• 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:
    The invention provides a process for epoxidation of an alkene by reaction with a peracid, characterized by supplying an aqueous phase comprising sulphuric acid, hydrogen peroxide and water and an organic phase comprising acetic acid or propionic acid in a chlorinated hydrocarbon solvent to a liquid-liquid extraction device in such manner that these two phases pass in countercurrent through the extraction device; withdrawing from such extraction device an organic solution of peracid and carboxylic acid in the chlorinated hydrocarbon; passing said organic solution and the alkene cocurrently to a reactor; withdrawing from the reactor a product mixture and effecting fractional distillation thereof; withdrawing from such fractional distillation a product phase comprising the oxirane and a recycle phase comprising carboxylic acid in the chlorinated hydrocarbon, and passing such recycle phase from the distillation to the extraction device to form the organic phase therein. The importance of the invention resides in the integration of the epoxidation step with that of the manufacture of the peracid, and in the fact that the carboxylic acid, sulphuric acid and chlorinated hydrocarbon solvent are all recycled.
    公开号:SU867307A3
    申请号:SU762318205
    申请日:1976-02-03
    公开日:1981-09-23
    发明作者:Макдовалд Хилдон Энтони；Фредерик Гринхолг Питер
    申请人:Интерокс Кемикалз Лимитед (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to an improved process for the preparation of alkene oxides, specifically propylene oxide or epichlorohydrin. A known method of producing alkene oxides (propylene oxide, 1,2-epoxypropan-3-ol, etc.), which consists in the interaction of formic acid with hydrogen peroxide in an aqueous medium in the presence of sulfuric acid with a subsequent synthesis of nadmuric acid with dichloromethane and effect on the resulting solution alkene ha The main disadvantage of this method is the complexity of the process, associated with the need to obtain a potentially explosive mixture of formic acid - antitracin on acid - hydrogen peroxide - water, and a three-stage process. The purpose of the invention is to simplify the process of producing propylene oxide and epichlorohydrin. The goal is achieved by the fact that according to the method of producing propylene oxide and epichlorohydrogen {by reacting carboxylic acid; goths with hydrogen peroxide in an aqueous medium in the presence of sulfuric acid using a carboxylic acid extraction with chlorinated hydrocarbon, followed by alkene in the chlorinated hydrocarbon produced by the resulting solution; propionic acid is used as carboxylic acid, propylene dichloride or ethylene dichloride is used as a chlorinated hydrocarbon, and propylene and allyl chloride are used as alkeys and the process is carried out in a countercurrent type extractor. liquid is liquid by reacting 1530 wt.% solution of propyrnic acid in propylene dichloride or ethylene dichloride with an aqueous solution containing 10-35 wt.% hydrogen peroxide 30bO wt.% sulfuric acids, at the molar ratio of propionic acid: hydrogen peroxide, equal to l: (i-2). The use of this invention simplifies the process by eliminating the formation of a potentially explosive mixture of carboxylic acid - iadcarboxylic acid - hydrogen peroxide - water, reducing the number / stage from three to two, and carrying out a continuous process.
    FIG. 1 shows an installation illustrating the proposed method, FIG. 2 - the same, 11-a STS1 for cleaning.
    The installation consists of a three-section extraction column 1 into which an aqueous phase consisting of dilute sulfuric acid, from circulation lines 3 and 4, and hydrogen peroxide from storage 5 for peroxide are fed through peroxide supply line 6 through an opening 2 in the upper part of the central section. The consumption of reagents and circulating streams are presented in table 1. The top of column 1 acts as a reverse acid wash. For this purpose, diluted sulfuric acid from the circulation line 3 is mixed with fresh acid from storage 7 supplied via line 8 and 9, and the inlet 10 in the upper part of the column 1. In the lower part of the central section of the extraction column 1 there is an opening 11 for the organic phase consisting of propylene dichloride propionic acid solution, this phase is fed from the storage for the organic phase 12 via line 13 and the circulation line 1 for the first organic phase. In the lower part of the extraction column 1 there is a distillation section into which circulating propylenedichloride is fed through the second circulation line 15 for the organic phase to the opening 16 in the lower part of the column 11.
