WO2014115067A1 - Method for obtaining soybean protein concentrate from soy meal by means of extraction with alcohol, obtaining a high-protein flour without antinutritional factors and a high-quality oil - Google Patents

Method for obtaining soybean protein concentrate from soy meal by means of extraction with alcohol, obtaining a high-protein flour without antinutritional factors and a high-quality oil Download PDF

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Publication number
WO2014115067A1
WO2014115067A1 PCT/IB2014/058325 IB2014058325W WO2014115067A1 WO 2014115067 A1 WO2014115067 A1 WO 2014115067A1 IB 2014058325 W IB2014058325 W IB 2014058325W WO 2014115067 A1 WO2014115067 A1 WO 2014115067A1
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WIPO (PCT)
Prior art keywords
ethanol
oil
carbohydrates
water
molasses
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PCT/IB2014/058325
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Spanish (es)
French (fr)
Inventor
Mario Domingo ALLOCCO
Mariana Carla ALLOCCO
Luis Eduardo Palacios
Mirta Bernarda GUALA
Original Assignee
Allocco Mario Domingo
Allocco Mariana Carla
Luis Eduardo Palacios
Guala Mirta Bernarda
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Application filed by Allocco Mario Domingo, Allocco Mariana Carla, Luis Eduardo Palacios, Guala Mirta Bernarda filed Critical Allocco Mario Domingo
Publication of WO2014115067A1 publication Critical patent/WO2014115067A1/en

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Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/14—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from leguminous or other vegetable seeds; from press-cake or oil-bearing seeds
    • A23J1/142—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from leguminous or other vegetable seeds; from press-cake or oil-bearing seeds by extracting with organic solvents
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J3/00—Working-up of proteins for foodstuffs
    • A23J3/14—Vegetable proteins
    • A23J3/16—Vegetable proteins from soybean
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J7/00—Phosphatide compositions for foodstuffs, e.g. lecithin
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L11/00—Pulses, i.e. fruits of leguminous plants, for production of food; Products from legumes; Preparation or treatment thereof
    • A23L11/05—Mashed or comminuted pulses or legumes; Products made therefrom
    • A23L11/07—Soya beans, e.g. oil-extracted soya bean flakes
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L11/00—Pulses, i.e. fruits of leguminous plants, for production of food; Products from legumes; Preparation or treatment thereof
    • A23L11/30—Removing undesirable substances, e.g. bitter substances
    • A23L11/32—Removing undesirable substances, e.g. bitter substances by extraction with solvents
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/02—Pretreatment
    • C11B1/04—Pretreatment of vegetable raw material
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/10—Production of fats or fatty oils from raw materials by extracting

Definitions

  • the present invention is related to the processes of preparation, oil extraction and protein concentration from soybeans with a new process route for treatment, replacing the hexane solvent with alcohol (ethanol) in the oil extraction, obtaining phospholipids and carbohydrates, using a fixed floor rotary extractor with special design, separating the soybean oil from the solvent by a non-distillation process, separating and fermenting the molasses formed by carbohydrates to obtain ethanol, with or without prior extraction of isoflavones, separating the phospholipids insolubilized in the oil and obtaining soy flour concentrated in protein free of anti-nutritional factors.
  • ethanol alcohol
  • Soy production is of relevant importance in Argentina and other countries of the world and is the source of obtaining valuable products for human and animal consumption.
  • Two of the most important products obtained are oils and flours. While both products can be consumed by humans, the main use of soy flour is as a component for animal feed.
  • Soy flour has high-value proteins and has proven to be an ideal source of essential amino acids used by animals to build / compose the proteins necessary for the nutrition of their tissues.
  • soybean meal contains a small amount of oil and soluble sugars, produced in efficient economic conditions, to be used in a wide variety of foods.
  • this intermediate deolventization step is not required, therefore in a single equipment the extraction of oil with ethanol is carried out and then the extraction of carbohydrates with ethanol-water mixture and a single stage of final deolventized instead of the two required by the conventional process.
  • Soy beans are received from the producer and properly stored in silos.
  • the stages of the process include cleaning, peeling and cracking, rolling, expanded as a possible alternative and then extraction with ethanol by means of a rotary extractor that allows the operation of countercurrent extraction of the oil with ethanol (embedding, percolation and runoff) ) and then embedded with ethanol and water solution (flood) and countercurrent extraction of carbohydrates with ethanol and water solution (percolation and runoff).
  • the oil-ethanol stream is cooled to less than 25 ° C, preferably between 15 and 25 ° C, causing the precipitation of 97% of the oil contained in the solution, the ethanol is separated from the oil by a centrifuge, returning to the process with a minimum of residual oil.
  • the separated oil with very low ethanol content then passes through a column under vacuum, working at a pressure of 50/200 mmHg at 95/105 ° C with a 0.5 / 1% weight by weight stripping steam (bubbling ), where traces of ethanol are removed and then passed through a dryer, obtaining a high quality product ready for commercialization.
  • the ethanol-carbohydrate stream is processed in a series of conventional evaporators, where a solution with an average composition of 60% ethanol-40% water is recovered, preferably a solution 40% ethanol - 60% water, more preferably 55% ethanol - 45% water, which returns to the process, obtaining a concentrate of sugars, called molasses.
  • the flowchart of Figure 1 has optionally included the recovery of isoflavones as a possible alternative and of residual molasses that are fermented according to the traditional method, with yeasts of the Saccharomyces type
  • the ethanol solution obtained is rectified in a dish distillation column that includes the drying stage and then used to feed the process.
  • the solid stream passes through a final stage of de -venting where the remaining ethanol evaporates at a temperature of 90/1 00 ° C until its remaining ethanol content is reduced below 500 ppm and then passes through a cooling equipment, where finally a temperature below 40 ° C is reached. Since only ethanol and dilutions in ethanol water are used, the intermediate deolventization step is not required as is the case if hexane was used in the first stage and then another solvent.
  • the material Before storage, the material goes through a system of mills and screens to regulate the particle size of the protein-concentrated soybean meal (SPC).
  • SPC protein-concentrated soybean meal
  • the object of the present invention is a process for obtaining concentrated soy protein and high quality oils, which unlike the traditional method, is done in a single extractor and comprises the following steps:
  • the previous stage (F) may or may not include the separation of isoflavones from molasses prior to fermentation.
  • the present invention is a process for obtaining concentrated soy protein and high quality oils, which unlike the traditional method, is made in a single extractor and comprises the following steps:
  • stage B Embedding and expansion of the soy material obtained in stage A with a solution of ethanol and oil, with approximately 20% oil.
  • stage B obtained in stage B by percolation of ethanol and mixtures (miscelles) of ethanol-oil of decreasing concentrations in countercurrent through the soy material;
  • stage C Embedding and expansion of the solid soy material obtained in stage C with a mixture of ethanol-water and carbohydrates, which contains up to 5% carbohydrates.
  • step C obtained in step C by a non-distillative method
  • stage F conditioning of the ethanol obtained in stage F for reuse in a closed cycle
  • step E separation of the carbohydrates from the ethanol-water from the carbohydrates-ethanol-water solution obtained in step E obtaining molasses and ethanol that returns to the process;
  • step J the isoflavones can be separated from the molasses prior to fermentation;
  • the preparation must meet the same premises that are used for a traditional soybean processing facility.
  • the first step is a cleaning stage to remove impurities, which consists of a system of sieves, screens and multi-vacuum cleaners.
  • the expanded material will be cooled to 70 oC and will enter a dual rotary extractor, whose unique design allows in the same equipment to do the embedding / soaking and the extraction of oil with ethanol and the embedding and extraction of carbohydrates with ethanol-water.
  • the extractor has a circular shape and has five well defined areas:
  • the working temperature is between 70/80 oC.
  • the residence time of the embedded is a 10/17 minute stay, preferably an 18/25 minute stay, more preferably a 15 minute stay.
  • the working temperature is 70 oC and between 4 and 5 tons of ethanol solution are used per ton of flour to be processed, according to the specifications of the product to be obtained. • Drainage zone with differential vacuum or gravimetric runoff to separate the remaining liquid in the material.
  • the evaporated ethanol vapors are condensed and the remaining gases are sucked through a gas scrubber by means of a centrifugal fan or a steam ejector.
  • the hot oil-ethanol mixture leaves the extractor at a temperature of between 70/80 ° C and is cooled to less than 25 ° C, preferably between 1 and 25 ° C, producing the separation of oil, ethanol and solids.
  • Figure 2 shows the Solubility Curve of soybean oil in ethanol as a function of temperature.
  • the oil and solids feed a decanter-type centrifuge in which the solids are separated from the oil and once dried, they are sold as lecithin.
  • the oil is sent to a stripper to remove the remaining ethanol, obtaining a high quality degummed oil.
  • Vapors from the stripper and the flour desolventizer / dryer are condensed and returned to the process.
  • the carbohydrates (molasses) of the ethanol / water mixture are extracted with 1 to 5% solids that leaves the extractor.
  • This mixture enters a system of conventional evaporators at 70/80 ° C under vacuum in which the ethanol that returns to the process is recovered and the molasses is concentrated to 10% solids.
  • This stream enters a distillation tower, which works at 85 ° C where the remaining ethanol is recovered, draining a molasses solution with 30% solids at the bottom, which is cooled to approximately 35 ° C and sent to the fermentation plant.
  • the ethanol-water-carbohydrate solution is subjected to an evaporation process at 70/80 ° C under vacuum, where a solution of 55/65% ethanol- 35/45% water is recovered that returns to the process after going through a Conventional distillation column to obtain the necessary portion of pure ethanol to feed the oil extraction process in the first stage and its dilutions with water for the extraction of carbohydrates in the second stage, obtaining a sugar solution called molasses, the ethanol solution obtained is rectified by distillation and used to feed the process, the molasses solution is concentrated to approximately 1.0% solids and distilled at an approximate temperature of 85 ° C where the remaining ethanol that returns to the process is recovered, obtaining a molasses with about 30% solids that is cooled to about 35 ° C and fermented to obtain ethanol.
  • the extraction of the isoflavones contained in the molasses can be carried out taking advantage of the low solubility of these compounds at low temperature and acidic pH, the molasses solution is brought to pH 4.5 and cooled to less than 5 ° C, precipitating more than 95% of the isoflavones. If the isoflavones are separated, the residual molasses must be reheated to approximately 35 ° C to proceed to fermentation.
