• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Tertiary aliphatic methylamines of the formula I, which have 1 to 2 long-chain alkyl or alkenyl radicals having 8 to 24 C atoms, are prepared by reacting the corresponding alcohols and/or aldehydes with primary or secondary methylamines in the liquid phase under virtually pressure-free conditions. In this process, a hydrogen/amine mixture, where the amine accounts for 1 to 20% by volume, is circulated. The reaction is carried out in the presence of a cobalt chromite or copper chromite catalyst. The water of reaction is removed from the circulating gas. The resulting amines can be used as intermediates. <IMAGE>
    公开号:SU745359A3
    申请号:SU762388321
    申请日:1976-08-05
    公开日:1980-06-30
    发明作者:Штраус Юлиус；Хюбнер Херберт；Мюллер Хайнц；Кремпль Энгельберт
    申请人:Хехст Аг (Фирма)；
    IPC主号:
    专利说明:

    (54) METHOD FOR OBTAINING TERTIARY ALIPHATIC
    one
    This invention relates to an improved production method. tertiary aliphatic amines, valuable products of organic synthesis.
    In the patent and technical literature, various methods for the preparation of tertiary amines are known, for example, by reductive alkylation of amines with aldehydes or ketones in the presence of i3 hydrogenation catalysts.
    The closest to the described method to the technical nature is the method of obtaining tertiary. amines by reacting an excess of aliphatic alcohol 04-022 with a substituted or unsubstituted amine c. the presence of hydrogen at 90–230 ° C and a pressure of 1–5 MPa, with continuous removal of water formed during the reaction, from the waste gas and its continuous return to the beginning of the 2J process. ,
    The yield of the target products does not exceed 69.5%.
    The disadvantage of this method is the relatively low yield and purity of the target products.
    The purpose of this method is to eliminate this disadvantage and AMONGES.
    2
    c) Observe the yield and purity of the target products.
    This goal is achieved by the use of cobalt and / or copper-chromium catalysts with a copper content of 27.5-79% and a chromium content of 45 to 1% as catalysts for the process. Moreover, copper-chromium oxide catalysts could also contain additives of oxides of metals I and II of the main groups of the periodic system in an amount of 0.1-10.0%, calculated on the metal, and interact with an oxygen-containing compound of the formula or aliphatic aldehyde of the formula Rj — C O, where an aliphatic residue containing from 7 to 23 carbon atoms is subjected
    Sfr gaseous mixture consisting of hydrogen and a primary or secondary amine of the formula H-NR2CH3, de
    or ,
    CyH-j
    CHg CgHg
    and the proportion of amine in this gas mixture is from 1 to 20% by volume. . Preferably, a portion of the waste gas, before being recycled to the liquid phase, is replaced by a mixture of hydrogen and amine, preferably 30-40 vol.%, Of hydrogen, with an inert gas. AT
    As the oxygen-containing compound, an alcohol, aldehyde, or mixture of an alcohol or aldehyde with a carbon number of 7 to 2 3 is preferably used.
    The method according to the invention consists in placing the appropriate alcohol, aldehyde or mixture thereof in a heated stirred reactor which is equipped with a device for circulating an amine-hydrogen mixture, as well as for withdrawing water from the cycle, while vigorously stirring and passing the amine hydrogen mixture. Heated to 1bO-230 ° C, prioritized to 190210 ° C. After completion of the reaction, the catalyst is filtered off and the resulting tertiary amines are distilled off.
    Some of the hydrogen in the circulating gas may be replaced with an inert gas, such as nitrogen or methane.
    Example 1. The reaction is carried out in the apparatus shown in the drawing. The apparatus consists of a 100 l reactor with a stirrer with a capacity of 100 l with a built-in packed column 2, a circulating gas compressor 3 and a piping for circulating gas 4 for mixing gaseous amine gas, hydrogen and under known conditions of inert gases, a cooler 5, separator b for water and volatile components Parts, as well as supplies for the amine 7 H, 8 and under known conditions Nj 9 (as a washing agent or under known conditions as an inert gas additive) and from pipeline 10 for evacuating off gas ov The heating and cooling of the reactor is carried out through the jacket 11. From the cooler 5 there is a conduit 12 to the reactor 1, through which the organic phase 14 can be recycled, separated from the aqueous phase 13.
