• 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:
    1. A process for esterifying acetic acid with an alcohol of 4 or more carbon atoms or with a glycol ether in the presence of a finely divided, strongly acidic ion exchanger in a vertical reactor with distillative separation of the resulting reaction mixture, characterised in that the esterification is carried out in a vertical reactor with descending or ascending flow, the reaction mixture leaving the reactor is introduced into the upper half of a downstream distillation column, the reactor is operated flooded with the aid of a pressure overflow valve between the reactor and distillation column, the water is removed azeotropically with an entraining agent via the top of the column, the ester formed is taken off as vapour below the first column tray, the unconverted amounts of acetic acid and alcohol are recycled to the esterification reactor after having been separated off by distillation and replenished with fresh quantities of acetic acid and alcohol corresponding to the amount of the ester taken off below the first column tray, and the high-boiling products formed are continuously taken off as liquid from the base of the column.
    公开号:SU1240352A3
    申请号:SU833642950
    申请日:1983-09-19
    公开日:1986-06-23
    发明作者:Альфс Гельмут；Бекскес Вернер；Вангермайн Эрвин
    申请人:Хемише Верке Хюльс Аг (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to a process for the preparation of acetic acid esters, which can be used as solvents.
    The aim of the invention is to increase the productivity of the process by changing the direction of flow,
    The drawing shows an installation that implements the proposed method
    The installation contains a dosing vessel 1, where pipelines 2 and 3 supply acetic acid and alcohol or glycol ether, receiver 4, heat exchanger 5, vertical reactor 6 operated in flooding mode, and distillation column 7 connected to reactor 6 through a pipe 8 with a discharge valve 9 placed in it; the receiver 4 is connected to the heat exchanger 5 through a pipe 10 with a dosing pump 11 placed in it and equipped with a pipe 12 through which a mixture of unreacted acetic acid is discharged from the column 7 alcohol or glycol ether. The upper part of the distillation column is equipped with a 13 Phase separator containing an azeropic agent, for example toluene, and its lower part is equipped with a pipe 14 for withdrawing the product and a capacity of 15 to receive high boiling point components supplied to the receiver 16. Phase 13 separator It is equipped with a conduit 17 for draining water separated from the azeotroping agent and a conduit 13 for recycling to the azeotroping agent column 7.
    PRI EMERA 1 .. Ethyl monoglycolic ester of acetic acid,
    A pipe with a diameter of 35 mm and a height of 65 cm supplied with a heated jacket is loaded with 150 g of dry, swollen in ethyl monoglycol ether to a constant volume of a strongly acidic cation exchanger of the SShch 118BG brand, having an exchange capacity in the dry state equal to 4.2 mEq / g to which enters popystirolsulfonic acid, crosslinked May 18, D divinylbenzene, (grain size 0.3-1.3 mm). the swollen catalyst is 480 cm. The catalyst bed is located on a VA stainless steel grid with 0.3 mm openings so that the removal of the catalyst from the reactor during
    the esterification reaction is prevented. 600 g / h of a mixture of ethyl monoglycol ether and acetic acid in a molar ratio of 1.1: 1 from receiver 4 is delivered to reactor 6 by means of a dosing pump 11 through heater 5, in which it is heated to 115 G. From the heater, the mixture is passed through a reactor from top to bottom, the reaction temperature is 115 s. Using a pressure relief valve 9 in the reactor, a pressure of 2 bar is established. The liquid mixture of etherification coming out of the reactor is fed to the upper half of the addition column 7 connected to the reactor with a diameter of 50 mm and a length of 180 cm (nozzle in the form of rings with a diameter of 6 mm) ,. the temperature in the cube of which is 158-1bO s, the reaction water is distilled off as an azeotrope with 343 g / h of toluene used in the amount of from the upper part at 80 ° C. From the separator 13 phases as the bottom
    67.6 g / h of water is removed from the layer, and toluene is completely recycled to column 7. The resulting ester is removed in vapor form at 155-1bO through pipe 14, located below the first plate of the column, and high boiling point components in The amount of 12.4 g / h is withdrawn from the capacity of 15 to the receiving 16. The crude ester can be recycled by known methods in successively under-. keyed columns
    From the vapor space below the first tray of the column 7 hourly 520 g of crude ester are removed.
    According to the gas chromatography data, the resulting crude ester has the following composition (in an anhydrous state), May,%:
    Ethylglycol5,2
    Ester 94.0 Unidentified high boiling side components 0.8
    Thus, the productivity of the process is 3.25 kg of ester / kg of catalysing for 1 hour, and the yield of ethyl monoglycolic ester of acetic acid, based on the reacted components, is 97% of the theoretical yield.
    Example 2, 2-ethylhexyl acetate
    The process is conducted as in Example 1 with the difference that 60Q g / h of a mixture of 2-ethylhexanol and acetic acid are subjected to esterification in a molar ratio of 1.2: 1.0 at 1lb-115 ° C, 5
    At a temperature in the cube of the column 7,200 Gj, through the pipeline 14 from the vapor space below the first plate, 518 g of crude ester are taken off hourly. According to the gas chromatographic data 10, the resulting crude ester has the following composition (in a state of absence), May. %: Ethylhexanol 11.5 Ethylhexyl acetate 88.3 t5 Unreacted components 0.2 Thus, the productivity of the process is 3.1.1 kg of ester / kg of catalyst1 h, and the yield of 20 | ethyl hexyl acetate per reacted components is 98% of the theoretical yield, Pm er 3, n-Butyl acetate. The process is carried out analogously to example 25.1 with the difference that the sterication is subjected to 360 g / h of n-butanol mixture
    and acetic acid in molar COOT-:
    1.2: 1, and the process is carried out at 105-110 ° C in the presence of. To 130 g of the ion exchanger of Example 1, at a temperature in the bottom of the column 7 and in the steam and space below the first plate, 297 g / h of the crude ester of the composition, in May,%: 25 n-Butanol 12.8 n-Vutyl acetate 86, eight
    Unidentified.
    components. 0.4 .-. Thus, the productivity of the process is 2.15 kg of ester / kg of catalyst per hour, and the code of n-butyl acetate is 99.4% of the theoretical.