  • the extraction of the isoflavones contained in the molasses can be carried out.
  • the average isoflavone content in molasses is as follows:
  • the molasses solution is brought to pH 4.5 and cooled to less than 5 ° C, precipitating more than 95% of the isoflavones
  • the following graph shows the solubility of isoflavone called Genistein in water as a function of temperature.
  • Figure 3 shows the solubility of Isoflavone Genistein in water as a function of temperature.
  • the precipitate is separated by filtration or centrifugation, obtaining a product enriched in isoflavones (between 5 and 10% concentration) that can be marketed in that form or subjected to subsequent purifications and / or enzymatic treatments to obtain isoflanovas in its conjugate or agluconas mode. .
  • composition of the molasses carbohydrates are:
  • the sugar content in Molasses with 30% solids is 16%.
  • Molasses sugar can be fermented by the traditional method to obtain ethanol.
  • the molasses is mixed with yeasts and kept at pH between 3.5 and 4 for 8/12 hours at room temperature (35 ° C).
  • the extractor is of rotary type, divided into uniform radial cells, which has the particularity that when completing a total 360 ° rotation, it performs the operations of feeding soybean sheets to the extractor, embedded / soaking with a mixture of ethanol and concentrated oil in oil, oil extraction in countercurrent, solvent drainage, soaking / soaking of the degreased flour with ethanol solution and water with 1 to 5% solids (molasses), sugar extraction in countercurrent with alcohol and water solution, drainage of the solids extracted with the ethanol-water solution and discharge of the concentrated protein flour.
  • the equipment has embedded areas that work by flooding and are achieved through blind floors, percolation areas, where the ethanol used for extraction drains (percolates) through the material through perforated / grooved floors, extracting oil in the first stage and sugars in the second stage and other drainage areas that also have perforated or grooved floors and allow excess liquids to drain from solids.
  • the drainage areas may have a vacuum in the lower compartment to improve the runoff of solids, although this solution is optional and may or may not be used.
  • the equipment is designed to maintain specific residence times in each section:
  • the principle is backwashing, that is to say that the material moves in one direction and is being washed by solutions with lower oil concentrations or molasses as it approaches the final stage of each process, allowing to maintain concentration gradients that allow extract both oil and molasses.
  • the flood zones are intended to cause the embedding of the material and its expansion.
  • the extractor cells in the embedded areas can be fed with solution both from below through the floor and from the top as is done in other parts of the extractor.
  • the flour is dosed on the cells flooded with the solution of ethanol and oil, which allows to avoid an excessive compaction of the material, obtaining a mass of porous composition that allows very good percolation (drainage) of ethanol through the bed of flour, with a very high degree of oil removal efficiency.
  • This solution of pumping the ethanol-oil and ethanol-water miscelles through the perforated floor to remove the material in process and achieve better percolation can also be used as an option in the backwash stages.
  • backwashing the concentrations of the products extracted by the solvents used in each stage go in the opposite direction to the concentrations of those products in the solids being washed.
  • the final wash is always done with a pure liquid mixture that is, oil-free ethanol in the first stage and water-free ethanol-water in the second.
  • concentrations of the products to be extracted from the solids go in the opposite direction to those of the liquid mixtures used to extract them, thus maintaining the concentration gradients that allow the extraction of oils and molasses.
  • concentration gradients that allow the extraction of oils and molasses.
  • the process begins with the entry of soybean sheets to the extractor on a cell flooded with a concentrated mixture of ethanol-oil and then several washes are carried out with ethanol mixture decreasing oil in percolation cells until the final wash with 99% pure ethanol of concentration, which allows to extract the fatty matter from the soybean sheet up to a residual less than 1%.
  • the next step is a draining cell to drain the solvent and then the solids enter a flood cell where the already defatted material is contacted with the ethanol-water solution, consisting of 60% ethanol and 40% water, preferably by a composition 80% ethanol and 20% water weight by weight, more preferably by a composition 70% ethanol and 30% water weight by weight, where the expansion of the material occurs by hydration.
  • the ethanol-water solution consisting of 60% ethanol and 40% water, preferably by a composition 80% ethanol and 20% water weight by weight, more preferably by a composition 70% ethanol and 30% water weight by weight, where the expansion of the material occurs by hydration.
  • the material enters a draining cell to drain the ethanol-water solution and passes into a dewatering pressing system where most of the remaining solvent is extracted.
  • the product enters a shredder to homogenize the size of the particles of the solid material and feed the desolventizer equipment.
  • This stage of dewatering and shredding may not be used, in that case from the drainage stage the material directly enters the desolventization stage which can be conventional or rotary tubes.
  • the product is dried by a system of rotary tube dryers that allows to avoid thermal damage on the protein, obtaining a concentrated soybean meal of excellent organoleptic and nutritional quality.
  • the ethanol-oil solution of the first stage and the ethanol-water-sugar solution of the second stage are recovered in differentiated circuits each having different treatment.
  • EXAMPLE 1 Obtaining Concentrated Soy Protein (SPC) from Soy Beans.
  • the pre-cleaning stage was started and then the beans were heated to a temperature of between 60/65 ° entering the shelling stage, where the bean was split and the shell was separated, by aspiration with countercurrent air.
  • the separated shell was ground and pelletized, obtaining 70 kg of shell pellet.
  • the shelled bean was laminated using special rollers, obtaining 0.35 / 0.45 mm thick sheets.
  • the ethanol used comes from the first stage and from the distillation / recovery system already described.
  • the ethanol-oil miscel was cooled to 25 ° C, separating the precipitated oil by differential of oil solubility in ethanol depending on the temperature and the hydrated lecithins insolubilized in the oil and separated by centrifugation.
  • the ethanol-sugar miscel was concentrated by the total evaporation of ethanol and part of the water in an evaporator, until obtaining a concentration of approximately 30% solids. Vapors condensed and returned to the process.
  • the process described in the Laboratory was simulated, using a pilot scale model.
  • the prototype was fed with soybeans and subjected to an extraction with pure ethanol in the first stage and with 70% ethanol solution and 30% water in the second, both in countercurrent.
  • the fat in the flour decreased from 23.55% to 0.31% in 6 washes.
  • Oligosaccharides Max 1%
  • Trypsin Inhibitor Max. 5000 TIU / g of product
  • the present invention is applicable throughout the food industry, both for human and animal nutrition.
  • Concentrated Soy Proteins SPC have an important potential in the field of aquaculture, due to the high concentration of proteins and the lack of anti-nutritional compounds.
  • the oil extraction process has less energy costs than the original, since the oil recovery is Non-Distillative.
  • a renewable solvent such as ethanol is used, which is obtained from the fermentation of molasses, so the process not only supplies itself with ethanol, but also generates a surplus for sale.
  • the ethanol generated has a high percentage of isoflavones, of increasing medicinal use, which generates an additional source of income.
  • the oil obtained is already degummed (it contains a very low amount of phosphorus) and has a low color because it is obtained at low temperatures, which makes it a Premium product.

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Abstract

The invention relates to a method for producing a soybean protein concentrate (SPC) flour having a low quantity of soluble carbohydrates and a reduced quantity of oil, comprising the use of ethanol as the only solvent and aqueous solutions of same, which does not require distillation in order to separate the oil, and in which the soybean protein concentrate (SPC) is obtained using a single solvent-removal heat treatment. The method comprises the following steps of: A. preparing the soybeans for treatment involving cleaning, grinding and de-hulling, separating the hull and milling the de-hulled soybeans, thereby obtaining a milled soybean material; B immersing and expanding the soybean material obtained in step A with a solution of ethanol and oil, containing approximately 20 % oil; C. using ethanol to extract oils and phospholipids from the soybean material obtained in step B by reverse-flow percolation of the ethanol and the mixtures (miscellas) of ethanol/oil with decreasing concentrations through the soybean material; D. immersing and expanding the solid soybean material obtained in step C with a mixture of ethanol/oil and carbohydrates, containing up to 5 % carbohydrates; E. using ethanol/water to extract the carbohydrates from the defatted soybean material obtained in step C by reverse-flow percolation of ethanol/water and the mixtures of ethanol/water/carbohydrates with decreasing concentrations through the defatted soybean material; F. separating the soybean oil from the ethanol in the ethanol/oil solution obtained in step C using a non-distillation method; G. conditioning the ethanol obtained in step F for re-use in a closed loop; H. separating the phospholipids and other impurities from the oil obtained in step F; I. separating the carbohydrates from the ethanol/water of the carbohydrates/ethanol/water solution obtained in step E, thereby obtaining molasses and ethanol that is returned to the process; J. separating, concentrating and fermenting the molasses formed by the carbohydrates obtained in step I in order to produce ethanol; K optionally in step J, separating the isoflavones from the molasses prior to fermentation; L. obtaining soybean protein concentrate (SPC) that is free of antinutritional factors and suitable for human and animal consumption, and producing soybean isolates. According to the invention, the only solvent used is pure ethanol and solutions in water and the process is performed without an intermediate solvent-removal step.

Description

"PROCESO PARA OBTENER PROTEINAS CONCENTRADAS DE SOJA A PARTIR DEL POROTO MEDIANTE LA EXTRACCION CON ALCOHOL, OBTENIENDOSE UNA HARINA DE ALTA PROTEINA SIN FACTORES ANTINUTRICIONALES Y UN ACEITE DE ALTA CALIDAD" Campo de la invención  "PROCESS FOR OBTAINING CONCENTRATED PROTEINS OF SOYBEAN FROM THE POROTO BY EXTRACTION WITH ALCOHOL, OBTAINING A HIGH PROTEIN FLOUR WITHOUT ANTI-NUTRITIONAL FACTORS AND A HIGH QUALITY OIL" Field of the invention
La presente invención está relacionada con los procesos de preparación, extracción de aceite y concentración de proteína a partir del poroto de soja con una nueva ruta de proceso para su tratamiento, reemplazando el solvente hexano por alcohol (etanol) en la extracción de aceite, obteniendo fosfolípidos y carbohidratos, utilizando un extractor rotativo de piso fijo con diseño especial, realizando la separación del aceite de soja del solvente mediante un proceso no destilativo, separando y fermentando las melazas formadas por los hidratos de carbono para obtener etanol, con o sin extracción previa de isoflavonas, separando los fosfolípidos insolubilizados en el aceite y obteniendo harina de soja concentrada en proteína libre de factores antinutricionales.  The present invention is related to the processes of preparation, oil extraction and protein concentration from soybeans with a new process route for treatment, replacing the hexane solvent with alcohol (ethanol) in the oil extraction, obtaining phospholipids and carbohydrates, using a fixed floor rotary extractor with special design, separating the soybean oil from the solvent by a non-distillation process, separating and fermenting the molasses formed by carbohydrates to obtain ethanol, with or without prior extraction of isoflavones, separating the phospholipids insolubilized in the oil and obtaining soy flour concentrated in protein free of anti-nutritional factors.
