98 Kg (6 pounds and 9 ounces) of oil are removed from the separator. We claim:

Claims

CLAIMS 1.- Process for extracting oil from rice bran, the process is characterized in that it comprises the steps of: loading rice bran containing rice bran oil into a reactor vessel; removing air from the reactor vessel to establish a first partial vacuum of 0.598 to 0.619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing an inert gas under pressure to discard or discharge additional air, and establishing a second partial vacuum of 0.598 to 0.619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce to the reactor vessel, a liquid solvent that has the capacity to dissolve rice bran oil, the liquid solvent is maintained at a temperature between 20 and 22.2 ° C (68 and 72 ° F), allow the liquid solvent to contact the bran of rice for a sufficient time to dissolve a substantial portion of the rice bran oil, introducing pressurized solvent vapors to the bottom of the reactor vessel, to cause mixing of rice bran in the combination of solvent and oil, thereby facilitating separation of fine particle matter of the heaviest particles in the reactor vessel, introduce solvent vapors heated under pressure in the upper part of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel, to facilitate separation of the combination of liquid solvent and oil from the reactor vessel.
2. - Process for extracting rice bran, the process is characterized in that it comprises the steps of: loading rice bran containing rice bran oil into a reactor vessel; removing air from the reactor vessel to establish a first partial vacuum of 0.598 to 0.619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing an inert gas under pressure to discard or discharge additional air, and establishing a second partial vacuum of 0.598 to 0.619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce to the reactor vessel, a liquid solvent that has solvent power for rice bran oil, the liquid solvent is maintained at a temperature between 20 and 51.67 ° C (68 and 125 ° F); allowing the liquid solvent to contact the rice bran for a sufficient time to dissolve a substantial portion of the rice bran oil; introducing pressurized solvent vapors to the bottom of the reactor vessel, to cause mixing of rice bran in the solvent and oil combination, thereby facilitating the separation of fine particulate matter into the heavier particles in the reactor vessel; introducing solvent vapors heated under pressure into the upper part of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel, to facilitate separation of the combination of liquid solvent and oil from the reactor vessel.
3. - Process for extracting rice bran oil, the process is characterized in that it comprises the steps of: loading rice bran containing oil into a reactor vessel; remove air from the reactor vessel to establish a first partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce an inert gas under pressure to discard or discharge additional air, and establish a second partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce the reactor vessel, a liquid solvent that has the ability to dissolve rice bran oil, the liquid solvent is maintained at a temperature between 20 and 22.2 ° C (68 and 72"F); allowing the liquid solvent to contact the rice bran for a sufficient time to dissolve a substantial portion of the rice bran oil; introducing pressurized solvent vapors to the bottom of the reactor vessel to cause mixing of rice bran in the solvent and oil combination, thereby facilitating separation of the fine particle matter from the heavier particles in the reactor vessel; introducing solvent vapors heated under pressure to the top of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel, to facilitate the separation of the liquid solvent and oil combination from the reactor vessel; Transfer the solvent and rice bran oil combination from the reactor vessel to a separating vessel and then evaporate the solvent inside the reactor vessel at a temperature sufficient to cause solvent vaporization, while avoiding denaturing of the constituent components of the bran oil. of rice .
4.- Procedure in accordance with the claim 3, characterized in that it further comprises the steps of: removing substantially all of the remai solvent from the reactor vessel by introducing vapor of the heated solvent to the top of the reactor vessel to increase the reactor pressure between 2,812 and 5,624 Kg / cm2 absolute (40 and 80) .psy), withdrawing liquid through the bottom of the reactor vessel, and repeat the stage of introducing hot steam twice and separating liquid.
5. Method according to claim 3, characterized in that it also comprises the steps of: forcing solvent vapor between 18,629 to 20.04 Kg / cra2 absolute (265 and 285 psia), to the bottom of the reactor vessel through a filter in a short burst and repeat the stage of forcing solvent vapor twice.
6. Method according to claim 5, characterized in that it further comprises the steps of: reducing the reactor pressure to between 7.03 and 7.382 absolute (100 and 105 psia), thus allowing heated solvent vapors to be removed without causing Freezing of solvent vapors.
