Units storage phosphatide concentrates,
Report the violation. Add your offer Register Log in. The plant "Svatovskoye maslo" is a large industrial complex, which is specialized in processing of sunflower seeds by pressing and extraction. Production structure corresponds to the technological requirements of acceptance, cleaning, processing and storage of sunflower seeds and it is represented by the main, auxiliary and service industries. Currently the company is represented by the following production units: - Basic: oil extraction production, raw material department, the section of the finished products, technical control department, grain storage; - Support unit: steam-boiler workshop, machine shop, electric station, control and measuring equipment and automatics workshop, water supply and sewerage workshop, buildings overhaul unit, motor transport section. Production capacity allows to process up to tones of sunflower seeds per season.VIDEO ON THE TOPIC: Modern Grower Interview with Precision Extraction Solutions
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- Drying phosphatide line
- Waffles "Zabodayka" milk
- EP1357803A2 - Methods for treating phosphatide-containing mixtures - Google Patents
- US2434788A - Fat-soluble vitamin concentrates - Google Patents
- Hawthorn Milk Beverage of Juice Concentrate
- WO2012036695A1 - Process to remove impurities from triacylglycerol oil - Google Patents
- US20060204632A1 - Concentrated human milk fortifier liquid - Google Patents
- FIELD OF THE INVENTION
- Preparation of the test with some improvers.
- US6172247B1 - Methods for refining vegetable oils and byproducts thereof - Google Patents
Drying phosphatide line
This invention relates to methods for treating distillates obtained during the process of deodorizing various oils. More particularly, this invention relates to methods for recovering fatty acids, tocopherols, and sterols from a distillate obtained from the deodorizing of various oils.
Oils derived from plants and animals are valuable sources of fatty acids, tocopherols, and sterols. During the process of refining such oils, however, significant amounts of these components, especially the tocopherols and sterols, are lost to various intermediate byproducts and waste streams, which include acidulated soapstocks, deodorizer distillates, or both, depending on the refining method selected. Accordingly, numerous methods have been proposed for recovering fatty acids, tocopherols, and sterols from various refining intermediates, including deodorizer distillates that are obtained as byproducts of a high-temperature distillation step commonly termed deodorization during the production of oils and fats.
Deodorization is usually the final step in producing oils and fats from plant and animal sources. Vegetable oils such as soybean oil typically contain volatile impurities that can impart objectionable odor and taste. These volatile compounds generally must be removed to produce edible oils. Deodorization generally involves a steam stripping process wherein steam is contacted with oil in a distillation apparatus operating at low pressure and a temperature sufficient to vaporize objectionable volatile impurities at the operating pressure.
This process, commonly known as vacuum-steam deodorization, relies upon volatility differences between the oil and the objectionable impurities to strip the relatively more volatile objectionable impurities from the relatively less volatile oil. In a typical vacuum-steam deodorizing process, vegetable oil is introduced into a distillation apparatus having a plurality of vertically spaced trays, commonly termed stripping trays.
Within each stripping tray, steam injected into the vegetable oil entrains objectionable volatile impurities. The combined steam and entrained distillation vapors are usually collected and condensed to form a distillate that can be disposed of or processed further to recover valuable materials.
The major constituents of deodorizer distillates are fatty acids, tocopherols, and sterols, which are present in various relative amounts depending on the oil source and the refining steps the oil is subjected to prior to deodorization. Deodorizer distillate itself has a certain commercial value. However, greater value can be realized when deodorizer distillate is split into a fatty acid-enriched fraction and a fraction enriched in sterols and tocopherols.
Fatty acids isolated from deodorizer distillates are utilized in several nonfood applications and are particularly useful as fluidizing agents for lecithin. Such fatty acids also can be utilized as precursors in a wide variety of molecular synthesis schemes. Typically, the fatty acid portion of deodorizer distillate comprises C 10 -C 22 saturated and unsaturated fatty acids.
Soybean deodorizer distillate in particular contains about 50 percent by weight fatty acids. Deodorizer distillates also contain sterols, which are valuable precursors in the production of hormones.
Stigmasterol is used in manufacturing progesterone and corticoids. Sitosterol is used to produce estrogens, contraceptives, diuretics, and male hormones.
The final major component of deodorizer distillates is tocopherol. Tocopherols are valuable natural antioxidants that help prevent oxidation and spoilage. Tocopherols are also utilized in the production of Vitamin E. Alpha tocopherol has the most powerful biological Vitamin E activity. The other tocopherols have weaker Vitamin E activity but stronger antioxidant activity.
If maximum Vitamin E activity is desired, non-alpha tocopherols can be converted into the alpha form by well-known techniques, such as methylation. In the past, recovering tocopherols and sterols from deodorizer distillates and related mixtures has proved complicated and expensive.