Antecedentes de la Invención  Background of the Invention
La producción de soja, es de una importancia relevante en Argentina y otros países del mundo y es la fuente de obtención de valiosos productos para consumo humano y animal. Dos de los más importantes productos obtenidos son los aceites y las harinas. Si bien ambos productos pueden ser consumidos por seres humanos, el uso principal de las harinas de soja es como componente para alimentos balanceados para animales. Las harinas de soja tienen proteínas de alto valor y han probado ser una fuente ideal de aminoácidos esenciales usados por los animales para construir/componer las proteínas necesarias para la nutrición de sus tejidos.  Soy production is of relevant importance in Argentina and other countries of the world and is the source of obtaining valuable products for human and animal consumption. Two of the most important products obtained are oils and flours. While both products can be consumed by humans, the main use of soy flour is as a component for animal feed. Soy flour has high-value proteins and has proven to be an ideal source of essential amino acids used by animals to build / compose the proteins necessary for the nutrition of their tissues.
Existen procesos bien conocidos para extraer el aceite de las semillas y obtener harina de soja desgrasada que mantiene el contenido original de carbohidratos solubles del poroto de soja. There are well-known processes to extract oil from seeds and obtain defatted soybean meal that maintains the original soluble carbohydrate content of soybeans.
Estos carbohidratos pueden causar problemas gástricos en carnívoros y animales jóvenes en general. Un ejemplo de esto es el efecto negativo que los carbohidratos no-metabolizables causan en el crecimiento y la salud de los peces en acuacultura, por ejemplo, Salmones y Truchas.  These carbohydrates can cause gastric problems in carnivores and young animals in general. An example of this is the negative effect that non-metabolizable carbohydrates cause on the growth and health of fish in aquaculture, for example, Salmon and Trout.
Además, la baja concentración proteica de la harina de soja desgrasada (debido al alto contenido de carbohidratos solubles no-metabolizables) limita el nivel de inclusión en las dietas para acuacultura intensiva y otros usos. La mayoría de las harinas de soja que se ofrecen en el mercado han sido obtenidas por extracción con hexano o prensas mecánicas, teniendo una alta cantidad de azúcares solubles que pueden causar efectos adversos cuando estas harinas se usan como componentes en alimentos balanceados para salmones, truchas, camarones, cerdos y terneros. In addition, the low protein concentration of defatted soybean meal (due to the high content of non-metabolizable soluble carbohydrates) limits the level of inclusion in diets for intensive aquaculture and other uses. Most of the soy flour that is offered on the market has been obtained by extraction with hexane or mechanical presses, having a high amount of soluble sugars that can cause adverse effects when these flours are used as components in balanced feed for salmon, trout , shrimp, pigs and calves.
Existe alto interés en una harina de soja que contenga una reducida cantidad de aceite y de azucares solubles, producida en condiciones económicas eficientes, para ser utilizada en una amplia diversidad de alimentos.  There is high interest in a soybean meal that contains a small amount of oil and soluble sugars, produced in efficient economic conditions, to be used in a wide variety of foods.
De acuerdo con esta invención, es posible producir una harina de soja de alto tenor de proteínas, baja cantidad de carbohidratos solubles y reducida cantidad de aceite residual, de manera muy eficiente, utilizando únicamente etanol puro y diluciones en agua sin desolventización intermedia. En la industria se usa hexano para extraer aceite del poroto de soja, y luego en una segunda etapa se utiliza otro solvente , generalmente alcoholes de cadena corta o soluciones acuosas de los mismos, para extraer los carbohidratos y concentrar la proteína. Al cambiar de solvente debe primero removerse el hexano. Este paso intermedio de desolventización degrada el producto en su calidad al requerir la aplicación de calor, ya que en este proceso se somete el producto a temperaturas mayores a 100°C durante más de 30 minutos , lo que carameliza los azucares/carbohidratos en la harina dificultando su extracción posterior . Por lo tanto el uso de hexano requiere un segundo equipo de extracción posterior al desolventizado intermedio. De acuerdo con esta invención no se requiere este paso intermedio de desolventización, por tanto en un solo equipo se realiza la extracción de aceite con etanol y a continuación la extracción de carbohidratos con mezcla de etanol-agua y una sola etapa de desolventizado final en lugar de las dos que requiere el proceso convencional.  In accordance with this invention, it is possible to produce a soybean meal of high protein content, low amount of soluble carbohydrates and reduced amount of residual oil, very efficiently, using only pure ethanol and dilutions in water without intermediate deolventization. In industry, hexane is used to extract oil from soybeans, and then in a second stage another solvent, usually short chain alcohols or aqueous solutions thereof, is used to extract carbohydrates and concentrate the protein. When changing solvents, hexane must first be removed. This intermediate deolventization step degrades the product in its quality by requiring the application of heat, since in this process the product is subjected to temperatures greater than 100 ° C for more than 30 minutes, which caramelizes the sugars / carbohydrates in the flour hindering its subsequent extraction. Therefore, the use of hexane requires a second extraction equipment after intermediate desolventized. According to this invention, this intermediate deolventization step is not required, therefore in a single equipment the extraction of oil with ethanol is carried out and then the extraction of carbohydrates with ethanol-water mixture and a single stage of final deolventized instead of the two required by the conventional process.
El poroto de soja es recibido del productor y almacenado adecuadamente en silos. Las etapas del proceso comprenden, limpieza, descascarado y quebrado, laminado, expandido como alternativa posible y luego extracción con etanol mediante un extractor rotativo que permite realizar en un mismo equipo la operación de extracción en contracorriente del aceite con etanol (embebido, percolación y escurrimiento) y a continuación embebido con solución de etanol y agua (inundación) y extracción en contracorriente de los carbohidratos con solución de etanol y agua (percolación y escurrimiento).  Soy beans are received from the producer and properly stored in silos. The stages of the process include cleaning, peeling and cracking, rolling, expanded as a possible alternative and then extraction with ethanol by means of a rotary extractor that allows the operation of countercurrent extraction of the oil with ethanol (embedding, percolation and runoff) ) and then embedded with ethanol and water solution (flood) and countercurrent extraction of carbohydrates with ethanol and water solution (percolation and runoff).
Del extractor salen dos corrientes liquidas: mezcla de etanol-aceite, mezcla de etanol- carbohidratos y una corriente solida (harina). Two liquid streams come out of the extractor: mixture of ethanol-oil, mixture of ethanol-carbohydrates and a solid stream (flour).
1 - La corriente aceite-etanol se enfría a menos de 25 ºC, preferiblemente entre 15 y 25ºC, provocando la precipitación del 97 % del aceite contenido en la solución, el etanol es separado del aceite mediante una centrifuga, retornando al proceso con un mínimo de aceite residual.  1 - The oil-ethanol stream is cooled to less than 25 ° C, preferably between 15 and 25 ° C, causing the precipitation of 97% of the oil contained in the solution, the ethanol is separated from the oil by a centrifuge, returning to the process with a minimum of residual oil.
El aceite separado con muy bajo contenido de etanol pasa luego por un columna sometida a vacío, trabajando a una presión de 50/200 mmHg a 95/105 °C con un 0,5/1 % peso en peso de vapor de stripping (borboteo), donde se eliminan las trazas de etanol y luego pasa por un secador, obteniéndose un producto de alta calidad listo para la comercialización.  The separated oil with very low ethanol content then passes through a column under vacuum, working at a pressure of 50/200 mmHg at 95/105 ° C with a 0.5 / 1% weight by weight stripping steam (bubbling ), where traces of ethanol are removed and then passed through a dryer, obtaining a high quality product ready for commercialization.
2 - La corriente etanol-carbohidratos se procesa en una serie de evaporadores convencionales, donde se recupera una solución con una composición promedio de 60 % etanol-40% agua, preferiblemente una solución 40% etanol - 60% agua, mas preferiblemente 55% etanol - 45 % agua, que vuelve al proceso, obteniéndose un concentrado de azucares, denominado melaza.  2 - The ethanol-carbohydrate stream is processed in a series of conventional evaporators, where a solution with an average composition of 60% ethanol-40% water is recovered, preferably a solution 40% ethanol - 60% water, more preferably 55% ethanol - 45% water, which returns to the process, obtaining a concentrate of sugars, called molasses.
En el diagrama de flujo de la figura 1 se ha incluido opcionalmente la recuperación de las isoflavonas como alternativa posible y de las melazas residuales que se fermentan según el método tradicional, con levaduras del tipo Saccharomyces  The flowchart of Figure 1 has optionally included the recovery of isoflavones as a possible alternative and of residual molasses that are fermented according to the traditional method, with yeasts of the Saccharomyces type
Cerevisiae a PH 3,5-4,5 y temperatura de 35°C durante 12 horas, obteniéndose unos 500 gramos de etanol por Kg de azúcar que ingresa al proceso. Cerevisiae at PH 3.5-4.5 and temperature of 35 ° C for 12 hours, obtaining about 500 grams of ethanol per Kg of sugar entering the process.
La solución de etanol obtenido, se rectifica en una columna de destilación de platos que incluye etapa de secado y luego se utiliza para alimentar el proceso. The ethanol solution obtained is rectified in a dish distillation column that includes the drying stage and then used to feed the process.
3 - La corriente sólida pasa por una etapa final de desolventizado donde se evapora el etanol remanente a una temperatura de 90/1 00 °C hasta reducir su contenido de etanol remanente por debajo de las 500 ppm y luego pasa por un equipo enfriador, donde finalmente se alcanza una temperatura inferior a los 40°C. Dado que solo se usa etanol y diluciones en agua de etanol, no se requiere el paso intermedio de desolventización como es el caso si se usara hexano en la primera etapa y luego otro solvente.  3 - The solid stream passes through a final stage of de -venting where the remaining ethanol evaporates at a temperature of 90/1 00 ° C until its remaining ethanol content is reduced below 500 ppm and then passes through a cooling equipment, where finally a temperature below 40 ° C is reached. Since only ethanol and dilutions in ethanol water are used, the intermediate deolventization step is not required as is the case if hexane was used in the first stage and then another solvent.