    In a heated reactor with a stirrer with a capacity of 1.m, 500 kg (2.68 per mole) of dodecanol-1 and 20 kg of a copper-chromite catalyst (41% Cu 31% Cr; 0.3% Ba) were introduced. The equipment through the pipeline 9 is flushed with nitrogen, heated with stirring, the nitrogen through the supply 8 is ignited with hydrogen and activated by the Compressor. The circulating gas is introduced into the 3,200 hydrogen cycle and at 150s the dimethylamine is fed through the supply 7. The reaction starts at 150 ° C and proceeds optimally at 200-210 ° C with a noticeable cleavage of water. The concentration of dimethylamine in the cycle set with the help of dosing and measuring devices 5-7 vol.%. Since small amounts of gaseous by-products are formed during the reaction, 10% of the free volume of the circulating gas (1 m) is continuously injected through (10) and replaced with fresh gas. In the assembled column 3 with a condenser 5 in the reactor, the mixture of amine with alcohol is divided on the one hand and the reaction water on the other. In the separator B, the organic phase is separated from the aqueous phase and the upper (organic) phase is reintroduced into the cycle in the column.
    After 6 hours the reaction is complete and
     53 liters of aqueous phase are separated after cooling to 100 ° C and washing with nitrogen and the mixture is filtered from the catalyst through a rotating filter. This is highlighted. 553 kg of crude amine
    0 with an amine number of 44.7 (theoretically 46.8).
    After distillation, the yield of the pure product is 92.5% with respect to the starting alcohol, with a degree
    5 purity 98%.
    EXAMPLE 2 500 kg of dodecanol-1 is converted in the same apparatus as in Example 1 under the same conditions. Additionally reactive
    The Q product is pumped, for which it is removed from the bottom of the reactor and re-introduced into the gas phase of the reactor.
    After distillation, get 98,5%
    5 dimethyldodecilam n with a general approach of 93.5% in relation to the initial alcohol, and 94.6% in 6 tnts} enyu To the initial dimethylamine ..
    Example 3. A-D. In laboratory equipment consisting of a flask
    0 with a 1 liter mixer with a thermostatted cooler, an attached condenser and a separator for separating the reaction water, 1 mol of dodecanol-1 is preliminarily placed
    5 and 4% copper-chromite catalyst (as in example 1). The stirrer is activated and the mixture in the flask is heated to nitrogen by passing nitrogen. From steel cylinder
    0 through capillaries and gas meter
    Pass various mixtures of hydrogen, dimethylamine and nitrogen through a reaction product and through a cooler into a hood. Amount of gas
    J mixtures were kept constant and the reaction temperature was set at 210c. The results for different gas mixture compositions can be seen from the table below.
    E. In a 100 liter reactor with a mixer, 50 kg- (240 mbl) of synthetic alcohol are placed with a distribution of 33% C, 2, 64% C | 4I 3% C 10 and C 1 and 2 kg of a copper-chromite catalyst (similarly example 1). The reactor is rinsed with nitrogen with stirring and the introduction of circulating hydrogen gas, heated for ½ hours to 160 ° C and then dimethylamine is added. The amount of circulating gas is 12 and the concentration of dimethylamine in the circulating gas is 5-10%. After 7 hours at 205-210c, the reaction is complete. During the subsequent vacuum distillation of the crude amine, 5.2% of the residue remains. Distilled dimethyl-C | 0. li, alkylamine
    . Contains 0.4% alcohol and 0.6% primary and secondary amine. The total yield is 91.3% based on alcohol and 93.4% based on the dimethylamine added.
    G. Proceed in a similar manner to item E with the difference that the concentration of dimathylamine in the cycle is 1520% volumes. The reaction is completed after 8 hours. After treatment, 12.4% of the residue remains in the reactor. The yield of 97.5% dimethyl-C | (., Α-alkylamine is 83.5%, based on alcohol, and 80.7%, based on the used dimethylamine.