    The organic solution of propionic acid in propylene dichloride is removed from column 1 via line 17, this solution is mixed with propylene coming from storage 18 for propylene via line 19, and fed to the reactor 20..
    From the reactor 20, the reaction mixture is transferred via line 21 to distillation unit 22, where all traces of unreacted propylene are removed. Propylene is removed from node 22 via line 23, part of it is output through line 24 to a reset, and part is pumped back through line 25 to line 19.
    Liquid from distillation unit 22 is fed via line 26 to a series of 4 distillation columns. From the first column 27, the heavy fraction is withdrawn via line 28 and fed into the column 29 to purify the solvent. In this column 29, the solvent mixture from line 28 is distilled and: A light fraction is obtained consisting of a solution of propionic acid in propylene dichloride, which is withdrawn from the column; 29 along the line 14, previously called the circulation line for the organic phase. The heavy fraction from the purification column 29 of the solvent is discarded through line 30 as a waste part. All or part of the liquid from the stream in line 28 is directed directly to JB line 14, to the bypass of the purification column 29.
    The light fraction from distillation column 27 is fed to line 31 and the second distillation column 32 is sent to the bottom. A solid fraction from column 32 is fed through line 33 to decanter 34, the aqueous phase is separated, which is sent to waste water 3 The organic part from decanter 34 is fed to the second circulation line 15 for organic matter and back to extrapolation column 1. The light fraction from the second distillation column 32 is fed via line 36 to the third distillation column 37, in this column the light fraction is separated and through the line 38 in brasyvayut the drain. This fraction is mainly acetaldehyde. The heavy fraction from column 37, through line 39, is sent to the final distillation column 40, where it is finally purified and a heavy fraction is obtained, which is withdrawn from the column through line 41 and sent to the effluent, this heavy fraction consists mainly, completely from propionaldehyde. The product from column 40 is sent to propylene oxide storage 42.
    In the extraction column 1, the aqueous phase leaves the bottom part of it via line 43 and part of it is acid discharge. The remainder of line 43 is sent to distillation column 44, in which sulfuric acid is regenerated. In this column 44, the light fraction mainly consists of water, is sent to the effluent through line 45, and the heavy fraction is circulating sulfuric acid, withdrawn from column 44 through line 3 and sent back to the extraction column 1.
    -.
    Tables 1 and 2 show the costs (in kg / h) in various parts of the installation. From these data it can be seen that 70% hydrogen peroxide is used, if 86% hydrogen peroxide is used, the only difference is that the water consumption in the raw material flow in line 5 is reduced by 5 kg / h and a corresponding reduction in water emission occurs. lines 45.
    8.41 0.03 19.33
    1.55
    29.45 15, 73 0, 32
    0.46 1, 74
    0.10 60.21 0.87
    186,73 58,5 €
    23.70
    6.73
    0.09
    0.01
    that
    :Table 2
    0.0005
    0.0004
    0.01
    0.35
    31.21
    0.06 0.0006
    0,0003
    0.02
    The installation, where it is obtained from epichlorohydrin from allyl chloride, is shown in FIG. 2, the difference from the plant for producing propylene oxide is generally in the purification steps. So from FIG. 2, it can be seen that the organic solution of supropropionic acid in line 1 is mixed with allyl chloride supplied from the storage for it via line 3, and fed to reactor 4.