Antes del almacenamiento, el material pasa por un sistema de molinos y zarandas para regular el tamaño de partículas de la harina de soja concentrada en proteína (SPC).  Before storage, the material goes through a system of mills and screens to regulate the particle size of the protein-concentrated soybean meal (SPC).
Detalle de la Invención El objeto de la presente invención es un proceso para la obtención de proteína de soja concentrada y aceites de alta calidad, que a diferencia del método tradicional , se hace en un solo extractor y comprende las siguientes etapas : Invention Detail The object of the present invention is a process for obtaining concentrated soy protein and high quality oils, which unlike the traditional method, is done in a single extractor and comprises the following steps:
A- Preparación del poroto de soja para su tratamiento A- Preparation of soybeans for treatment
B- Extracción con etanol de aceites y fosfolípidos y de carbohidratos con etanol-agua. C- Separación del aceite de soja del solvente mediante un método no destílativo. D- Acondicionamiento del solvente para su reutilización en ciclo cerrado  B- Extraction with ethanol of oils and phospholipids and carbohydrates with ethanol-water. C- Separation of the soybean oil from the solvent by a non-distillation method. D- Solvent conditioning for reuse in closed cycle
E- Separación de fosfolípidos y otras impurezas del aceite. . E- Separation of phospholipids and other impurities from the oil. .
F- Separación, concentración y fermentación de las melazas formadas por los hidratos de carbono para producir etanol.  F- Separation, concentration and fermentation of molasses formed by carbohydrates to produce ethanol.
G- La etapa anterior (F) puede o no incluir la separación de las isoflavonas de las melazas previo a su fermentación. G- The previous stage (F) may or may not include the separation of isoflavones from molasses prior to fermentation.
H- Obtención de harina de soja de proteína concentrada (SPC) libre de factores antinutricionales, apta para consumo humano y animal y la producción de aislados de proteína soja. H- Obtaining concentrated protein soybean meal (SPC) free of anti-nutritional factors, suitable for human and animal consumption and the production of soy protein isolates.
Más específicamente la presente invención es un proceso para la obtención de proteína de soja concentrada y aceites de alta calidad, que a diferencia del método tradicional , se hace en un solo extractor y comprende las siguientes etapas : More specifically, the present invention is a process for obtaining concentrated soy protein and high quality oils, which unlike the traditional method, is made in a single extractor and comprises the following steps:
A preparación del poroto de soja para su tratamiento mediante limpieza; quebrado y descascarado de porotos de soja, separación de la cáscara y laminado de los porotos de soja descascarados, obteniéndose un material laminado de poroto de soja;  A preparation of soybeans for treatment by cleaning; cracking and shelling of soybeans, peel separation and rolling of peeled soybeans, obtaining a soy bean laminate material;
B. embebido y expansión del material de soja obtenido en la etapa A con una solución de etanol y aceite, con aproximadamente 20 % aceite. B. Embedding and expansion of the soy material obtained in stage A with a solution of ethanol and oil, with approximately 20% oil.
C. extracción con etanol de aceites y fosfolípidos del material de soja C. ethanol extraction of oils and phospholipids from soy material
obtenido en la etapa B por percolación del etanol y las mezclas (miscellas) de etanol-aceite de concentraciones decrecientes en contracorriente a través del material de soja;  obtained in stage B by percolation of ethanol and mixtures (miscelles) of ethanol-oil of decreasing concentrations in countercurrent through the soy material;
D. embebido y expansión del material sólido de soja obtenido en la etapa C con una mezcla de etanol-agua y carbohidratos, que contiene hasta 5 % de carbohidratos.  D. Embedding and expansion of the solid soy material obtained in stage C with a mixture of ethanol-water and carbohydrates, which contains up to 5% carbohydrates.
E. extracción con etanol-agua de los carbohidratos del material de soja  E. Ethanol-water extraction of carbohydrates from soy material
desgrasado obtenido en la etapa C por percolación de etanol-agua y las mezclas de etanol-agua-carbohidratos de concentración decreciente en contracorriente a través de dicho material de soja desgrasado;degreasing obtained in stage C by ethanol-water percolation and the mixtures of ethanol-water-carbohydrates of decreasing concentration in countercurrent through said defatted soy material;
F. separación del aceite de soja del etanol en la solución etanol-aceite F. separation of soybean oil from ethanol in the ethanol-oil solution
obtenida en la etapa C mediante un método no destilativo;  obtained in step C by a non-distillative method;
G. acondicionamiento del etanol obtenido en la etapa F para su reutilización en ciclo cerrado;  G. conditioning of the ethanol obtained in stage F for reuse in a closed cycle;
H. separación de fosfolípidos y otras impurezas del aceite obtenido en la etapa F;  H. separation of phospholipids and other impurities from the oil obtained in step F;
I. separación de los carbohidratos del etanol-agua de la solución carbohidratos-etanol-agua obtenida en la etapa E obteniéndose melazas y etanol que vuelve al proceso;  I. separation of the carbohydrates from the ethanol-water from the carbohydrates-ethanol-water solution obtained in step E obtaining molasses and ethanol that returns to the process;
J. separación, concentración y fermentación de las melazas formadas por los hidratos de carbono obtenidos en la etapa I para producir etanol;  J. separation, concentration and fermentation of molasses formed by the carbohydrates obtained in stage I to produce ethanol;
K. opcionalmente en la etapa J se pueden separar las isoflavonas de las melazas previo a su fermentación;  K. Optionally in step J the isoflavones can be separated from the molasses prior to fermentation;
L. obtención de harina de soja de proteína concentrada (SPC) libre de factores antinutricionales, apta para consumo humano y animal y la producción de aislados de soja,  L. obtaining concentrated protein soybean meal (SPC) free of anti-nutritional factors, suitable for human and animal consumption and the production of soy isolates,
donde en dicho proceso se utiliza como único solvente etanol puro y diluciones en agua, y donde dicho proceso se realiza sin una etapa intermedia de desolventización. where in said process pure ethanol and dilutions in water are used as the sole solvent, and where said process is carried out without an intermediate stage of desolventization.
Descripción ampliada de cada etapa Extended description of each stage
A- Preparación del poroto de soja para su tratamiento  A- Preparation of soybeans for treatment
La preparación debe cumplir las mismas premisas que se utilizan para una instalación tradicional de procesamiento de soja.  The preparation must meet the same premises that are used for a traditional soybean processing facility.
El primer paso es una etapa de limpieza para eliminar impurezas, que consta de un sistema de cernidores, zarandas y multiaspiradores  The first step is a cleaning stage to remove impurities, which consists of a system of sieves, screens and multi-vacuum cleaners.
Luego el poroto de soja limpio, pasa a un sistema de quebradores, separadores de cáscara, laminadores y opcionalmente por la etapa de expandido, cumpliendo las mismas especificaciones que se utilizan en el proceso estándar para obtener harina de soja de Alta Proteína (High Pro).  Then the clean soy bean passes into a system of crushers, shell separators, laminators and optionally through the expanded stage, complying with the same specifications used in the standard process to obtain High Protein soy flour (High Pro) .
La harina de Alta Proteína (High Pro) tiene un contenido proteico de 47/48 % tal cual (52 - 53 % Base Seca) y es distinta de la harina de soja Concentrada en Proteína (SPC = Soybean Protein Concéntrate) que tiene un contenido proteico de 67 - 68 % tal cual (71 -72 % Base seca). High Protein flour (High Pro) has a protein content of 47/48% as is (52 - 53% Dry Base) and is different from Protein Concentrated soybean meal (SPC = Soybean Protein Concentrate) which has a protein content of 67-68% as is (71 -72% Dry Base).
B- Extracción con etanol de aceites, fosfolípidos y carbohidratos  B- Ethanol extraction of oils, phospholipids and carbohydrates
El material expandido se enfriara a 70 ºC e ingresara a un extractor rotativo dual, cuyo diseño único permite en un mismo equipo hacer el embebido/remojo y la extracción de aceite con etanol y el embebido y extracción de carbohidratos con etanol-agua. El extractor tiene forma circular y posee cinco áreas bien definidas:  The expanded material will be cooled to 70 ºC and will enter a dual rotary extractor, whose unique design allows in the same equipment to do the embedding / soaking and the extraction of oil with ethanol and the embedding and extraction of carbohydrates with ethanol-water. The extractor has a circular shape and has five well defined areas:
• Embebido/remojo del material que ingresa al extractor por inundación de las bandejas con mezcla de etanol y aceite con composición peso en peso de 15 % de aceite - 85 % de etanol, preferiblemente por una composición de 30 % de aceite y 70 % de etanol, mas preferiblemente por una composición de 20 % de aceite y 80 % de etanol.  • Embedding / soaking of material entering the extractor by flooding the trays with a mixture of ethanol and oil with a weight composition of 15% oil - 85% ethanol, preferably with a composition of 30% oil and 70% ethanol, more preferably by a composition of 20% oil and 80% ethanol.
• Extracción del aceite con etanol de 99% de pureza, mediante extracción por percolación con una mezcla de etanol-aceite de concentración decreciente a través del material a extraer en un sistema en contracorriente.  • Extraction of the oil with 99% purity ethanol, by percolation extraction with a mixture of ethanol-oil of decreasing concentration through the material to be extracted in a countercurrent system.
La temperatura de trabajo esta entre 70/80 ºC. The working temperature is between 70/80 ºC.
• Zona de drenaje del solvente residual de los sólidos extraídos mediante escurrimiento gravimétrico .  • Waste solvent drainage zone of solids extracted by gravimetric runoff.
• Embebido por inundación de las bandejas con solución conformada por 60 % etanol y 40 % agua, preferiblemente por una composición 80% etanol y 20 % agua peso en peso, mas preferiblemente por una composición 70% etanol y 30 % agua peso en peso. El propósito de esta etapa es promover la expansión del volumen del material al entrar en contacto la solución con la materia prima.  • Embedded by flooding the trays with a solution consisting of 60% ethanol and 40% water, preferably by an 80% ethanol and 20% water weight by weight composition, more preferably by a 70% ethanol composition and 30% water weight by weight. The purpose of this stage is to promote the expansion of the volume of the material when the solution comes into contact with the raw material.
