• 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:
    Ethylene glycol is prepared by a process in which ethylene oxide is extracted from an aqueous solution with near-critical or super-critical carbon dioxide. Thereafter an ethylene oxide-carbon dioxide-water mixture is contacted with a catalyst to form ethylene carbonate, which is then hydrolyzed to ethylene glycol in the presence of the same catalyst. The ethylene glycol is separated as product and the carbon dioxide and the catalyst are recycled.
    公开号:SU1572414A3
    申请号:SU833605804
    申请日:1983-06-13
    公开日:1990-06-15
    发明作者:С.Байз Виджей
    申请人:Сайентифик Дизайн Компани, Инк (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to organic chemistry, more specifically to a method for producing ethylene glycol from ethylene oxide.
    The purpose of the invention is to simplify the process by eliminating a separate step of purification and purification of ethylene oxide.
    The method is illustrated by the following example.
    Example. In an ethylene oxide reactor at a temperature of approximately 240 ° C and a pressure of 17, these are produced by ethylene oxide by reacting ethylene and molecular oxygen on a supported silver catalyst. The reactor flow is cooled and washed in the column with a recycle stream at a flow rate of 98300 mol / h. The recycle stream contains 99.8% water and 0.14% ethylene glycol. Received 100000 mol / / h solution contain 948 mol / h oxide
    ethylene, a small amount of dissolved gases (ethylene and carbon dioxide), 140 mol / h of ethylene glycol and a small amount of other impurities. The stream is in contact with 41700 mol / h of carbon dioxide at 4h5 C and 85 ati in the extractor with mesh plates. The stripped water stream (101960 mol / / h) includes 2.9% carbon dioxide and 0.14% ethylene glycol. From this stream, 99% of the carbon dioxide in the evaporator is distilled. Carbon dioxide is compressed and returned to the extractor. The distilled solution is returned to the absorber.
    A stream of carbon dioxide enriched in ethylene oxide is returned to the extractor after the pressure is reduced to 60–65 ppm and the removal of a significant part of the carbon dioxide and light impurities. The liquid product (3012 mol / h) contains 31.5% of ethylene oxide, 0.3% of water and traces of impurities. Bearing ratio 1
    Ј
    acid gas to ethylene oxide can be controlled in order to have a mixture suitable for producing these ethylene carbonate. Nedogon from the SP2 separator is combined with a 1970 mol / h recycle stream, which mainly contains ethylene carbonate, as well as about 3 mol% catalyst (methyl triphenylphosphonium iodide) and about 28 mol% solid Stripping. The amount of heavy by-products is insignificant.
    The carbonization reactor maintains a pressure of 63 these and a temperature of 90 ° C. The holding time is 1–5 h, and the conversion of ethylene oxide to ethylene carbonate is 99.5%. tlocne evaporation C02 product stream Contains approximately 68.5 mol% ethylene Carbonate, 27.5 mol% solid side products, 3.2 mol% catalyst, and small amounts of water and lycols. 1620 mol / h of water (ratio of water to carbonate 1.7: 1) are added to this stream and hydrolysis is carried out in a reactor at 150 ° C and a pressure of 63 of these. The ethylene carbonate is converted to monoethylene glycol with a conversion of 98.9%, the rest is diethylene glycol and by-products; 1 mole of tOj is released for each mole of ethylene carbon converted. It is distilled and returned to the reactor. Liquid flow from the reservoir of the Racing contains, they say,%: monoethylenegly — Kohl 930; diethylene glycol 2.8; water 695; heavy by-products 380; Catalyst 44. Water is removed in a distillation column under a pressure of 300 mm Hg. Abs. (bottom) The product contains monoethylene glycol, diethylene glycol and heavy by-products.
    and catalyst. It is subjected to rectification in a column at a pressure of 85 mm Hg. abs (bottom) to remove monoethylene glycol as a head fraction. Diethylene glycol is obtained as the head fraction of the other column. The residue is heavy by-products and catalyst. Approximately 0.4-0.5 mol% of the heavy by-products are evaporated, the rest together with the catalyst is recycled to the process.
    Catalyst loss is compensated by adding fresh catalyst to the stream. This can be carried out periodically or continuously. The yield of the target product is 98.1%.
    The proposed method allows to simplify the process by eliminating a separate stage of separation and purification of ethylene oxide, while maintaining the yield of the target product,
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The method of producing ethylene glycol by reacting ethylene oxide with carbon dioxide and water at elevated temperature and pressure in the presence of a catalyst, followed by separation of the target product, characterized in that as a technical aqueous solution obtained by water absorption of the product of catalytic vapor-phase oxidation of ethylene, which is in contact with carbon dioxide under conditions that are close to critical for carbon dioxide.
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1572414A3|1990-06-15|Method of obtaining ethylene glycol
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    US4663477A|1987-05-05|Process for the hydrolysis of dialkyl carbonates
    US4003952A|1977-01-18|Direct hydration of olefins to alcohols
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    同族专利:
    公开号 | 公开日
    FR2528417A1|1983-12-16|
    US4400559A|1983-08-23|
    AU1564083A|1983-12-22|
    IT1169063B|1987-05-27|
    YU129483A|1986-02-28|
    NO159164B|1988-08-29|
    DE3321448C2|1988-04-21|
    DE3321448A1|1983-12-15|
    NO832140L|1983-12-15|
    FR2528417B1|1986-01-17|
    KR870000542B1|1987-03-18|
    YU44436B|1990-08-31|
    NO159164C|1988-12-07|
    ES8501357A1|1984-11-16|
    JPS5921634A|1984-02-03|
    RO88641A|1986-02-28|
    KR840005062A|1984-11-03|
    NL8302020A|1984-01-02|
    SE8303324D0|1983-06-13|
    DD210026A5|1984-05-30|
    IN159399B|1987-05-16|
    ES523213A0|1984-11-16|
    IT8348494D0|1983-06-13|
    GB2122614A|1984-01-18|
    BR8303125A|1984-01-31|
    BE897039A|1983-12-13|
    GB8316153D0|1983-07-20|
    CA1219602A|1987-03-24|
    SE459089B|1989-06-05|
    MX157512A|1988-11-28|
    CH656871A5|1986-07-31|
    ZA834364B|1985-02-27|
    GB2122614B|1986-03-19|
    JPS6327333B2|1988-06-02|
    AR241527A1|1992-08-31|
    AU556132B2|1986-10-23|
    SE8303324L|1983-12-15|
    EG16051A|1990-10-30|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/388,395|US4400559A|1982-06-14|1982-06-14|Process for preparing ethylene glycol|
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