Another difficulty is that deodorizer distillate can undergo thermal degradation if it is processed for extended periods at the temperatures at which sterols and tocopherols vaporize, such temperature conditions which can cause fatty acids to convert into undesirable trans isomeric forms.
Numerous methods have been proposed for treating deodorizer distillates to isolate and recover one or more components. In many of these methods, a first essential process step involves subjecting the fatty acids to an esterification or saponification reaction. For example, U. The sterols and tocopherols are then fractionally extracted from the esterification product mixture with a combination of polar and nonpolar solvents. In an alternative esterification method, U. Sterols are then isolated from the residue by subjecting the sterol esters to cleavage under acidic conditions.
The extract is then washed and concentrated, as for example by solvent distillation, and then cooled to crystallize sterols which are removed by filtration, leaving a high purity tocopherol fraction.
The fatty acid soaps formed by the process can be acidulated and converted into free fatty acids. Extractive separation methods also have been employed in treating deodorizer distillates to isolate one or more components.
The raffinate stream and the extract stream are then cooled to a temperature at which the organic components thereof are immiscible with liquid water, whereupon removal of water produces a tocopherol-enriched fraction and a fatty acid-enriched fraction, respectively.
None of the above methods for isolating one or more components from a deodorizer distillate has proved satisfactory, however. Methods employing an esterification step or saponification step introduce processing complexity and require later processing steps that often involve use of strong mineral acids in order to convert the respective esters or soaps into free sterols and free fatty acids. Mineral acids can be dangerous in handling and can induce discoloration or other degradation of distillate components.
Methods requiring extractive steps are expensive and create the potential for contamination by residual solvent. Previously known methods for isolating one or more components from a deodorizer distillate generally have required lengthy and costly processing steps. Consequently, further improvements in methods for treating deodorizer distillates have been sought.
The present invention relates to improved processes having advantages over those previously disclosed. The methods of the invention produce a fatty acid-enriched distillate fraction directly and simply from a vaporized distillate. The methods of the invention also produce a distillate fraction enriched in sterols and tocopherols, which can be treated further by various methods to isolate a sterol fraction and a tocopherol fraction.
One aspect of the present invention relates to methods for isolating one or more components from vaporized distillates obtained from the deodorization of various oils. Another aspect of the present invention relates to methods for producing mixtures enriched in free fatty acids from distillates obtained from the deodorization of various oils.
Yet another aspect of the invention relates to methods for producing mixtures enriched in sterols and tocopherols from distillates obtained from the deodorization of various oils. These and other aspects of the invention will become apparent in light of the detailed description below. The patent or application file contains at least one drawing executed in color. Copies of this patent or patent application publication with color drawing s will be provided by the office upon request and payment of the accessory fee.
Reference numeral 10 of FIG. As illustrated in FIG. The improved processes of the invention can be conducted as batch, semi-continuous, or continuous processes. The improved processes of the invention serve to isolate the components of vaporized distillates obtained from the deodorization of various oils. Many such distillates are suitable for use in the invention, including but not limited to those obtained from the deodorization of soybean oil, corn oil, cottonseed oil, palm oil, peanut oil, rapeseed oil, safflower oil, sunflower seed oil, sesame seed oil, rice bran oil, coconut oil, canola oil, and mixtures thereof.
A particularly suitable distillate is soybean deodorizer distillate. The composition of deodorizer distillates will vary depending upon the oil type and pre-deodorization refining history. Distillate obtained from the deodorization of alkali-refined soybean oil generally contains about 50 percent by weight fatty acids, about 15 percent by weight tocopherols, and about 18 percent by weight sterols.
Distillate resulting from the deodorization of physically refined soybean oil usually comprises about 70 percent by weight fatty acids, about 9 percent by weight tocopherols, and about 11 percent by weight sterols. Distillate obtained from the deodorization of soybean oil refined via an organic acid refining process, as disclosed in U. Any of these deodorizer distillates, concentrated forms of such distillates, or mixtures thereof are suitable for use in the present invention.
Such distillates are best provided in vaporized form in order to minimize the risk of thermal degradation that can occur when a distillate is allowed to cool into a condensate and is then reheated for further processing. The vaporized distillate 20 is introduced into a first condensing zone 30 of a condensing unit 10 having at least two condensing zones and operating at a pressure of less than about 10 mm Hg.
The condensing unit 10 can be any piece of equipment capable of operating at reduced pressure and elevated temperature and having at least two condensing zones. Preferably, the condensing unit 10 is a scrubber fabricated or adapted to contain at least two condensing zones. Reduced pressure can be generated by any convenient source. Steam jet ejector systems are commonly employed. Most preferred is to use a Nash-Kinema three-stage vacuum system or a two-stage vacuum system plus a vacuum pump.