El tiempo de residencia del embebido es de una permanencia de 10/17 minutos, preferiblemente una permanencia de 18/25 minutos, mas preferiblemente una permanencia de 15 minutos. The residence time of the embedded is a 10/17 minute stay, preferably an 18/25 minute stay, more preferably a 15 minute stay.
• Extracción de los carbohidratos en contracorriente, por percolación a través del material de una solución conformada por 60 % etanol y 40 % agua, preferiblemente por una composición 80% etanol y 20 % agua peso en peso, mas preferiblemente por una composición 70% etanol y 30 % agua peso en peso.  • Extraction of carbohydrates in countercurrent, by percolation through the material of a solution consisting of 60% ethanol and 40% water, preferably by a composition 80% ethanol and 20% water weight by weight, more preferably by a composition 70% ethanol and 30% water weight by weight.
La temperatura de trabajo es de 70 ºC y se utilizan entre 4 y 5 toneladas de solución de etanol por tonelada de harina a procesar, según las especificaciones del producto a obtener. • Zona de drenaje con vacío diferencial o escurrimiento gravimétrico para separar el líquido remanente en el material. The working temperature is 70 ºC and between 4 and 5 tons of ethanol solution are used per ton of flour to be processed, according to the specifications of the product to be obtained. • Drainage zone with differential vacuum or gravimetric runoff to separate the remaining liquid in the material.
El producto que sale de la zona de drenaje, con un contenido de materia grasa inferior a 1 %, es transportado mediante un redler al sistema de desolventacion, donde se evaporara el etanol y agua remanente, en forma suave para mantener en forma óptima las condiciones nutricionales y organolépticas de la harina de soja concentrada en proteínas (SPC).  The product that leaves the drainage zone, with a fat content of less than 1%, is transported by means of a redler to the solvent system, where the ethanol and remaining water will evaporate, in a gentle way to optimally maintain the conditions Nutritional and organoleptic protein concentrate soybean meal (SPC).
Los vapores de etanol evaporados son condensados y los gases remanentes, son succionados a través de un lavador de gases por medio de un ventilador centrífugo o un eyector de vapor.  The evaporated ethanol vapors are condensed and the remaining gases are sucked through a gas scrubber by means of a centrifugal fan or a steam ejector.
C- Separación del aceite de soja del solvente mediante un método no destilativo C- Separation of the soybean oil from the solvent by a non-distillation method
La mezcla de etanol-aceite caliente, abandona el extractor a una temperatura de entre 70/80 ºC y es enfriada a menos de 25 ºC, preferiblemente entre 1 5 y 25 ºC, produciendo la separación del aceite, etanol y sólidos. La figura 2 muestra la Curva de Solubilidad de aceite de soja en etanol en función de la temperatura. The hot oil-ethanol mixture leaves the extractor at a temperature of between 70/80 ° C and is cooled to less than 25 ° C, preferably between 1 and 25 ° C, producing the separation of oil, ethanol and solids. Figure 2 shows the Solubility Curve of soybean oil in ethanol as a function of temperature.
El 95-98 % del etanol que entra al enfriador es liberado y retornado al extractor .  95-98% of the ethanol entering the cooler is released and returned to the extractor.
Un 2-5% del etanol permanece solubilizado en el aceite junto a los fosfolípidos precipitados.  2-5% of ethanol remains solubilized in the oil along with the precipitated phospholipids.
El aceite y los sólidos alimentan a una centrífuga tipo decanter en la cual los sólidos son separados del aceite y una vez secos, se venden como lecitina.  The oil and solids feed a decanter-type centrifuge in which the solids are separated from the oil and once dried, they are sold as lecithin.
El aceite es enviado a un stripper para remover el etanol remanente, obteniéndose un aceite desgomado de alta calidad.  The oil is sent to a stripper to remove the remaining ethanol, obtaining a high quality degummed oil.
Los vapores provenientes del stripper y del desolventizador/secador de harina, son condensados y retornados al proceso.  Vapors from the stripper and the flour desolventizer / dryer are condensed and returned to the process.
D - Separación y concentración de las melazas formadas por los hidratos de carbono. D - Separation and concentration of molasses formed by carbohydrates.
En la segunda etapa del extractor, luego del embebido/remojo del material y de la extracción de carbohidratos con la solución de etanol-agua, se extraen los carbohidratos (melaza) de la mezcla etanol/agua con un 1 a 5% de sólidos que sale del extractor.  In the second stage of the extractor, after the embedding / soaking of the material and the extraction of carbohydrates with the ethanol-water solution, the carbohydrates (molasses) of the ethanol / water mixture are extracted with 1 to 5% solids that leaves the extractor.
Esta mezcla (miscela) entra a un sistema de evaporadores convencionales a entre 70/80 ºC bajo vacío en los cuales se recupera el etanol que vuelve al proceso y se concentra la melaza hasta 10% de sólidos. Esta corriente entra a una torre de destilación, que trabaja a 85 ºC donde se recupera el etanol restante, drenando por el fondo una solución de melaza con 30% de sólidos, que se enfría a aproximadamente 35 ºC y envía a la planta de fermentación. This mixture (miscela) enters a system of conventional evaporators at 70/80 ° C under vacuum in which the ethanol that returns to the process is recovered and the molasses is concentrated to 10% solids. This stream enters a distillation tower, which works at 85 ° C where the remaining ethanol is recovered, draining a molasses solution with 30% solids at the bottom, which is cooled to approximately 35 ° C and sent to the fermentation plant.
Más concretamente la solución etanol -agua-carbohidratos se somete a un proceso de evaporación a 70/80 ºC bajo vacío, donde se recupera una solución de 55/65 % etanol- 35/45% agua que vuelve al proceso luego de pasar por una columna de destilación convencional para obtener la porción necesaria de etanol puro para alimentar el proceso extracción de aceite en la primera etapa y sus diluciones con agua para la extracción de carbohidratos en la segunda etapa , obteniéndose una solución de azucares denominado melaza, la solución de etanol obtenida se rectifica por destilación y se utiliza para alimentar el proceso, la solución de melaza se concentra hasta aproximadamente 1 0% de sólidos y se destila a una temperatura aproximada de 85 ºC donde se recupera el etanol restante que vuelve al proceso, obteniéndose una melaza con aproximadamente 30% de sólidos que se enfría a aproximadamente 35 ºC y se fermenta para obtener etanol. Opcionalmente previo a la fermentación, puede realizarse la extracción de las isoflavonas contenidas en la melaza aprovechando la baja solubilidad de estos compuestos a baja temperatura y PH acido, se lleva la solución de melazas a pH 4,5 y se enfría a menos de 5 °C , precipitando más del 95% de las isoflavonas. Si se hace la separación de las isoflavonas, la melaza residual debe volver a calentarse hasta aproximadamente 35 ºC para proceder a la fermentación. More specifically, the ethanol-water-carbohydrate solution is subjected to an evaporation process at 70/80 ° C under vacuum, where a solution of 55/65% ethanol- 35/45% water is recovered that returns to the process after going through a Conventional distillation column to obtain the necessary portion of pure ethanol to feed the oil extraction process in the first stage and its dilutions with water for the extraction of carbohydrates in the second stage, obtaining a sugar solution called molasses, the ethanol solution obtained is rectified by distillation and used to feed the process, the molasses solution is concentrated to approximately 1.0% solids and distilled at an approximate temperature of 85 ° C where the remaining ethanol that returns to the process is recovered, obtaining a molasses with about 30% solids that is cooled to about 35 ° C and fermented to obtain ethanol. Optionally prior to fermentation, the extraction of the isoflavones contained in the molasses can be carried out taking advantage of the low solubility of these compounds at low temperature and acidic pH, the molasses solution is brought to pH 4.5 and cooled to less than 5 ° C, precipitating more than 95% of the isoflavones. If the isoflavones are separated, the residual molasses must be reheated to approximately 35 ° C to proceed to fermentation.
F - Precipitación y separación de las isoflavonas F - Precipitation and separation of isoflavones
Previo a la fermentación, puede realizarse la extracción de las isoflavonas contenidas en la melaza.  Prior to fermentation, the extraction of the isoflavones contained in the molasses can be carried out.
El contenido promedio de isoflavonas en la melaza es el siguiente:  The average isoflavone content in molasses is as follows:
Genistein 0,6 - 0,8 %  Genistein 0.6 - 0.8%
Daidzein 0,5 - 0,7 %  Daidzein 0.5 - 0.7%
Glycitein 1 - 1 ,2 %  Glycitein 1 - 1, 2%
Aprovechando la baja solubilidad de estos compuestos a baja temperatura y PH acido, se lleva la solución de melazas a pH 4,5 y se enfría a menos de 5 °C , precipitando mas del 95% de las isoflavonas Taking advantage of the low solubility of these compounds at low temperature and acidic pH, the molasses solution is brought to pH 4.5 and cooled to less than 5 ° C, precipitating more than 95% of the isoflavones
A modo de referencia, en el siguiente gráfico se observa la solubilidad de la isoflavona denominada Genistein en agua en función de la temperatura. La figura 3 muestra la solubilidad de la Isoflavona Genistein en agua en función de la temperatura. By way of reference, the following graph shows the solubility of isoflavone called Genistein in water as a function of temperature. Figure 3 shows the solubility of Isoflavone Genistein in water as a function of temperature.
El precipitado se separa mediante filtración o centrifugación, obteniendo un producto enriquecido en isoflavonas (entre 5 y 10 % de concentración) que puede ser comercializado en esa forma o sometido a posteriores purificaciones y/o tratamientos enzimáticos para obtener isoflanovas en su modo conjugado o agluconas.  The precipitate is separated by filtration or centrifugation, obtaining a product enriched in isoflavones (between 5 and 10% concentration) that can be marketed in that form or subjected to subsequent purifications and / or enzymatic treatments to obtain isoflanovas in its conjugate or agluconas mode. .
E - Fermentación de las melazas. E - Fermentation of molasses.