7. - Procedure in accordance with the claim 6, characterized in that it also comprises the steps of: removing steam through the bottom of the reactor vessel, heating steam between 26.67 and 65.56"C (80 and 150" F) and introducing heated steam through the upper part of the reactor vessel, vaporizing in this way traces of liquid solvent remai in the reactor vessel.
8.- Procedure in accordance with the claim 7, characterized in that it further comprises the steps of: removing steam through the bottom of the reactor vessel, condensing the removed vapor, and transferring the condensed solvent to a storage vessel.
9.- Procedure in accordance with the claim 8, characterized in that it further comprises the steps of: introducing an inert gas into the reactor vessel to increase the reaction to 1.0545 Kg / cm 2 absolute (15 psia) force inert gas into the reactor vessel in repeated bursts to increase the reactor pressure between 2.46 and 2,812 Kg / cm2 absolute (35 and 45 psia) and remove the inert gas from the reactor vessel to reduce the pressure to between 0.598 and 619 Kg / cm2 absolute (8.5 and 8.8 psia).
10. Method according to claim 8, characterized in that it further comprises the steps of: discharging residual rice bran from the reactor vessel by means of an upper venturi, while dry compressed air is introduced to the bottom of the reactor vessel between 2.812 and 8.085 Kg / cm2 absolute (40 and 115 psia).
11. Method according to claim 10, characterized in that it further comprises the steps of: discharging rice bran from the bottom of the reactor vessel by means of a bottom venturi.
12. Process for extracting oil from plant material contai oil, the process is characterized in that it comprises the steps of: placing plant material contai oil selected from a group consisting of rice bran, corn, naba / canola, soybeans , cardamom, pre-pressed peanut cake, pre-pressed jojoba cake and Kenaf; removing air from the reactor vessel to establish a first partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing an inert gas under pressure to discard or discharge additional air, and establishing a second partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce the reactor vessel, a liquid solvent that has the ability to dissolve oil from plant material, the liquid solvent is maintained at a temperature between 20 and 22.2 ° C (68 and 12 ° T); allowing the liquid solvent to contact the plant material for a sufficient time to dissolve a substantial portion of the plant material oil; introducing pressurized solvent vapors to the bottom of the reactor vessel, to cause mixing of rice bran in the solvent and oil combination, thereby facilitating separation of fine particle matter from the heavier particles in the reactor vessel; introducing solvent vapors heated under pressure into the upper part of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel; transferring the solvent and oil combination of plant material from the reactor vessel to a separator vessel and then evaporating the solvent into the reactor vessel at a temperature sufficient to cause vaporization of the solvent while avoiding denaturation of the constituent components of the plant oil.
13. Method according to claim 12, characterized in that it also comprises the steps of: removing substantially all the remaining solvent to the reactor vessel by introducing steam of the heated solvent to the upper part of the reactor vessel to increase reactor pressure between 2,812 and 5,624. Kg / cm2 absolute (40 and 80 psia), remove liquid through the bottom of the container, and repeat the stage of introducing hot steam twice and remove liquid.
14.- Procedure in accordance with the claim 3, characterized in that it also comprises the steps of: forcing solvent vapor between 18,629 to 20.04 Kg / cma absolute (265 and 285 psia), to the bottom of the reactor vessel through a filter in a short burst and repeating the step of forcing twice solvent vapor.
15. - Method according to claim 14, characterized in that it further comprises the steps of: reducing the reactor pressure to between 7.03 and 7.382 kg / cm2 absolute (100 and 105 psia), thus allowing heated solvent vapors to be removed, without causing freezing of solvent vapors.
16. Process according to claim 6, characterized in that it also comprises the steps of: removing steam through the bottom of the reactor vessel, heating steam between 26.67 to 65.56 ° C (80 to 150 ° F) and introducing heated steam through from the upper part of the reactor vessel, thereby vaporizing traces of liquid solvent remaining in the reactor vessel.
