• 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:
    A METHOD OF CONTINUOUS SEMIUM OF SECONDARY BUTYL ALCOHOL by hydrating n-butene on a fixed layer of an acidic cation exchanger at elevated temperature and pressure when the raw material is fed upwards through a fixed layer of cation exchanger followed by processing the vapor product obtained in the upper part of the reactor in order to improve the quality of the target product, the resulting vapor stream is throttled to a pressure of 5-60 atm, cooled at this pressure to 20-135 ° C to obtain a two-phase liquid system, aqueous The latter, which is removed from the system, and the organic, containing butenes, butanes, and the target. secondary butyl alcohol, is evaporated when heated and fed to the rectification stage, where, at a pressure of 6.5-8 atm, a mixture of butenes and butanes is separated as distillate. output from the system, and the target product as a bottom product. spz-
    公开号:SU1106445A3
    申请号:SU813346098
    申请日:1981-10-28
    公开日:1984-07-30
    发明作者:Нейер Вильгельм；Веберс Вернер；Рукхабер Райнер；Остербург Гюнтер；Оствальд Вольф
    申请人:Дойче Тексако Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to an improved method for producing lower alcohols, in particular, to a method for continuously producing secondary butyl alcohol, which can be used as a solvent. A known method for producing butyl alcohols by hydration of butenes at a molar ratio of water: butenes active 0.06-0.24. 1, in the presence of an acidic cation exchanger as a catalyst when the feedstock is fed from top to bottom through the catalyst bed, to produce a vapor stream of product in the lower part of the reactor, which is divided into two Asti, a first output to the step of isolating the desired product by distillation, and the other is cooled and fed to the hydration step. Butyl alcohol does not contain water. The selectivity of the process to the target product is 12.8-60.7% 1. The disadvantage of this method is the low selectivity of the process to the desired product (12.8-60.7%). A known method for the continuous production of lower alcohols by hydration of n-buttrans. Consists in the fact that: through a fixed layer of cation exchanger, an olefin-containing vapor stream is fed upwards with a ratio of reactants equal to at least 1 mol of water per 1 mole of olefin; the reaction is carried out at a temperature and pressure that is slightly below or above the critical values of the olefin used; the aqueous phase of the reaction mixture is completely left in the reaction zone or the majority of this phase is recycled to the reaction zone; a vapor stream containing unreacted olefin and almost all of the reaction product is withdrawn from the top of the reactor, and unreacted olefin fed to the reactor and the crude liquid product, mainly consisting of the alcohol formed, is recovered by stripping the vapor stream, for example, by depressurizing 2. A disadvantage of the known method is that the resulting secondary butyric alcohol contains OKO 10% of water, which must be removed by distillation drying before the recycled alcohol, for example, to produce methyl ethyl ketone. The purpose of the invention is to improve the quality of the secondary butyl alcohol obtained (by reducing the water content). The goal is achieved by the method of continuously producing secondary butyl alcohol by hydrating n-butene on a fixed bed of acidic cation exchanger at elevated temperature and pressure when the raw material is fed from below up through the fixed bed of cation exchanger to produce a vapor stream of the product, the latter is throttled to a pressure of 5-60 atm, cooled at this pressure to 20-135 ° C to obtain two The hot liquid system, the aqueous layer of which is removed from the system, and the organic, containing butenes, butanes, and the target secondary butyl alcohol, is evaporated when heated and fed to the rectification stage, where at a pressure of 6.5-8 atm distillate mixture of butenes and butanes, which is removed from the system, and the target product as a bottom product. The proposed method allows to obtain a secondary buti, a new alcohol containing less than 0.1% water. The drawing shows an installation for carrying out the proposed method. Using the metering pump 1, the feed gas supplied through the pipeline 2 is mixed with the circulating gas supplied through the pipeline 3, evaporated in the evaporator 4 and fed through the pipeline 5 to the reactor 6. Through the pump 7, water is supplied to the reactor 6 through the pipeline 8 after preheating in the heat exchanger 9. The reactor contains a fixed bed of cation exchanger based on styrene and divinylbenzene. Both reagents are passed from bottom to top through a fixed bed of catalyst. A steam stream is withdrawn from the top of the reactor through line 10, containing the 1st produced alcohol and excess feed gas (butane / n-butenes). This stream is throttled to a pressure of 560 atm and passed through heat exchangers 11 and 12, where it is cooled.
    权利要求:
    Claims (1)
    [1]
    METHOD FOR CONTINUOUS PRODUCTION OF SECONDARY BUTYL ALCOHOL by hydration of n-butene on a fixed bed of acidic cation exchange resin at elevated temperature and pressure while supplying the feedstock from the bottom up through a fixed bed of cation exchange resin followed by processing of the vapor product obtained in the upper part of the reactor, characterized in that, c In order to improve the quality of the target product, the resulting vapor stream is throttled to a pressure of 5-60 atm, cooled at this pressure to 20-135 ° C to obtain a two-phase liquid system, the water layer of which It is removed from the system, and the organic one containing butenes, butanes and target. Secondary butyl alcohol is evaporated by heating. § They are fed to the rectification stage, where at a pressure of 6.5-8 atm a mixture of butenes and Λ butanes is isolated as distillate. deduced from the system and the target product as a cubic £ product.