La composición de los carbohidratos de la melaza son:  The composition of the molasses carbohydrates are:
50 % Sucrose  50% Sucrose
25 % Stachyose  25% Stachyose
25 % Raffinose  25% Raffinose
El contenido de azucares en Melaza con 30% de sólidos, es de 16%.  The sugar content in Molasses with 30% solids is 16%.
El azúcar de la melaza, puede ser fermentado por el método tradicional para obtener etanol. En grandes fermentadores, se mezcla la melaza con levaduras y se mantiene a PH entre 3,5 y 4 durante 8/12 horas a temperatura ambiente (35 ºC). Molasses sugar can be fermented by the traditional method to obtain ethanol. In large fermenters, the molasses is mixed with yeasts and kept at pH between 3.5 and 4 for 8/12 hours at room temperature (35 ° C).
Descripción del extractor rotativo La figura 4 describe el proceso de extracción con Etanol y la figura 5 el proceso de extracción con Etanol-Agua. Description of the rotary extractor Figure 4 describes the ethanol extraction process and figure 5 the ethanol-water extraction process.
Ambas etapas se realizan en un mismo extractor. Both stages are carried out in the same extractor.
El extractor es de tipo rotativo, dividido en celdas radiales uniformes, que tiene la particularidad de que al completar un giro total de 360°, realiza las operaciones de alimentación de laminas de soja al extractor , embebido/remojo con mezcla de etanol y aceite concentrada en aceite, extracción de aceite en contracorriente, drenaje del solvente, embebido/remojo de la harina desgrasada con solución de etanol y agua con 1 a 5 % de sólidos (melazas), extracción de azucares en contracorriente con solución de alcohol y agua, drenaje de los sólidos extraídos con la solución de etanol- agua y descarga de la harina de proteína concentrada.  The extractor is of rotary type, divided into uniform radial cells, which has the particularity that when completing a total 360 ° rotation, it performs the operations of feeding soybean sheets to the extractor, embedded / soaking with a mixture of ethanol and concentrated oil in oil, oil extraction in countercurrent, solvent drainage, soaking / soaking of the degreased flour with ethanol solution and water with 1 to 5% solids (molasses), sugar extraction in countercurrent with alcohol and water solution, drainage of the solids extracted with the ethanol-water solution and discharge of the concentrated protein flour.
El equipo tiene zonas de embebido que trabajan por inundación y se logran mediante pisos ciegos, zonas de percolación, donde el etanol utilizado para la extracción drena (percola) a través del material por pisos perforados/ranurados, extrayendo aceite en la primera etapa y los azucares en la segunda etapa y otras zonas de drenaje que también tienen pisos perforados o ranurados y permiten escurrir los líquidos excedentes de los sólidos. Las zonas de drenaje pueden tener vacío en el compartimento inferior para mejorar el escurrimiento de los sólidos, aunque esta solución es opcional y puede o no utilizarse. El equipo esta diseñado de manera de mantener tiempos de residencia determinados en cada sección: The equipment has embedded areas that work by flooding and are achieved through blind floors, percolation areas, where the ethanol used for extraction drains (percolates) through the material through perforated / grooved floors, extracting oil in the first stage and sugars in the second stage and other drainage areas that also have perforated or grooved floors and allow excess liquids to drain from solids. The drainage areas may have a vacuum in the lower compartment to improve the runoff of solids, although this solution is optional and may or may not be used. The equipment is designed to maintain specific residence times in each section:
- Embebido etanol puro y aceite : 15 minutos - Embedded pure ethanol and oil: 15 minutes
- Lavado con etanol puro en contracorriente : 60 minutos  - Washing with pure ethanol in countercurrent: 60 minutes
- Drenaje : 15 minutos  - Drainage: 15 minutes
- Embebido solución etanol-agua : 1 5 minutos  - Embedded ethanol-water solution: 1 5 minutes
- Lavado solución etanol- agua en contracorriente : 75 minutos  - Ethanol-water solution wash in countercurrent: 75 minutes
- Drenaje : 15 minutos - Drainage: 15 minutes
El principio es de lavado en contracorriente, es decir que el material avanza en una dirección y va siendo lavado por soluciones con concentraciones de aceite o melazas menores a medida que se acerca a la etapa final de cada proceso, permitiendo mantener gradientes de concentraciones que permiten extraer tanto el aceite como las melazas.  The principle is backwashing, that is to say that the material moves in one direction and is being washed by solutions with lower oil concentrations or molasses as it approaches the final stage of each process, allowing to maintain concentration gradients that allow extract both oil and molasses.
Las zonas de inundación tienen por finalidad provocar el embebido del material y su expansión. Las celdas del extractor en las zonas de embebido pueden alimentarse con solución tanto desde abajo a través del piso como por la parte superior como se hace en otras partes del extractor.  The flood zones are intended to cause the embedding of the material and its expansion. The extractor cells in the embedded areas can be fed with solution both from below through the floor and from the top as is done in other parts of the extractor.
En las celdas de la primera etapa de embebido con mezcla de etanol y aceite, se dosifica la harina sobre las celdas inundadas con la solución de etanol y aceite, lo que permite evitar una compactación excesiva del material, obteniendo una masa de composición porosa que permite muy buena percolación (drenaje) del etanol a través del lecho de harina, con un muy alto grado de eficiencia de remoción de aceite. In the cells of the first stage of embedding with mixture of ethanol and oil, the flour is dosed on the cells flooded with the solution of ethanol and oil, which allows to avoid an excessive compaction of the material, obtaining a mass of porous composition that allows very good percolation (drainage) of ethanol through the bed of flour, with a very high degree of oil removal efficiency.
En las etapas de embebido una corriente de estas soluciones concentradas se recicla sobre la misma celda tanto por el piso ciego inferior como por encima del material, lo que permite mantener la celda siempre inundada. La corriente que ingresa por el piso tiene como objetivo lograr un movimiento de convección de la mezcla de sólidos y líquidos de la celda inundada para evitar la compactación del material durante la fase de embebido/aumento de volumen por absorción de etanol-aceite en la primera fase o de etanol-agua en la segunda fase. In the embedding stages a stream of these concentrated solutions is recycled on the same cell both by the lower blind floor and above the material, which allows to keep the cell always flooded. The current entering the floor aims to achieve a convection movement of the mixture of solids and liquids of the flooded cell to avoid compacting the material during the embedding phase / volume increase by ethanol-oil absorption in the first phase or ethanol-water in the second phase.
Esta solución de bombear las miscellas de etanol-aceite y etanol-agua a través del piso perforado para remover el material en proceso y lograr mejor percolación puede utilizarse también como opción en las etapas de lavado en contracorriente. En los lavados en contracorriente las concentraciones de los productos extraídos por los solventes utilizados en cada etapa van en sentido contrario a las concentraciones de esos productos en los sólidos que se están lavando. Siempre el lavado final se hace con una mezcla líquida pura es decir etanol sin aceite en la primera etapa y etanol-agua sin carbohidratos en la segunda. This solution of pumping the ethanol-oil and ethanol-water miscelles through the perforated floor to remove the material in process and achieve better percolation can also be used as an option in the backwash stages. In backwashing, the concentrations of the products extracted by the solvents used in each stage go in the opposite direction to the concentrations of those products in the solids being washed. The final wash is always done with a pure liquid mixture that is, oil-free ethanol in the first stage and water-free ethanol-water in the second.
Las concentraciones de los productos a extraer de los sólidos van en sentido contrario a las de las mezclas líquidas utilizadas para extraerlos, manteniendo de este modo los gradientes de concentración que permiten la extracción de aceites y melazas. Estas mezclas de concentración decreciente se recirculan en las distintas etapas a través de la masa sólida mediante bombas.  The concentrations of the products to be extracted from the solids go in the opposite direction to those of the liquid mixtures used to extract them, thus maintaining the concentration gradients that allow the extraction of oils and molasses. These mixtures of decreasing concentration are recirculated in the different stages through the solid mass by means of pumps.
El proceso comienza con la entrada de láminas de soja al extractor sobre una celda inundada con una mezcla concentrada de etanol- aceite y luego se realizan varios lavados con mezcla de etanol aceite decreciente en celdas de percolación hasta el lavado final con etanol puro de 99 % de concentración, que permite extraer la materia grasa de la lamina de soja hasta un residual menor de 1 %.  The process begins with the entry of soybean sheets to the extractor on a cell flooded with a concentrated mixture of ethanol-oil and then several washes are carried out with ethanol mixture decreasing oil in percolation cells until the final wash with 99% pure ethanol of concentration, which allows to extract the fatty matter from the soybean sheet up to a residual less than 1%.
El paso siguiente es una celda de escurrido para drenar el solvente y a continuación los sólidos entran a una celda de inundación donde se pone en contacto el material ya desgrasado con la solución de etanol-agua, conformada por 60% etanol y 40% agua , preferiblemente por una composición 80% etanol y 20% agua peso en peso , mas preferiblemente por una composición 70% etanol y 30% agua peso en peso, donde se produce la expansión del material por hidratación.  The next step is a draining cell to drain the solvent and then the solids enter a flood cell where the already defatted material is contacted with the ethanol-water solution, consisting of 60% ethanol and 40% water, preferably by a composition 80% ethanol and 20% water weight by weight, more preferably by a composition 70% ethanol and 30% water weight by weight, where the expansion of the material occurs by hydration.
Luego se realizan múltiples lavados con la solución etanol-agua descripta, donde se extrae con gran eficiencia la mayoría de los azucares solubles.  Then multiple washes are carried out with the described ethanol-water solution, where most of the soluble sugars are extracted with great efficiency.
A continuación, el material ingresa a una celda de escurrido para drenar la solución etanol - agua y pasa a un sistema de prensado dewatering donde se extrae la mayor parte de solvente remanente. Next, the material enters a draining cell to drain the ethanol-water solution and passes into a dewatering pressing system where most of the remaining solvent is extracted.
Luego el producto entra en un desmenuzador para homogenizar el tamaño de las partículas del material sólido y alimentar el equipo desolventizador.  Then the product enters a shredder to homogenize the size of the particles of the solid material and feed the desolventizer equipment.
Esta etapa de dewatering y desmenuzado puede no utilizarse, en ese caso desde la etapa de drenaje el material entra directamente a la etapa de desolventización que puede ser convencional o de tubos rotativos. This stage of dewatering and shredding may not be used, in that case from the drainage stage the material directly enters the desolventization stage which can be conventional or rotary tubes.