With a three-stage ejector system, the usual vacuum generated in the condensing unit will be from about 4 to about 6 mm Hg. Preferably, the condensing unit 10 operates at a pressure of less than about 6 mm Hg. Most preferably, the condensing unit 10 operates at a pressure of less than about 4 mm Hg. The first condensing zone 30 operates at a temperature less than the boiling point of tocopherols and sterols at the operating temperature but greater than the boiling point of fatty acids at the operating pressure.
Table 1 indicates the boiling point of tocopherols and sterols at several reduced pressures. Within the first condensing zone 30 , a first fraction of the vaporized distillate 20 is condensed to produce a first condensate 40 enriched in sterols and tocopherols, which can be recovered and profitably sold or processed further.
Remaining uncondensed vaporized distillate, termed herein as a remaining fraction of vaporized distillate 50 , flows to a second condensing zone 60 for further processing. Generally, the first condensate 40 is obtained in an amount of about 50 weight percent of the vaporized distillate The first condensate 40 generally comprises about 5 percent by weight fatty acids, about 25 percent by weight tocopherols, and about 30 percent by weight sterols. Optionally, a level controller in the bottom of the first condensing zone 30 maintains a constant volume of the first condensate 40 in the system, with the excess drawn off and sent to storage or subsequent processing steps.
Generally, at least a portion of the first condensate 40 is recirculated into the first condensing zone 30 through a spray nozzle 90 as a mist or spray countercurrent to the flow direction of the vaporized distillate 20 to provide direct cooling upon contact with vaporized distillate 20 as it passes upward. The use of packing substantially increases the surface area in which recycled first condensate and vaporized distillate can interact.
The packing itself also provides an additional source of cooling, since it tends to acquire the temperature of the recycled first condensate. The type of packing is selected based on factors well known to those in the art, including mechanical strength, resistance to corrosion, cost, capacity, and efficiency. The packing may take the form of a stainless steel grid or mesh, porcelain or ceramic rings or saddles, or other suitable inert materials. Preferably, first packing comprises a plurality of sawtooth-profile stainless steel plates spaced closely apart and perforated by a plurality of holes.
The amount of the first packing used depends upon the cross-sectional area of the first condensing zone 30 , the maximum desired pressure drop, the flow rate of vaporized distillate 20 , and the desired percentage conversion of vaporized distillate to first condensate.
Generally, for a first condensing zone 30 having a inch diameter circular cross-sectional area, about 15 vertical inches of first packing are utilized, and the first packing extends substantially throughout the entire cross-sectional area of the first condensing zone The remaining fraction of vaporized distillate 50 exiting the first condensing zone 30 enters the second condensing zone 60 of the condensing unit 10 , where a second fraction of the remaining fraction of vaporized distillate 50 is condensed into a second condensate 70 enriched in fatty acids, leaving a waste vapor The second condensing zone 60 operates at a temperature less than the boiling point of fatty acids at the operating pressure.
Within the second condensing zone 60 , a second fraction of the remaining fraction of vaporized distillate 50 is condensed to produce a second condensate 70 enriched in fatty acids, which can be recovered and profitably sold. The remaining waste vapor 80 , flows to the vacuum system. Generally, the second condensate 70 is obtained in an amount of about 50 weight percent of the original vaporized distillate The second condensate 70 generally comprises about 90 percent by weight fatty acids, and only trace amounts of sterols and tocopherols.
Optionally, a level controller in the bottom of the second condensing zone 60 maintains a constant volume of the second condensate 70 in the system, with the excess drawn off and sent to storage.
Waffles "Zabodayka" milk
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This invention relates to improved methods for refining vegetable oils and byproducts thereof. More particularly, this invention relates to improved processes for producing vegetable oils having reduced content of impurities such as free fatty acids and phosphatides. This invention also relates to an improved process for deodorizing lecithin. This invention additionally relates hydrolyzed lecithin, deodorized lecithin and deodorized vegetable oil obtained by improved processes of the invention. Vegetable oils are typically obtained by pressing or extracting the oil seeds of plants such as corn or soybeans.
EP1357803A2 - Methods for treating phosphatide-containing mixtures - Google Patents
US2434788A - Fat-soluble vitamin concentrates - Google Patents
Vapor phase phospholipid mix produced in rotary film apparatus is removed and filtered out into liquid phospholipid fraction and vapor-gas mix in closed-circuit cycle with the help of vacuum pump. Dehydrated phospholipid concentrate of sunflower-seed oil is discharged as finished product and heated in tank to increase its fluidity. Here used is refrigerator made up of compressor, evaporator and heat control valve. Preheating of phospholipid emulsion and subsequent heating of dehydrated phospholipid concentrate are performed by water. Vapor-gas mix after filter is, first, condensed in refrigerator evaporator to discharge condensate and, then, high-pressure pump is used to force said mix into steam generator, thus making closed cycle.