    1 106445
    类似技术:
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    同族专利:
    公开号 | 公开日
    TR21194A|1983-12-08|
    AU543310B2|1985-04-18|
    NO155001B|1986-10-20|
    PL128874B1|1984-03-31|
    YU41798B|1987-12-31|
    DD201769A5|1983-08-10|
    RO82951A|1984-01-14|
    EP0051164A1|1982-05-12|
    RO82951B|1984-01-30|
    CS221298B2|1983-04-29|
    EP0051164B1|1983-12-14|
    AU7681281A|1982-05-06|
    YU258781A|1983-02-28|
    FI74701B|1987-11-30|
    FI813070L|1982-05-01|
    BR8106920A|1982-07-13|
    AR224968A1|1982-01-29|
    JPS5799540A|1982-06-21|
    CA1192916A|1985-09-03|
    NO813497L|1982-05-03|
    DE3040997C2|1983-07-21|
    ZA816554B|1982-09-29|
    DE3040997A1|1982-05-19|
    IN155461B|1985-02-02|
    FI74701C|1988-03-10|
    JPS6261573B2|1987-12-22|
    ES505769A0|1982-08-16|
    NO155001C|1987-01-28|
    PL233641A1|1982-06-21|
    DE3161653D1|1984-01-19|
    DK480881A|1982-05-01|
    US4476333A|1984-10-09|
    MX154625A|1987-11-04|
    ES8205741A1|1982-08-16|
    AT5581T|1983-12-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2144750A|1934-03-05|1939-01-24|Shell Dev|Process for the production of hydrated olefines|
    NL288077A|1962-01-24|1900-01-01|
    DE2429770C3|1974-06-21|1981-04-16|Deutsche Texaco Ag, 2000 Hamburg|Process for the production of lower alcohols by direct catalytic hydration of lower olefins|DE3512518A1|1985-04-06|1986-10-09|Deutsche Texaco Ag, 2000 Hamburg|METHOD FOR THE CONTINUOUS PRODUCTION OF LOW ALCOHOLS|
    DE3728428A1|1987-08-26|1989-03-09|Texaco Ag|METHOD FOR DISTILLATIVE CLEANING OF RAW SEC-BUTYL ALCOHOL|
    IT1223016B|1987-10-29|1990-09-12|Enichem Anic Spa|PROCESS FOR THE DIRECT HYDRATION OF LINEAR OLEFINS|
    CN1057075C|1997-09-10|2000-10-04|中国石油化工总公司|Process for producing low carbon alcohol by directly hydrating low carbon olefines|
    US6563006B2|2001-04-30|2003-05-13|Melvin K. Carter|Catalytic oxidative conversion of hydrocarbons to aldehydes|
    DE102008000785A1|2008-03-20|2009-09-24|Evonik Röhm Gmbh|Process for the preparation of methacrylic acid|
    US20110136926A1|2009-12-08|2011-06-09|Jianguo Cai|Catalysts for Olefin Hydration and Method of Preparation|
    US8558036B2|2010-11-15|2013-10-15|Saudi Arabian Oil Company|Dual phase catalysts system for mixed olefin hydrations|
    US9187388B2|2012-09-05|2015-11-17|Saudi Arabian Oil Company|Olefin hydration process using oscillatory baffled reactor|
    US10155707B2|2012-09-05|2018-12-18|Saudi Arabian Oil Company|Olefin hydration process using oscillatory baffled reactor|
    US9732018B2|2014-02-11|2017-08-15|Saudi Arabian Oil Company|Process for production of mixed butanols and diisobutenes as fuel blending components|
    CN103910601B|2014-04-22|2015-07-22|凯瑞环保科技股份有限公司|Method for producing monohydric alcohol from water and olefins|
    EP2939995A1|2014-04-30|2015-11-04|Sasol Solvents Germany GmbH|Improved water management for the production of isopropyl alcohol by gas phase propylene hydration|
    CN104475109A|2014-11-20|2015-04-01|北京恩泽福莱科技有限公司|Catalyst for preparing sec-butyl alcohol and preparation method of catalyst|
    CN106669375B|2015-11-09|2020-06-05|中国石油化工股份有限公司|Process for treating tail gas of methyl ethyl ketone device|
    CN107459442B|2016-06-03|2020-12-29|中国石油化工股份有限公司|Sec-butyl alcohol production device and process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3040997A|DE3040997C2|1980-10-31|1980-10-31|Process for the continuous production of sec-butyl alcohol|
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