Finalmente el producto se seca mediante un sistema de secadores de tubos rotativos que permite evitar el daño térmico sobre la proteína, obteniendo una harina concentrada de soja de excelente calidad organoléptica y nutricional. La solución etanol-aceite de la primera etapa y la solución etanol-agua-azucares de la segunda etapa, se recuperan en circuitos diferenciados teniendo cada uno distinto tratamiento. Finally, the product is dried by a system of rotary tube dryers that allows to avoid thermal damage on the protein, obtaining a concentrated soybean meal of excellent organoleptic and nutritional quality. The ethanol-oil solution of the first stage and the ethanol-water-sugar solution of the second stage are recovered in differentiated circuits each having different treatment.
EJEMPLO 1. Obtención de Proteína Concentrada de Soja (SPC) a partir de Porotos de Soja.  EXAMPLE 1. Obtaining Concentrated Soy Protein (SPC) from Soy Beans.
Se procesaron 1000 kg poroto de soja, de calidad estándar de mercado en una instalación piloto.  1000 kg of soybeans were processed, of market standard quality in a pilot installation.
Se comenzó con la etapa de prelimpieza y luego los porotos fueron calentados hasta una temperatura de entre 60/65° ingresando a la etapa de descascarado, donde se partió el poroto y se separó la cáscara, mediante la aspiración con aire en contracorriente.  The pre-cleaning stage was started and then the beans were heated to a temperature of between 60/65 ° entering the shelling stage, where the bean was split and the shell was separated, by aspiration with countercurrent air.
La cáscara separada, se molió y se pelletizó, obteniéndose 70 Kg de pellet de cáscara.  The separated shell was ground and pelletized, obtaining 70 kg of shell pellet.
El poroto descascarado se laminó usando rodillos especiales, obteniendo láminas de 0,35/0,45 mm de espesor.  The shelled bean was laminated using special rollers, obtaining 0.35 / 0.45 mm thick sheets.
Las láminas obtenidas ingresaron al extractor donde en la primer sección se realizo el embebido y la extracción del aceite con etanol puro y en la segunda sección se hizo el embebido y la extracción de los azucares, mediante el lavado en contracorriente con una solución compuesta por 70% de etanol proveniente de la primera etapa y 30% de agua. El etanol utilizado proviene de la primera etapa y del sistema de destilación/recuperación ya descripto.  The sheets obtained entered the extractor where in the first section the embedding and extraction of the oil with pure ethanol was carried out and in the second section the embedding and extraction of the sugars was made, by backwashing with a solution composed of 70 % of ethanol from the first stage and 30% of water. The ethanol used comes from the first stage and from the distillation / recovery system already described.
La miscela etanol-aceite se enfrío a 25 °C, separando el aceite precipitado por diferencial de solubilidad de aceite en etanol en función de la temperatura y las lecitinas hidratadas insolubilizadas en el aceite y separadas por centrifugación.  The ethanol-oil miscel was cooled to 25 ° C, separating the precipitated oil by differential of oil solubility in ethanol depending on the temperature and the hydrated lecithins insolubilized in the oil and separated by centrifugation.
Luego de eliminar las trazas de etanol por calentamiento bajo vacío, se obtuvieron 6 Kg de Lecitina y 1 95 Kg de aceite de soja desgomado . After removing traces of ethanol by heating under vacuum, 6 Kg of Lecithin and 1 95 Kg of degummed soybean oil were obtained.
La miscela de etanol-azúcares se concentró mediante la evaporación total del etanol y parte del agua en un equipo evaporador, hasta obtener una concentración de aproximadamente 30 % de sólidos. Los vapores se condensaron y retornaron al proceso.  The ethanol-sugar miscel was concentrated by the total evaporation of ethanol and part of the water in an evaporator, until obtaining a concentration of approximately 30% solids. Vapors condensed and returned to the process.
Las melazas concentradas, alimentaron el proceso de fermentación con levaduras, donde luego de evaporar y rectificar, se obtuvieron 52,3 Kg de etanol. Luego de secar y enfriar las harinas que salieron del extractor, se obtuvieron 530 kg de Proteína Concentrada de Soja (SPC) con un contenido de proteína de 68,4% tal cual ( 71 ,50 % en base seca.) The concentrated molasses fed the fermentation process with yeasts, where after evaporating and rectifying, 52.3 kg of ethanol were obtained. After drying and cooling the flours that came out of the extractor, 530 kg of Concentrated Soy Protein (SPC) were obtained with a protein content of 68.4% as is (71, 50% on a dry basis.)
Datos analíticos obtenidos durante el test. Analytical data obtained during the test.
Se simuló el proceso descripto en Laboratorio, utilizando un modelo a escala piloto. Se alimento el prototipo con láminas de soja y se lo sometió a una extracción con etanol puro en la primera etapa y con solución 70% etanol y 30% agua en la segunda, ambas en contracorriente. The process described in the Laboratory was simulated, using a pilot scale model. The prototype was fed with soybeans and subjected to an extraction with pure ethanol in the first stage and with 70% ethanol solution and 30% water in the second, both in countercurrent.
Se tomaron muestras en cada etapa de lavado en cada sección para establecer la curva de rendimiento del proceso.  Samples were taken at each wash stage in each section to establish the process performance curve.
Durante la primera etapa de extracción de aceite, la materia grasa de la harina decreció de 23,55% a 0,31 % en 6 lavados.  During the first stage of oil extraction, the fat in the flour decreased from 23.55% to 0.31% in 6 washes.
Luego de la segunda etapa de extracción de azucares descripta precedentemente, la proteína de la harina creció de 40,75 % a 71 ,50 % (base seca)  After the second stage of sugar extraction described above, the flour protein grew from 40.75% to 71.50% (dry basis)
La siguiente Tabla I muestra datos analíticos obtenidos durante el Test. The following Table I shows analytical data obtained during the Test.
Figure imgf000016_0001
Figure imgf000016_0001
Las características Físico Químicas de las harinas de alta proteína obtenidas fueron las siguientes:  The Chemical Physical characteristics of the high protein flours obtained were the following:
Apariencia: Polvo fino , seco .  Appearance: Fine, dry powder.
Proteína: Min. 68%( como N x 6.25) Protein: Min. 68% (as N x 6.25)
Humedad: Max 7 % Humidity: Max 7%
Oligosacáridos: Max 1 % Oligosaccharides: Max 1%
Materia Grasa: Max. 1 % Fatty matter: Max. one %
Inhibidor Tripsina: Max. 5000 TIU/g de producto Trypsin Inhibitor: Max. 5000 TIU / g of product
Beneficios económicos inherentes al proceso Economic benefits inherent in the process
El valor diferencial de los productos recuperados respecto a la situación actual indica que es una excelente oportunidad de generación de valor: The differential value of the products recovered with respect to the current situation indicates that it is an excellent opportunity to generate value:
Figure imgf000017_0001
Figure imgf000017_0001
Rendimientos del Proceso Process returns
- Harina SPC/ Poroto descascarado : 52-54 % - Proteína Base Seca :71-73 % - SPC Flour / Shelled Bean: 52-54% - Dry Base Protein: 71-73%
- Materia Grasa : 0,3-0,6 % Aplicación industrial de la invención - Fatty matter: 0.3-0.6% Industrial application of the invention
La presente invención es de aplicación en toda la industria alimenticia, tanto para nutrición humana como animal. Las Proteínas Concentradas de Soja (SPC) tienen un importante potencial en el campo de la acuacultura, debido a la alta concentración de proteínas y la falta de compuestos antinutricionales.  The present invention is applicable throughout the food industry, both for human and animal nutrition. Concentrated Soy Proteins (SPC) have an important potential in the field of aquaculture, due to the high concentration of proteins and the lack of anti-nutritional compounds.
El proceso de extracción de aceite tiene menos costos energéticos que el original, ya que la recuperación del aceite es No Destilativa .  The oil extraction process has less energy costs than the original, since the oil recovery is Non-Distillative.
Se usa un solvente renovable como el etanol, que se obtiene de la fermentación de las melazas, por lo que el proceso no solo se autoabastece de etanol, sino que también genera un excedente para la venta.  A renewable solvent such as ethanol is used, which is obtained from the fermentation of molasses, so the process not only supplies itself with ethanol, but also generates a surplus for sale.
El etanol generado, tiene un alto porcentaje de isoflavonas, de creciente uso medicinal, lo que genera una fuente de ingreso adicional.  The ethanol generated, has a high percentage of isoflavones, of increasing medicinal use, which generates an additional source of income.
El aceite obtenido ya esta desgomado (contiene una muy baja cantidad de fosforo) y tiene bajo color por obtenerse a bajas temperaturas, lo que lo convierte en un producto Premium.  The oil obtained is already degummed (it contains a very low amount of phosphorus) and has a low color because it is obtained at low temperatures, which makes it a Premium product.