    Example 4. Analogously to Example 3, 50 kg of isooctyl alcohol (a mixture of branched C-alcohols, obtained from the oxosynthesis of pure heptene through codimerization of butene and propylene) in the presence of the copper-chromite catalyst of Example 1 is brought into contact with dimethylamine. Due to the low boiling accuracy, isooctanol (180-185 ° C) is operated at elevated pressure (3-4 bar). The reaction temperature is 195-200s, the amount of circulating gas is 20 m® / h and the concentration of dimethylamine in the circulating gas is 6-8% by volume. The product and water are discharged from both sides of the column, separated in a separator and the organic phase is reintroduced into the reactor. After 8 hours, when 7.8 liters of water containing amine are released, the reaction
    0 is ending. Dimethylisooctylamine is obtained in a total yield of 91.8%, based on alcohol, and 98.5% based on the equivalent of a tertiary amine.
    Example 5. Similarly to Example 5 of 3, 50 kg of octenol (oleic alcohol with a iodine number of 92% is introduced into I reacting with dimethylamine in the presence of 2 kg of catalyst 1 example. The reaction temperature was 0 I et the circulating i gas is 14 and the concentration of amine in the circulating gas is 4-6% by volume, 10% by volume of the circulating gas is replaced every hour by 5 with fresh gas. After 5.5 hours the reaction is completed. 3 liters of water are separated. distillations provide pure dimethyl oleyl amine with a yield of 93.4%.
    Example 6. In the laboratory apparatus described in example 3,
    0 300 g (1.6 mol) of dodecanol and 12 g of cobalt catalyst (45% of cobalt on kieselguhr) are preliminarily placed. The mixture in the flask 5 is heated to 100 ° C while stirring and passing nitrogen, the nitrogen is displaced by hydrogen, and dimethylamine is added at an internal temperature of 195 ° C. Pass through the reaction product gas
    The mixture contains 100 liters of hydrogen and 5 liters of dimethylamine, the reaction temperature is 195-19s. After reaction for 8 hours and separation of 27.5 ml of water, the reaction is terminated and the reaction mixture is filtered off from the catalyst. After distillation, dimethyldodecylamine is obtained with purity,. 94.7%. The residual alcohol content is below 0.1%.
    0
    权利要求:
    Claims (1)
    [1]
    1. The method of producing tertiary ali 65 fatic amines by the interaction
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    同族专利:
    公开号 | 公开日
    CA1101889A|1981-05-26|
    FI62822C|1983-03-10|
    ES450344A1|1977-08-16|
    FR2320287A1|1977-03-04|
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    AU509878B2|1980-05-29|
    GB1538138A|1979-01-10|
    CH622237A5|1981-03-31|
    FR2320287B1|1983-01-28|
    NO142709B|1980-06-23|
    PL106214B1|1979-12-31|
    MX143899A|1981-07-31|
    LU75536A1|1977-04-20|
    DK145493B|1982-11-29|
    IT1065117B|1985-02-25|
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    引用文献:
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    DE500692C|1925-05-24|1930-09-05|I G Farbenindustrie Akt Ges|Process for the production of pure iron|
    US2597701A|1948-12-06|1952-05-20|Gen Aniline & Film Corp|Method of producing finely divided metals|
    DE824198C|1949-10-22|1951-12-10|Basf Ag|Process for the production of iron powder|
    DE833955C|1950-01-03|1952-03-13|Basf Ag|Production of coarse-grained metal powders|
    US2612440A|1950-05-03|1952-09-30|Gen Aniline & Film Corp|Production of metal carbonyl powders of small size|
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    DE1433361A1|1964-11-26|1968-12-12|Friedenberg Serafima E|Process for the production of highly dispersed carbonyl iron powder|BE530219A|1976-05-14|
    DE2621449C3|1976-05-14|1988-07-07|Basf Ag, 6700 Ludwigshafen, De|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2535073A|DE2535073C3|1975-08-06|1975-08-06|
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