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Hawthorn Milk Beverage of Juice Concentrate
Sunflower processing capacity. One-time storage capacity our factory. Constant control quality. Is carried out in ourcertified laboratory.
Patented J ao, s Loran 0. Buxton, Newark, N. In other words, the percentage of vitamin found in the extract fraction, and that remaining'behind in the residue has been very much less than 1 the vitamin contained in the original oil. It has now been discovered, however, that if a small quantity of antioxidant is added to marine qoils prior to fractionation, ,whether or not these marine oils have been previously refined in such a manner as to destroy a large proportion of the natural antioxidants or are'the crude, relatively stable oils, a verysubstantial increase in the yields of vitamin A ester in theconcentrate or extract portion and of vitamin content in the residue OCCLII'S j There is further produced in accordance with I the present invention, a, vitamin ester concentrate which is relatively stable, and this is particularly true if an antioxidant is used which is largely soluble in the solvent used for fractionation. The present procass is particularly applicable to' fractionation processes for producingvitamin esters, wherein the solvent used for fractionation is very similar to the solvent usedior the extraction of antioxidants in accordance with theaforementioned It is, therefore, one of the objects of the present invention to fractionate a vitamin-containing marine oil with a solvent capable of extracting a large proportion of the vitamin esters from the marine oil in the presence of a suitable anti- "oxidant. A second object of the present invention is to More particularly, the present invention relates tothe fractionation of vitamin-containing marine oils in order to produce a concentrate consisting largely of vitamin 2 can.
WO2012036695A1 - Process to remove impurities from triacylglycerol oil - Google Patents
Preparation of the test with some improvers. In terms of mechanization and automation of bakery production, the introduction of a continuous process for the preparation of the dough, reducing its fermentation period is particularly important ability to adjust the physical properties of semi-finished products and dough to get the best quality products. Also ways of changing process parameters, is used in the method of adding a semi-finished products of various improvers. This chapter considers the influence of surfactants, enzyme preparations, dairy products and certain other substances to the quality of semi-finished and finished products, as well as methods for their use. The use of surfactants. Among the enhancers used in the baking industry, occupy considerable space surfactants, when added to the semi-finished products change their physical properties.
In the refining of crude vegetable oils, it is conventional to remove phosphatides frequently referred to as lecithin from the oil. This process is commonly referred to as "degumming". Degumming is typically achieved by hydrating the lecithin-containing crude oil and recovering the insoluble hydrated lecithin frequently referred to as wet gum from the oil. A commercial lecithin product is then obtained by drying the wet gum.
US20060204632A1 - Concentrated human milk fortifier liquid - Google Patents
This invention relates to improved methods for treating phosphatide-containing mixtures. More particularly, this invention relates to methods for recovering purified vegetable oil, aqueous organic acid, and organic acid-treated phosphatide from a phosphatide-containing mixture comprising an acid-and-oil mixture obtained from organic acid refining of vegetable oil. Vegetable oils are typically obtained by pressing or extracting the oil seeds of plants such as corn or soybeans. Properly processed vegetable oils are suitable for use in many edible oil and fat compositions destined for human consumption.
FIELD OF THE INVENTION
Drying phosphatide line is indispensable equipment for such technological line as the hydration process. The process of removing phosphate from vegetable oil is needed to improve the quality of the vegetable oils and for a special product - phosphatide concentrate used in various fields. Hydrofusion of capacity E24n N25n pump is supplied to the dryer E63n.
Fat is a concentrated source of energy stored by our bodies as reserve fuel. Fat is an important component of diet and serves a number of functions in the body. Fats like carbohydrates are composed of the three elements carbon, hydrogen and oxygen. The lower amount of oxygen in relation to the other two elements results in fat being a more concentrated source of energy than carbohydrates. Lipids are very wide spread in nature among all vegetable and animal matter.
Preparation of the test with some improvers.
Frank D. Gunstone , John L. Harwood , Albert J. Extensively revised, reorganized, and expanded, the third edition of the industry standard, The Lipid Handbook reflects many of the changes in lipid science and technology that have occurred in the last decade. All chapters have been rewritten, many by new authors, to match the updated thinking and practice of modern lipid science and bring a fresh perspective to twenty years of tradition. New contributions highlight the latest technologies utilized in today's lipid science such as chromatographic analysis and nuclear magnetic resonance spectroscopy.
US6172247B1 - Methods for refining vegetable oils and byproducts thereof - Google Patents
Что это? - вскрикнула Сьюзан между сигналами. - ТРАНСТЕКСТ перегрелся! - сказал Стратмор. В его голосе слышалось беспокойство. - Быть может, Хейл был прав, говоря, что система резервного питания подает недостаточное количество фреона.