Claims

Reivindicaciones: Claims:
1 . Proceso para producir una harina de soja de proteína concentrada (SPC - Soybean Protein Concéntrate), baja cantidad de carbohidratos solubles y reducida cantidad de aceite caracterizado porque se utiliza etanol como único solvente y diluciones acuosas del mismo, no requiere destilación para la separación del aceite, donde la harina de soja de proteína concentrada (SPC) se obtiene con un solo tratamiento térmico de desolventizacion y que comprende las siguientes etapas:  one . Process to produce a concentrated protein soybean meal (SPC - Soybean Protein Concentrate), low amount of soluble carbohydrates and reduced amount of oil characterized in that ethanol is used as the sole solvent and aqueous dilutions thereof, does not require distillation for oil separation , where concentrated protein soybean meal (SPC) is obtained with a single heat treatment of desolventization and which comprises the following stages:
A preparación del poroto de soja para su tratamiento mediante limpieza; quebrado y descascarado de porotos de soja, separación de la cáscara y laminado de los porotos de soja descascarados, obteniéndose un material laminado de poroto de soja;  A preparation of soybeans for treatment by cleaning; cracking and shelling of soybeans, peel separation and rolling of peeled soybeans, obtaining a soy bean laminate material;
B. embebido y expansión del material de soja obtenido en la etapa A con una solución de etanol y aceite, con aproximadamente 20 % aceite; B. embedding and expansion of the soy material obtained in step A with a solution of ethanol and oil, with approximately 20% oil;
C. extracción con etanol de aceites y fosfolípidos del material de soja C. ethanol extraction of oils and phospholipids from soy material
obtenido en la etapa B por percolación del etanol y las mezclas (miscellas) de etanol-aceite de concentraciones decrecientes en contracorriente a través del material de soja;  obtained in stage B by percolation of ethanol and mixtures (miscelles) of ethanol-oil of decreasing concentrations in countercurrent through the soy material;
D. embebido y expansión del material sólido de soja obtenido en la etapa C con una mezcla de etanol-agua y carbohidratos, que contiene hasta 5 % de carbohidratos;  D. Embedding and expansion of the solid soy material obtained in stage C with a mixture of ethanol-water and carbohydrates, containing up to 5% carbohydrates;
E. extracción con etanol-agua de los carbohidratos del material de soja  E. Ethanol-water extraction of carbohydrates from soy material
desgrasado obtenido en la etapa C por percolación de etanol-agua y las mezclas de etanol-agua-carbohidratos de concentración decreciente en contracorriente a través de dicho material de soja desgrasado; degreasing obtained in step C by percolation of ethanol-water and mixtures of ethanol-water-carbohydrates of decreasing concentration in countercurrent through said defatted soy material;
F. separación del aceite de soja del etanol en la solución etanol-aceite F. separation of soybean oil from ethanol in the ethanol-oil solution
obtenida en la etapa C mediante un método no destilativo;  obtained in step C by a non-distillative method;
G. acondicionamiento del etanol obtenido en la etapa F para su reutilización en ciclo cerrado;  G. conditioning of the ethanol obtained in stage F for reuse in a closed cycle;
H. separación de fosfolípidos y otras impurezas del aceite obtenido en la etapa F;  H. separation of phospholipids and other impurities from the oil obtained in step F;
I. separación de los carbohidratos del etanol-agua de la solución carbohidratos-etanol-agua obtenida en la etapa E obteniéndose melazas y etanol que vuelve al proceso; J. separación, concentración y fermentación de las melazas formadas por los hidratos de carbono obtenidos en la etapa I para producir etanol; I. separation of the carbohydrates from the ethanol-water from the carbohydrates-ethanol-water solution obtained in step E obtaining molasses and ethanol that returns to the process; J. separation, concentration and fermentation of molasses formed by the carbohydrates obtained in stage I to produce ethanol;
K. opcionalmente en la etapa J se pueden separar las isoflavonas de las melazas previo a su fermentación;  K. Optionally in step J the isoflavones can be separated from the molasses prior to fermentation;
L. obtención de harina de soja de proteína concentrada (SPC) libre de factores antinutricionales, apta para consumo humano y animal y la producción de aislados de soja,  L. obtaining concentrated protein soybean meal (SPC) free of anti-nutritional factors, suitable for human and animal consumption and the production of soy isolates,
donde en dicho proceso se utiliza como único solvente etanol puro y diluciones en agua, y donde dicho proceso se realiza sin una etapa intermedia de desolventización. where in said process pure ethanol and dilutions in water are used as the sole solvent, and where said process is carried out without an intermediate stage of desolventization.
2. El proceso de la reivindicación 1 CARACTERIZADO porque dicha etapa C de extracción con etanol comprende embeber/remojar el material que ingresa al extractor con una composición etanol y aceite en una proporción de 1 5% de aceite - 85% de etanol. 2. The process of claim 1 CHARACTERIZED in that said step C of extraction with ethanol comprises embedding / soaking the material entering the extractor with an ethanol and oil composition in a proportion of 1.5% oil - 85% ethanol.
3. El proceso de la reivindicación 1 CARACTERIZADO porque dicha etapa C de extracción con etanol comprende embeber/remojar el material que ingresa al extractor con una composición etanol y aceite en una proporción de 30% de aceite - 70% de etanol. 3. The process of claim 1 CHARACTERIZED in that said step C of extraction with ethanol comprises embedding / soaking the material entering the extractor with an ethanol and oil composition in a proportion of 30% oil - 70% ethanol.
4. El proceso de la reivindicación 1 CARACTERIZADO porque dicha etapa C de extracción con etanol comprende embeber/remojar el material que ingresa al extractor con una composición etanol y aceite en una proporción de 20% de aceite - 80% de etanol. 4. The process of claim 1 CHARACTERIZED in that said step C of extraction with ethanol comprises embedding / soaking the material entering the extractor with an ethanol and oil composition in a proportion of 20% oil - 80% ethanol.
5. El proceso de la reivindicación 1 CARACTERIZADO porque el tiempo de residencia del embebido del paso B es de 18 a 25 minutos. 5. The process of claim 1 CHARACTERIZED in that the residence time of the embedding of step B is 18 to 25 minutes.
6. El proceso de la reivindicación 1 CARACTERIZADO porque el tiempo de residencia del embebido del paso B es de 10 a 17 minutos. 6. The process of claim 1 CHARACTERIZED in that the residence time of the embedding of step B is 10 to 17 minutes.
7. El proceso de la reivindicación 1 CARACTERIZADO porque el tiempo de residencia del embebido del paso B es de 15 minutos. 7. The process of claim 1 CHARACTERIZED in that the residence time of the embedding of step B is 15 minutes.
8. El proceso de la reivindicación 1 CARACTERIZADO porque el paso F de separación del aceite de soja del etanol se realiza enfriando la mezcla etanol-aceite a menos de 25 ºC. 8. The process of claim 1 CHARACTERIZED in that step F of separating soybean oil from ethanol is carried out by cooling the ethanol-oil mixture to less than 25 ° C.
9. El proceso de la reivindicación 1 CARACTERIZADO PORQUE el aceite de soja obtenido se somete a vacío trabajando a una presión de 50/200 mmHg a 95/1 05°C con un 0,5/1 % peso en peso de stripping de vapor , donde se eliminan las trazas de etanol y luego el aceite se seca , obteniéndose un producto disponible para la comercialización y los sólidos se secan, se procesan y comercializan como lecitina. 9. The process of claim 1 CHARACTERIZED BECAUSE the soybean oil obtained is subjected to vacuum working at a pressure of 50/200 mmHg at 95/1 05 ° C with a 0.5 / 1% weight by weight of steam stripping , where the traces of ethanol are removed and then the oil is dried, obtaining a product available for commercialization and the solids are dried, processed and marketed as lecithin.
10. El proceso de la reivindicación 1 CARACTERIZADO PORQUE la solución etanol -agua-carbohidratos se somete a un proceso de evaporación a 70/80 ºC bajo vacío, donde se recupera una solución de 55/65 % etanol- 35/45% agua que vuelve al proceso luego de pasar por una columna de destilación convencional para obtener la porción necesaria de etanol puro para alimentar el proceso extracción de aceite en la primera etapa y sus diluciones con agua para la extracción de carbohidratos en la segunda etapa , obteniéndose una solución de azucares denominado melaza, la solución de etanol obtenida se rectifica por destilación y se utiliza para alimentar el proceso, la solución de melaza se concentra hasta aproximadamente 1 0% de sólidos y se destila a una temperatura aproximada de 85 ºC donde se recupera el etanol restante que vuelve al proceso, obteniéndose una melaza con aproximadamente 30% de sólidos que se enfría a aproximadamente 35 ºC y se fermenta para obtener etanol, opcionalmente previo a la fermentación, puede realizarse la extracción de las isoflavonas contenidas en la melaza aprovechando la baja solubilidad de estos compuestos a baja temperatura y PH ácido, se lleva la solución de melazas a pH 4,5 y se enfría a menos de 5 °C , precipitando más del 95% de las isoflavonas, si se hace la separación de las isoflavonas, la melaza residual debe volver a calentarse hasta aproximadamente 35 ºC para proceder a la fermentación. 10. The process of claim 1 CHARACTERIZED BECAUSE the ethanol-water-carbohydrate solution is subjected to an evaporation process at 70/80 ° C under vacuum, where a solution of 55/65% ethanol- 35/45% water is recovered which returns to the process after going through a conventional distillation column to obtain the necessary portion of pure ethanol to feed the oil extraction process in the first stage and its dilutions with water for the extraction of carbohydrates in the second stage, obtaining a solution of sugars called molasses, the ethanol solution obtained is rectified by distillation and used to feed the process, the molasses solution is concentrated to approximately 1.0% solids and distilled at an approximate temperature of 85 ° C where the remaining ethanol is recovered which returns to the process, obtaining a molasses with approximately 30% solids that is cooled to approximately 35 ° C and fermented to obtain ethanol, option Only prior to fermentation, the extraction of the isoflavones contained in the molasses can be carried out taking advantage of the low solubility of these compounds at low temperature and acidic pH, the molasses solution is brought to pH 4.5 and cooled to less than 5 ° C, precipitating more than 95% of the isoflavones, if the separation of the isoflavones is made, the residual molasses must be reheated to approximately 35 ° C to proceed to fermentation.
1 1 . El proceso de la reivindicación 1 CARACTERIZADO PORQUE las corrientes de etanol obtenidas vuelven al proceso. eleven . The process of claim 1 CHARACTERIZED BECAUSE the ethanol streams obtained return to the process.
1 2. El proceso CARACTERIZADO PORQUE se obtiene una harina de soja de Proteína Concentrada (SPC - Soybean Protein Concéntrate) de muy alta calidad, alto % de Proteínas y muy bajo contenido de Factores Antinutricionales (ANF - Antinutritional Factors). p.a. LUIS EDUARDO PALACIOS 1 2. The CHARACTERIZED process BECAUSE a high-quality, high-quality Concentrated Protein soybean meal (SPC) is obtained. % of Proteins and very low content of Antinutritional Factors (ANF - Antinutritional Factors). for LUIS EDUARDO PALACIOS
p.a. MARIO DOMINGO ALLOCCO  p.a. MARIO DOMINGO ALLOCCO
p.a. MARIANA CARLA ALLOCCO  p.a. MARIANA CARLA ALLOCCO
p.a. MIRTA BERNARDA GUALA  p.a. MIRTA BERNARDA GUALA
PCT/IB2014/058325 2013-01-23 2014-01-16 Method for obtaining soybean protein concentrate from soy meal by means of extraction with alcohol, obtaining a high-protein flour without antinutritional factors and a high-quality oil WO2014115067A1 (en)

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