• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Disclosed is a process for the production from raw lecithin of pure lecithin directly usable for physiological purposes, comprising the steps of contacting raw lecithin with gas as the extraction medium under supercritical conditions with respect to pressure and temperature in an extraction stage to produce a gas containing an extract; passing the gas containing the extract from the extraction stage into a separation stage; varying at least one of the pressure and the temperature of the gas in the separation stage to separate the extract-containing gas into the gas and the extract; recycling the gas after the step of varying the pressure and/or temperature; and removing pure lecithin from the extraction stage.
    公开号:SU984412A3
    申请号:SU813257549
    申请日:1981-03-05
    公开日:1982-12-23
    发明作者:Хайгель Вальтер；Хюшенс Рольф
    申请人:Кали-Хеми Фарма Гмбх (Фирма)；
    IPC主号:
    专利说明:

    WAY OF CLEANING LECITHIN
    (
    This invention relates to the chemistry of organophosphorus compounds, namely. to a new method of purification of lecithin, which is used for the manufacture, processing and preservation of products. nutrition and for the preparation of cosmetic and pharmaceutical preparations, in connection with which high quality requirements are placed on the quality of lecithin. 10
    By lecithins is meant the group of substances belonging to the phosphatide range. These are compounds containing phosphorus in the form of phosphoric acid ester, which can be obtained by processing certain fat-containing plant and animal products.
    A known method for producing lecithin from phosphatide concentrates of beans of soybean and sunflower is treated twice with acetone, filtered, followed by extraction of the precipitate twice with ethanol and evaporation of the solvent. You get raw lecithin in
    as a semi-solid pasty material, which consists of 60-70% phosphatides and oil 1.
    However, for further processing and technical use of lecithin, a minimum content of oil in it is necessary.
    The closest in technical essence and the achieved result to the proposed method is a method of cleaning raw lecithin cheese by extracting it with ethanol, separating lecithin from ethanol by decantation and returning ethanol in process 2.
    However, the known method does not completely remove lecithin. oils. The content of the latter in the target product is.
    The aim of the invention is to increase the purity of lecithin.
    The goal is achieved by the fact that according to the method of purifying lecithin, crude lecithin is treated with carbon dioxide at a temperature of 31 ° C and a pressure of 72-600 atm, 3 g of pure lecithin is separated from carbon dioxide containing extract, carbon dioxide is separated from the extract at a temperature of 15 31, 3 C atm pressure and return it to the process. The proposed method allows the HocTbfo floor to clean the crude lecithin from oily impurities, thereby making it possible to use it in the production of pepper products for the preparation of pharmaceutical and cosmetic preparations. The drawing is a diagram for implementing the method. The method is carried out as follows. Crude lecithin is placed in an extraction stage 1. The air is not forced out of the system, and an extracting agent, carbon dioxide, is injected through the inlet valve 2, which is then fed through a heat exchanger 3 to the compressor. o After the pressure and temperature required in the extraction stage 1 have been reached, the inlet valve 2 is closed and carbon dioxide is fed into it. Next, carbon dioxide, containing the extract, is fed to the sifting device 5, which prevents the capture of solid components, then through the throttle valve 6 and the heat exchanger 7- to the separation stage 8, where the extract and extractant are stratified. The latter, through heat exchanger 3, is introduced into compressor k and again into extraction stage 1. The extract is removed from separation stage 8 through gateway 9 or, after completion of npotiecca, is removed from it. Pure lecithin is drawn from extraction stage 1. Extraction-stage 1 and separation stage B are made in the form of thermostatically controlled autoclaves so that with additional thermostating it is possible to precisely set the temperature in these process steps. If the extraction stage 1 consists instead of one of two or more autoclaves, the proposed method can be carried out continuously. In this case, it is possible to extract lecithin from one tank and reload it with fresh substrate, while the extraction can be continued continuously in another or other autoclaves at an extractive stage. At the same time it is possible to include separate tanks in parallel or in series. For the latter case, a countercurrent extraction process is particularly advantageous, i.e. in the autoclave containing the extracted substrate, feed from the compressor k an extracting agent and, accordingly, always include an autoclave containing the freshest substrate, as the last link in the extraction stage. The examples show the following process parameters. Extraction pressure P-j, temperature T. level:. Separation pressure Pj, tempestration:. Peru T2. Example 1. 1000 g of raw lecithin paste is placed in an extraction stage, closed, and the extraction process is carried out with carbon dioxide at 400 atm. supercritical conditions: Р Т 60 ° С ;, Р 50 atm, Tq. Extraction time 4h. 580 g of a solid light-colored, yellow substance — pure lecithin, which is extracted from the extraction vessel are obtained. about 30% of the oil is placed in the extraction stage, closed, and carbon dioxide is extracted under the following conditions: P 300 atm, T., P,., O -, Tj 20 ° C. The extraction time is 6 hours. A precipitate remains in the extraction stage — b9 g of pure lecithin in the form of a solid, light yellow non-hygroscopic substance. In the separation step, 31 g of a yellow clear oil is present. The products of both examples are free of oil components according to thin layer chromatography. Example 3. 100 g of raw lecithin in the form of a paste is placed in an extraction stage, closed, and extraction is carried out with carbon dioxide at P 600 atm, T | , P 50 atm, Tj 22C. Extraction time 4h. In the extraction step, 69 g of pure lecithin remain as solid (
    权利要求:
    Claims (1)
    [1]
    The method of purification of lecithin using extraction, characterized in that, in order to increase the purity of the target product, crude lecithin is treated with carbon dioxide at a temperature of 31.3 "80 a C and a pressure of 72-600 bar, clean lecithin from carbon dioxide extract containing carbon dioxide, carbon dioxide is separated from the extract at a temperature of 1531, W d C and a pressure of 30-72 atm and return it to the process.