    From the reactor 4, the reaction mixture is fed via line 5 to distillation column b, where the light fraction is separated, consisting of allyl chloride, propylene dichloride and water. The light fraction is fed via line 7 to the second distillation column 8, where the allyl chloride is separated as a light fraction and sent along line 9. Part of the allyl chloride in line 9 goes out of emission through line 10, and part of it is sent back through line 11 to the line 3
    The heavy fraction from the second column 8 is withdrawn via line 9 to decanter 12, where the aqueous phase is separated, which is sent to the effluent through line 13. The organic phase from decanter 12 is withdrawn through line 14 and distributed between the second circulation line for
    Sulfuric acid
    Water
    Hydrogen peroxide
    Propionic sour
    Propylene dichloride
    Allyl chloride
    N-propanoic acid
    Sulfuric acid
    Water
    Hydrogen peroxide
    organics 15, leading to the bottom of the extraction column 16, and line 17, leading to the mixing deviceCTJBO.
    The heavy fraction from the first column 6 is fed through line 18 to the distillation column 19. The light fraction from column 19 is the product that is sent to storage 20, and the heavy fraction is sent to line 22 via line 21. In the column 22 tons; The 1 fraction from column 19 (mainly propioic acid) is distilled to give a light fraction, free from heavy impurities. The heavy fraction from column 22 is sent to the effluent via line 23.
    The light fraction from the column 22 is selected through line 24 to a mixing device 25g where it is mixed with a solution from line 17 and sent to line 26, previously called an organic circulation line.
    The remainder of FIG. 2 is basically described in FIG. 1, for a more complete understanding of the operation of the installation, Tables 3 and 4 are shown, in which the flow rates (kg / h) are shown in different parts of the installation of FIG. 2, at those points where they differ from the installation in Figure 1.
    T a b l and c a 3
    29.45
    15.73
    0.52
    0.46

    0, 10 61.80 167, 6 72.7
    36.73
    43.67
    0.01
    .Table 4
    0.04
    1.55 1.39
    15,73 0, 02 Propionic Acid Propylene Dichloride Allyl Chloride Other
    Supropionic acid
    权利要求:
    Claims (1)
    [1]
    Glycol Epichlorohydrin Formulation and here and in order to simplify the process, propionic acid is used as carboxylic acid, as chlorinated coal Hydrogen - Propylene Dichloride or
    Continuation of table 4
    0.01
    0.01
    0.02 0.001
    0.01 0.95 49, 27 ethylene dichloride, and t; as an alkene, propylene or allyl chloride, and the process is carried out in a liquid-liquid type rotary co-collector by reacting 15-30 wt.% propionic acid solution in propylene dichloride or ethylene dichloride with a water solution containing 10-35 wt.% hydrogen peroxide and 30-60 wt. % sulfuric acid, at a molar ratio of propionic acid i, hydrogen peroxide equal to 1: (1-2). (.. .. Sources of information / taken into account during the examination 1. UK patent No. 1188791, cl. С 2 С, 1970 (prototype).