17. Process for extracting oil from plant material containing oil, the process comprises the steps of: loading plant material containing oil, selected from the group consisting of part of plants containing oil that can be ground into particles between mesh # 100 and # 325 in a reactor vessel; remove air from the reactor vessel to establish a first partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing an inert gas under pressure to discard or discharge additional air, and establishing a second partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce into the reactor vessel, a liquid solvent that has the ability to dissolve oil from plant material, the liquid solvent is maintained at a temperature between 20 and 22.2 ° C (68 and 72 ° F), allow the liquid solvent to contact the plant material for a sufficient time to dissolve a substantial portion of the oil from plant material, introduce pressurized solvent vapors to the bottom of the reactor vessel to cause mixing of rice bran in the combination of liquid solvent and oil, thereby facilitating separation of fine particulate matter the heaviest particles in the reactor vessel, transfer the solvent and oil combination of plant material from the reactor vessel to a separator vessel and then evaporate the solvent into the separator vessel at a temperature between 21.1 and 48.89 ° C (70 and 120 ° F), thus avoiding the denaturation of the constituent components of the oil. 8.- Procedure in accordance with the claim 17, characterized in that it also comprises the steps of: removing substantially all of the remaining solvent from the reactor vessel, by introducing steam from the heated solvent to the upper part of the reactor vessel to increase the reactor pressure between 2,812 and 5,624 Kg / cm2 absolute (40 and 80 psia), withdrawing liquid through the bottom of the container and repeating the stage of introducing hot steam twice and separating liquid. 19.- Procedure in accordance with the claim 18, characterized in that it also comprises the steps of: forcing solvent vapor between 18,629 to 20.04 Kg / cm2 absolute (265 and 285 psia), to the bottom of the reactor vessel through a filter in a short burst and repeating the step of forcing twice solvent vapor. 20. Method according to claim 19, characterized in that it also comprises the steps of: reducing the pressure of the reactor to between 7.03 and 7.382 Kg / cm2 absolute (100 and 105 psia), thus allowing solvent vapors to be removed heated, without causing freezing of solvent vapors. 21.- Procedure in accordance with the claim 20, characterized in that it further comprises the steps of: removing steam through the bottom of the reactor vessel, heating steam between 26.67 and 65.56 ° C (80 and 150 'F) and introducing heated steam through the upper part of the reactor vessel, vaporizing in this way traces of liquid solvent remaining in the reactor vessel. 22. Procedure in accordance with the claim 21, characterized in that it further comprises the steps of: removing steam through the bottom of the reactor vessel, condensing the removed vapor, and transferring the condensed solvent to a storage vessel. 23.- Procedure in accordance with the claim 22, characterized in that it also comprises the steps of: introducing an inert gas into the reactor vessel, to increase the reaction to 1.0545 Kg / cm2 absolute (15 psia) force inert gas into the reactor vessel in repeated bursts to increase the reactor pressure between 2.46 and 2,812 Kg / cm2 absolute (35 and 40 psia) and remove the inert gas from the reactor vessel to reduce the pressure to between 0.598 to 619 Kg / cm2 absolute (8.5 and 8.8 psia). 24. Procedure for extracting oil from plant material containing oil, the process is characterized in that it comprises the steps of: depositing a plant material containing oil in a reactor vessel; removing air from the reactor vessel to establish a vacuum; introducing a suitable liquid solvent to dissolve oil in the plant material containing oil in the reactor vessel, the liquid solvent is kept at a temperature sufficient to cause the liquid solvent to dissolve the oil from the plant material containing oil, while avoiding denaturing the constituent components of the oil and the plant material containing oil; allowing the liquid solvent to contact the plant material containing oil for a sufficient time to dissolve a substantial portion of the oil; introducing the solvent vapors under pressure into the bottom of the reactor vessel to cause mixing in the plant material in the combination of solvent and oil, thereby causing separation of the material from the fine particles of the heavier particles; and introducing solvent vapors heated under pressure to the top of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel. 25.- Procedure in accordance with the claim 24, characterized in that it also comprises the steps of: providing at least one filter device at the bottom of the reactor vessel and for forcing solvent vapors under pressure through the filter device to the bottom of the reactor vessel, to remove the fine particulate matter that accumulates in the filter during separation of the combination of liquid solvent and oil. 26.- Procedure in accordance with the claim 25, characterized in that the filter device comprises a hollow body having an upper portion that is provided with internal threads and a bottom portion that is provided with a discharge opening; an inlet body comprising an annular plate adapted for threadable engagement with the upper portion, a perforated cover which is supported by a reinforcing layer and firmly connects to the annular plate; a sieve mesh filter housed inside the entrance body; a perforated plate mounted within the hollow body a distance from the discharge opening; and a fibrous filter material placed between the perforated plate and the mesh filter screen. 