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    同族专利:
    公开号 | 公开日
    IT1135364B|1986-08-20|
    IL62025D0|1981-02-27|
    PT72478B|1982-02-05|
    BE887863A|1981-07-01|
    DK126381A|1981-09-23|
    DE3011185A1|1981-10-01|
    IL62025A|1984-05-31|
    FI67477B|1984-12-31|
    US4367178A|1983-01-04|
    FI810799L|1981-09-23|
    GR74833B|1984-07-12|
    IT8119594D0|1981-02-09|
    CH648765A5|1985-04-15|
    FI67477C|1985-04-10|
    PH17788A|1984-12-13|
    NZ196304A|1982-12-07|
    ATA132781A|1985-10-15|
    AT380479B|1986-05-26|
    NO161118C|1989-07-05|
    CA1153776A|1983-09-13|
    NL8100382A|1981-10-16|
    NO161118B|1989-03-28|
    FR2478643A1|1981-09-25|
    IE810257L|1981-09-22|
    GB2072189B|1983-06-22|
    AU537973B2|1984-07-19|
    SE8101622L|1981-09-23|
    IE50893B1|1986-08-06|
    DE3011185C2|1988-01-28|
    PT72478A|1981-03-01|
    DD157560A5|1982-11-17|
    SE456997B|1988-11-21|
    GB2072189A|1981-09-30|
    NO810957L|1981-09-23|
    ES499169A0|1981-12-16|
    HU188003B|1986-03-28|
    ES8201589A1|1981-12-16|
    AR222130A1|1981-04-15|
    JPS56145295A|1981-11-11|
    AU6767381A|1981-10-01|
    ZA81446B|1982-02-24|
    FR2478643B1|1985-07-12|
    引用文献:
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    RU2673716C2|2013-10-30|2018-11-29|Карджилл, Инкорпорейтед|Method for the purification of lecithine|DE1493190C3|1963-04-16|1980-10-16|Studiengesellschaft Kohle Mbh, 4330 Muelheim|Process for the separation of mixtures of substances|
    DE2127596A1|1971-06-03|1972-12-21|Hag Ag, 2800 Bremen|Process for the production of vegetable fats and oils.|
    US3923847A|1973-05-23|1975-12-02|Studiengesellschaft Kohle Mbh|Methods of producing cocoa butter|
    JPS5410539A|1977-06-24|1979-01-26|Matsushita Electric Works Ltd|Door|
    DE2843920A1|1978-10-09|1980-04-10|Krupp Gmbh|METHOD FOR TREATING RAW PLANT FATS AND OILS|DE3207914A1|1982-03-04|1983-09-15|Skw Trostberg Ag, 8223 Trostberg|METHOD FOR EXTRACTIVELY OBTAINING HIGH QUALITY NATURAL WAXES|
    US4466923A|1982-04-01|1984-08-21|The United States Of America As Represented By The Secretary Of Agriculture|Supercritical CO2 extraction of lipids from lipid-containing materials|
    DE3229041C2|1982-08-04|1990-05-10|Lucas Meyer Gmbh & Co, 2000 Hamburg, De|
    US4568495A|1983-05-16|1986-02-04|Union Camp Corporation|Fractionation of polymerized fatty acids|
    DE3329249A1|1983-08-12|1985-02-21|Skw Trostberg Ag, 8223 Trostberg|METHOD FOR EXTRACTION OF FORMABLE FLOWABLE MEASURES|
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    US4714571A|1984-02-13|1987-12-22|The Liposome Company, Inc.|Process for purification of phospholipids|
    DE3411755A1|1984-03-30|1985-11-07|Lucas Meyer GmbH & Co, 2000 Hamburg|METHOD FOR OBTAINING LECITHIN, PREFERABLY FOR CONTINUOUSLY OBTAINING PURE LECITHIN |
    JPH0437838B2|1984-04-21|1992-06-22|Q P Corp|
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    US4762658A|1986-10-08|1988-08-09|Central Soya Company, Inc.|Method of tableting of de-oiled phosphatides |
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3011185A|DE3011185C2|1980-03-22|1980-03-22|
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