    类似技术:
    公开号 | 公开日 | 专利标题
    SU867307A3|1981-09-23|Method of preparing propylene oxide or epichlorohydrin
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    GB1390090A|1975-04-09|Recovering anhydrous acrylic acid
    US4294776A|1981-10-13|Process for the purification of organic solutions of percarboxylic acids
    JPH066583B2|1994-01-26|Epoxidation method for olefinic unsaturated hydrocarbon compounds
    US3992417A|1976-11-16|Process for manufacture of gamma butyrolactones
    KR900017987A|1990-12-20|Method for producing acrylic ester
    JP4677066B2|2011-04-27|Post-treatment of liquid crude vinyl acetate
    US4424391A|1984-01-03|Process for the manufacture of olefine oxides
    Sonoda et al.1965|Hydroxylation of Olefins with Hydrogen Peroxide in the Presence of Selenium Dioxide Catalyst
    JPH11292802A|1999-10-26|Improved co-production of propylene oxide and styrene monomer
    US4218400A|1980-08-19|Process for the production of fluorenone by catalytic oxidation of fluorene
    KR0150442B1|1998-10-15|A continuous process for the production of dichlorohydrin
    US4177196A|1979-12-04|Epoxidation
    US3821286A|1974-06-28|Process for the production of methyl methacrylate
    US4172840A|1979-10-30|Epoxidation
    GB1082572A|1967-09-06|Production of carboxylic acids
    US3350420A|1967-10-31|Production and recovery of oxygenated hydrocarbons by plural distillation
    GB1577019A|1980-10-15|Process for producing high quality terephthalic acid
    JPH05186391A|1993-07-27|Method for purifying ethyl acetate
    US4344897A|1982-08-17|Process for the preparation of percarboxylic acid solutions
    US4562274A|1985-12-31|Process for the preparation and isolation of polyglycidyl compounds
    GB1424747A|1976-02-11|Method and apparatus for the continuous dehydration of maleic acid
    EP0074009B1|1986-10-01|Process for the preparation of tetramethyl oxirane
    US3337618A|1967-08-22|Preparation and recovery of acetic acid
    同族专利:
    公开号 | 公开日
    NO148672B|1983-08-15|
    ES444910A1|1977-04-16|
    IN141031B|1977-01-15|
    BE838068A|1976-07-30|
    FR2379520A1|1978-09-01|
    NL7601048A|1976-08-06|
    CS227653B2|1984-05-14|
    AU506647B2|1980-01-17|
    SE424726B|1982-08-09|
    BR7600626A|1976-08-31|
    JPS51101906A|1976-09-08|
    AU1033176A|1977-07-21|
    FR2379520B1|1981-06-26|
    FR2300085B1|1980-10-03|
    GB1535313A|1978-12-13|
    NO760310L|1976-08-05|
    ZA76244B|1977-01-26|
    LU74299A1|1976-06-18|
    DK38776A|1976-08-05|
    US4071541A|1978-01-31|
    SE7601146L|1976-08-05|
    IE42394L|1976-08-04|
    DE2602776A1|1976-08-05|
    RO69626A|1981-11-24|
    CA1070703A|1980-01-29|
    JPS6025432B2|1985-06-18|
    AT356124B|1980-04-10|
    NO148672C|1983-11-23|
    NL181579C|1987-09-16|
    PL109648B1|1980-06-30|
    IE42394B1|1980-07-30|
    DE2602776C2|1984-05-17|
    FI760167A|1976-08-05|
    PT64713A|1976-02-01|
    ATA60976A|1979-09-15|
    NL181579B|1987-04-16|
    FR2379519B1|1980-10-31|
    DD122970A5|1976-11-12|
    AR208107A1|1976-11-30|
    PT64713B|1977-08-11|
    FR2300085A1|1976-09-03|
    FR2379519A1|1978-09-01|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3141896A|1964-07-21|Process for the percarboxylic acid epqxr |
    US3065246A|1962-11-20|Continuous epoxidation method |
    US2977374A|1961-03-28|Process for preparing oxirane |