27.- Filtering device, comprising: a hollow body having an upper portion that is provided with internal threads and a bottom portion that is provided with a discharge opening; an inlet body comprising an annular plate adapted for threaded engagement with the upper portion and a perforated cover supported by a reinforcing layer, the cover is fixedly connected to the annular plate; a sieve mesh filter housed inside the entrance body; a perforated plate mounted within the hollow body, a distance from the discharge opening; and a fibrous filter material that is placed between the perforated plate and the mesh filter screen. 28.- Process for extracting oil from rice bran, the process is characterized in that it comprises the steps of: loading rice bran containing the rice bran oil into a reactor vessel; removing air from the reactor vessel to establish a first partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing an inert gas under pressure to discard or discharge additional air, and establishing a second partial vacuum of 0.598 to 619 Kg / cm absolute (8.5 to 8.8 psia); introducing into the reactor vessel, a liquid solvent having the capacity to dissolve rice bran oil, the liquid solvent is maintained at a temperature between 20 and 51.67 ° C (68 and 125 ° F); allowing the liquid solvent to contact the rice bran for a sufficient time to dissolve a substantial portion of the rice bran oil; introducing pressurized solvent vapors to the bottom of the reactor vessel, to cause mixing of rice bran in the solvent and oil combination, thereby facilitating separation of fine particle matter from the heavier particles in the reactor vessel; introducing solvent vapors heated under pressure into an upper part of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel, to facilitate separation of the liquid solvent and oil combination from the reactor vessel; Transfer the solvent and rice bran oil combination from the reactor vessel to a separating vessel and then evaporate the solvent inside the reactor vessel at a temperature sufficient to cause solvent vaporization, while avoiding denaturing of the constituent components of the bran oil. of rice. 29.- Process for extracting oil from plant material containing oil, the process is characterized in that it comprises the steps of: placing plant material containing oil selected from the group consisting of rice bran, corn, naba / canola, soybeans, cardamom, pre-pressed peanut cake, pre-pressed jojoba cake and Kenaf; removing air from the reactor vessel to establish a first partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce an inert gas under pressure to discard or discharge additional air, and establish a second partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introduce in the reactor vessel, a liquid solvent that has the ability to dissolve oil from plant material, the liquid solvent is maintained at a temperature between 20 and 51.67"C (68 and 125 ° F), allow the liquid solvent to contact the plant material for a sufficient time to dissolve a substantial portion of the plant material oil, introduce pressurized solvent vapors to the bottom of the reactor vessel, to cause mixing of plant material in the solvent and oil combination, thereby facilitating separation of fine particle matter of the heaviest particles in the reactor vessel, introduce solvent vapors heated under pressure in an upper part of the reactor vessel, while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel, to facilitate separation of the combination of liquid solvent and oil from the reactor vessel, transfer the combination of solvent and oil of plant material from the reactor vessel to a separator vessel and then vaporizing the solvent into the separator vessel at a temperature sufficient to cause evaporation of the solvent while preventing the denaturing of the constituent components of the plant oil. 30.- Process for extracting oil from plant material containing oil, the process is characterized in that it comprises the steps of: loading plant material containing oil selected from the group consisting of part of plants containing oil that can be ground into particle size between # 100 mesh and # 325 in a reactor vessel; remove air from the reactor vessel to establish a first partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing an inert gas under pressure to discard or discharge additional air, and establishing a second partial vacuum of 0.598 to 619 Kg / cm2 absolute (8.5 to 8.8 psia); introducing into the reactor vessel, a liquid solvent having solvent power for plant material oil, the liquid solvent is maintained at a temperature between 20 and 51.67 ° C (68 and 125 ° F); allowing the liquid solvent to contact the plant material for a sufficient time to dissolve a substantial portion of the plant material oil; introducing solvent vapors heated under pressure into an upper part of the reactor vessel while the combination of liquid solvent and oil is removed from the bottom of the reactor vessel; transfer the solvent-oil combination of plant material from the reactor vessel to a separator vessel and then evaporate the solvent into the separator vessel at a temperature between 21.1 and 48.89 ° C (70 and 120 ° F), thereby avoiding denaturation of the constituent components of the oil.