    Example 4, 1-methoxypropyl-2-acetate,. .
    The process is carried out analogously to Example 1 with the difference that 320 g / h of a mixture of 1-methoxy-propanol-2 and acetic acid is subjected to etherification in a molar ratio of 1: 2: 2, and the process is carried out at 88-94 0 in the presence of 100 g ionite prima 1, At a temperature in the cube of the column 7,139 - 146 ° C, 258.7 g / h of the crude ester of the composition, May,% is withdrawn from the vapor space below the first tray,%: Acetic
    acid. 2.4 1-Methoxy-
    : propanol-2 0.8 1-methoxy-propnl-2-acetate86, 7
    Unidentified ComponentsAbout 1
    Thus, the productivity of the process is 1.95 kg of ester / kg of catalyst for 1 hour, and the output of 1-methoxypropyl-2-acetate is 98.7% of the theoretical,
    Editor N. Margolin
    . Compiled by A. Evstigneev-
    Tehred V. Kadar; Proofreader A. Obruchar
    3416/60
    Circulation 3 79 Subscription
    VNIIPI USSR State Committee: for Inventions and Discoveries 113035, Moscow, Zh-35 Ra; usska nab. 4/5
    Production and printing company, Uzhgorod, st. Project, 4
    权利要求:
    Claims (1)
    [1]
    (57) METHOD FOR PRODUCING ETHERS OF ACETIC ACID BY ETHERIFICATION OF Acetic Acid With An Alcohol Selected From The Group n-butanol, 2-ethylhexanol, ethoxyethanol, 1-methoxy-2-propanol, with an excess of alcohol in the presence of a strongly acidic cation exchange resin * general distillation of the resulting reaction mixture, it is noteworthy that, in order to increase the productivity of the process, the latter is conducted in a vertical reactor operating in the flooding mode by means of a discharge bypass valve; th between the reactor and distillation column, followed by distillation of the obtained reaction mixture fed into the top of the rectification column,. with obtaining water as an azeotrope distillate with an azeotropically forming agent — toluene, as a bottoms product — high-boiling by-products, products continuously discharged in the form of liquid, as a side stream, discharged below the first plate — the target product in the form of steam and as an overlying side a shoulder strap removed from the distillation distillation column — a mixture of unreacted starting materials supplied to the esterification stage after replenishing it with fresh acetic acid and alcohol in accordance with the quantity Twomey formed ester.
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    同族专利:
    公开号 | 公开日
    DE3235531A1|1984-03-29|
    ES525866A0|1984-06-01|
    JPS59108740A|1984-06-23|
    DE3360125D1|1985-05-23|
    ES8405357A1|1984-06-01|
    EP0105111A1|1984-04-11|
    DE3235531C2|1992-05-21|
    EP0105111B1|1985-04-17|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE975700C|1962-05-10|Chemische Werke Hüls Aktiengesellschaft Marl |Process for the production of pure carboxylic acid esters|
    NL72344C|1947-11-03|1952-12-15|
    FR1068367A|1951-12-19|1954-06-24|Knapsack Ag|Process for the continuous preparation of esters of aliphatic carboxylic acids|
    FR1575909A|1968-06-12|1969-07-25|
    US4314947A|1978-12-21|1982-02-09|Basf Aktiengesellschaft|Process for completing the esterification of carboxylic acids with alcohols|
    DE3121383C2|1981-05-29|1983-04-14|Chemische Werke Hüls AG, 4370 Marl|Process for the esterification of acetic acid with C 2 to C 5 alcohols|DE3337101A1|1983-10-12|1985-05-02|Chemische Werke Hüls AG, 4370 Marl|METHOD FOR THE ESTERIFICATION OF ACETIC ACID WITH ALCOHOLS WHOSE ACETIC ESTERS ARE HIGHER THAN BOILING THAN ACETIC ACID|
    DE3501761A1|1985-01-21|1986-07-24|Henkel KGaA, 4000 Düsseldorf|METHOD FOR PRE-Esterification OF FREE FATTY ACIDS IN RAW FATS AND / OR OILS|
    GB8518575D0|1985-07-23|1985-08-29|Bp Chem Int Ltd|Esterification process|
    US5618973A|1994-11-10|1997-04-08|Union Carbide Chemicals & Plastics Technology Corporation|Esterification process|
    GB2345911B|1997-10-31|2001-07-18|Celanese Int Corp|Continuous process for the production of carboxylic acid esters of alkylene glycol monoalkyl ethers|
    US6906164B2|2000-12-07|2005-06-14|Eastman Chemical Company|Polyester process using a pipe reactor|
    US7649109B2|2006-12-07|2010-01-19|Eastman Chemical Company|Polyester production system employing recirculation of hot alcohol to esterification zone|
    US7943094B2|2006-12-07|2011-05-17|Grupo Petrotemex, S.A. De C.V.|Polyester production system employing horizontally elongated esterification vessel|
    US7863477B2|2007-03-08|2011-01-04|Eastman Chemical Company|Polyester production system employing hot paste to esterification zone|
    US7892498B2|2007-03-08|2011-02-22|Eastman Chemical Company|Polyester production system employing an unagitated esterification reactor|
    US7829653B2|2007-07-12|2010-11-09|Eastman Chemical Company|Horizontal trayed reactor|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3235531A|DE3235531C2|1982-09-25|1982-09-25|
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