    DE1240515B|1964-10-22|1967-05-18|Knapsack Ag|Process for the continuous production of epoxy compounds|
    GB1188791A|1966-04-14|1970-04-22|Laporte Chemical|Olefin Oxides|
    BE755100A|1969-08-21|1971-02-01|Degussa|PROCESS FOR THE EPOXIDATION OF UNSATURATED COMPOUNDS|
    DE2060190C3|1970-12-08|1983-12-08|Degussa Ag, 6000 Frankfurt|Process for separating propionic acid or butyric acid from a mixture of epichlorohydrin, allyl chloride and one of the aforementioned carboxylic acids|
    DE2141156C3|1971-08-17|1981-01-22|Degussa Ag, 6000 Frankfurt|Process for obtaining anhydrous organic percarboxylic acid solutions|JPS53105410A|1976-03-02|1978-09-13|Propylox Sa|Process for preparing peracid|
    GB1584355A|1976-10-26|1981-02-11|Propylox Sa|Epoxidation|
    GB1589066A|1977-02-26|1981-05-07|Propylox Sa|Process for the production of peroxycarboxylic acids|
    US4172086A|1977-03-28|1979-10-23|Fmc Corporation|Process for the manufacture of peroxycarboxylic acids|
    DE2718602A1|1977-04-22|1978-10-26|Kraftwerk Union Ag|DEVICE FOR TENSIONING SEVERAL SCREW BOLTS|
    DE2734085A1|1977-07-28|1979-02-22|Bayer Ag|PROCESS FOR THE PREPARATION OF HALOGENALKYL SUBSTITUTED OXIRANS|
    DE2734086A1|1977-07-28|1979-02-22|Bayer Ag|PROCESS FOR THE PREPARATION OF HALOGENALKYL SUBSTITUTED OXIRANS|
    DE2734243A1|1977-07-29|1979-02-08|Bayer Ag|PROCESS FOR THE PREPARATION OF HALOGEN SUBSTITUTED VINYLOXIRANS|
    DE2734242A1|1977-07-29|1979-02-08|Bayer Ag|PROCESS FOR THE MANUFACTURING OF VINYLOXIRAN|
    DE2734240A1|1977-07-29|1979-02-08|Bayer Ag|PROCESS FOR THE MANUFACTURING OF VINYLOXIRAN|
    US4325888A|1978-01-13|1982-04-20|Propylox|Preparation of peracid by liquid-liquid extraction|
    FR2421168B1|1978-03-28|1980-09-19|Propylox Sa|
    DE2835883A1|1978-08-16|1980-02-28|Bayer Ag|METHOD FOR PRODUCING MALEIC ACID GLYCIDYLESTERS|
    DE2835884A1|1978-08-16|1980-02-28|Bayer Ag|METHOD FOR PRODUCING 7-OXABICYCLOHEPTAN-3,4-DICARBONIC ACID DIGLYCIDYLESTER|
    DE2835881A1|1978-08-16|1980-02-28|Bayer Ag|METHOD FOR PRODUCING GLYCIDYL ESTERS OF CYCLOALIPHATIC POLYCARBONIC ACIDS|
    DE2835885A1|1978-08-16|1980-02-28|Bayer Ag|METHOD FOR PRODUCING 7-OXABICYCLOHEPTAN-3,4-DICARBONIC ACID DIGLYCIDYLESTER|
    DE2835882A1|1978-08-16|1980-02-28|Bayer Ag|METHOD FOR PRODUCING FUMAR ACID GLYCIDYL ESTERS|
    DE2835886A1|1978-08-16|1980-02-28|Bayer Ag|METHOD FOR PRODUCING GLYCIDYL ESTERS OF AROMATIC POLYCARBONIC ACIDS|
    DE2856665A1|1978-12-29|1980-07-17|Bayer Ag|METHOD FOR PRODUCING PERCARBONIC ACID SOLUTIONS|
    FR2455580B1|1979-05-04|1981-12-24|Propylox Sa|
    US4370251A|1980-07-25|1983-01-25|Fmc Corporation|Continuous process for the production of peroxycarboxylic acid compositions|
    DE3049434A1|1980-12-30|1982-07-29|Peroxid-Chemie GmbH, 8023 Höllriegelskreuth|METHOD FOR PRODUCING EPOXIES|
    DE3260740D1|1981-01-15|1984-10-25|Bayer Ag|Process for the preparation and isolation of n-alkyl oxiranes|
    FR2502620B1|1981-03-24|1983-11-10|Ugine Kuhlmann|
    JPS6357952U|1986-10-01|1988-04-18|
    US7012154B2|2004-07-28|2006-03-14|Peragen Systems, Llc|Continuous process for on-site and on-demand production of aqueous peracteic acid|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    GB4692/75A|GB1535313A|1975-02-04|1975-02-04|Production of peracids and of epoxides|
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