• 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:
    <P> Process providing an optimum conversion of the starting bisimide to the corresponding acid or anhydride It consists in heating in a container 15 a mixture of a bis (phthalimide ether), water, phthalic anhydride or phthalic acid for produce a two-phase reaction mixture, the liquid phase containing a bis (phthalic acid ether) and phthalic acid and the vapor phase containing an N-organo phthalimide, to be purged by means of the valve 20 the vapor phase of the reaction medium and to recover the bis (phthalic acid ether). </ P> <P> Application to the manufacture of dianhydride of bisØ (dicarboxy-3 ', 4'-phenoxy) -4-phenyl-2,2-propane acid. </ P>
    公开号:SU904517A3
    申请号:SU772527551
    申请日:1977-10-04
    公开日:1982-02-07
    发明作者:Линн Вебб Джимми
    申请人:Дженерал Электрик Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to organic chemistry, in particular, to an improved method for producing 2,2-bis / 4- (3,4-dicarboxyphenoxy) phenyl / propane dianhydride, an important organic product.
    The closest in technical essence and the achieved results to the proposed is a method for producing 2,2-bis- / 4- (3,4, -dicarboxyphenoxy) -phenyl / propane dianhydride by hydrolysis of 2,2-bis- / 4- (N-phenylphthalimide -4-hydroxy) phenyl / propane in the medium of 50% NaOH solution at 160 - 175 e C under 11 atm, followed by treating the resulting salt with hydrochloric acid, and then formed as a result of 2,2-bis / 4- (3, 4-dicarboxyphenoxy) phenyl / propane is subjected to dehydration with acetic anhydride in acetic acid medium at boiling [1].
    A disadvantage of the known method is the multi-stage process, since it initially includes a hydrolysis step, after which the salt formed is converted to tetra-. acid, which must be further dehydrated in the case of anhydride.
    2
    The purpose of the invention is the simplification of the process. This goal is achieved by the fact that according to the method for producing 2,2-bis - / 4- (3,4-dacarboxyphenoxy) phenyl / propane dianhydride 5 by heating, they are subjected to treatment
    2,2-bis- / 4- (3,4-dicarboxyphenoxy) fenpp / propane-bis-N-methylimide with phthalic anhydrides at a weight ratio of 0.5: 0.2 in a closed system at 100-300 ° C at in the presence of water at a ratio of water: imide of 7.5-12 :) usually in the presence of a catalyst, N-amnobutyl is used, followed by separation of the side-forming N-phthalimide as a vapor phase. 15 Advantageously, after separation of the side-forming N-phthalimide, water and phthalic anhydride are additionally added to the reaction mass.
    As a result of the proposed process, an exchange occurs between bisimide and phthalic anhydride to obtain, as a result, the corresponding tetra-acid or its anhydride according to the equation
    A + B 5 = * d '+ B, where A, bismide;
    904
    A r - organoftalimid;
    B - phthalic anhydride;
    B - bisanhydride or tetraacid.
    The optimal conversion of bisimide to tetraacid can be achieved as a result of an exchange reaction if the imide formed in the process is selectively removed. It was found that the removal of imide can be carried out by blowing part of the vapor phase of the reaction mixture, consisting of liquid and vapor phases. It turned out that the vapor phase consists practically of water and M-organophthalimide and contains only a small part of phthalic acid. Thus, by conducting continuous blowing, the reaction is shifted to the right, which allows the conversion of the starting bisimide to the corresponding acid or bisanhydride without shutting down the reactor or recycling excess phthalic acid.
    In FIG. 1 shows a diagram of an implementation of the proposed method using a batch process, an autoclave is used as a reactor; in FIG. 2 - the same, using a continuous process, a distillation column is used as a reactor.
    The reservoir 1 (Fig. 1) is intended for snoring water or an aqueous catapitizer solution. An aqueous solution of organic carboxylic acid used in the implementation of the proposed method, and has a concentration of the order of from 0.01 to 80 wt.% - acid in relation to the weight of water. The tank 1 is equipped with a valve 2. In FIG. 1 also shows a metering pump that is capable of supplying the catalyst mixture in the required amount to a reactor 3 that can operate at a pressure higher than atmospheric, i.e. about 15 atm or less, about 70.3 atm. Pressure gauge 4 and valve 5 for. water flow sampling is also shown in FIG. 1. The reactor 3, designed for pro. the process at high pressure, is an autoclave or a thick-walled 1 cylinder (Parr bomb), equipped with a valve 6 on the pipeline for entering the fluid flow, as well as a mixing device 7, an immersion tube 8 and a jacket for heating 9. The mixture is loaded into the reactor consisting of bisimide and phthalic anhydride or phthalic acid. The drain valve 10 is designed to control the passage of vaporous materials leaving the reactor, and the refrigerator 11 is designed to cool the vaporous reaction products, such as water and N-organophthalimide.
    In FIG. 2 shows a distillation column. This distillation column is divided into three sections: section A, section B and section C.
    A 517 jacket (not shown) is used to maintain the temperature in the column in the range of 100 to 300 ° C during the reaction. In addition, a container 5 13, which is a source of heated bisimide, i.e. maintained at a temperature at which it is in the molten state, a pump designed to supply molten bisimide from the tank 13 0 to the distillation column (to point E]), a tank 19 for storing phthalic anhydride, which can be fed in the molten state to the column pump distillation to point E 2 . Water from tank 15 is pumped to the Distillation column (Point E > ).
    'The reaction between bisimide and phthalic anhydride proceeds in section B of the distillation column as a result of contact between the molten bisimide as it flows down the column for 20 and phthalic anhydride as it rises up the distillation column. At the same time, water or an aqueous catalyst mixture is continuously pumped into the zone in which a mixture of components is formed, i.e. to point E3. The reaction product is tetra-acid or its bisangide. the read is formed continuously in the form of a melt in section C. Valve V 2 (Fig. 2) is designed so that the bisanhydride can be at least 30 intermediate, introduced in the required amount.
    At the top of the distillation column, in section A, N-organophthalimide and water, along with other volatile components, are discharged from the distillation column using a variable speed valve 35 Vi. The discharged reaction product is then transferred to the refrigerator 11, and the mixture consisting of N-organophthalimide and water is recovered in receiver A (FIG. 2).
    40 Example 1. 20 parts of 2,2-bis / 4- (3,4-dicarboxyphenoxy) phenyl / propane bps-M-methylimide, 22.75 parts of phthalic anhydride and 250 parts of water are charged into an autoclave reactor. Next, the autoclave reactor is tightly closed and 45 are heated with stirring at a pressure of about 14.06 kg / cm 2 . After heating the reaction mixture thus obtained for one hour, the purge valve is opened and the steam mixture is piped into the refrigerator at a rate of about 2-8 parts by weight. per minute. The solid residue recovered from the aqueous distillate is then recovered by filtration. Solid residue before is N-methyl phthalimide. The aqueous condensate 55 is recycled to the reaction mixture using a high pressure pump. After heating for 14.2 g, the resulting mixture was cooled to room temperature. Next, in addition to the autoclave, 20 weight parts phthalic anhydride. After this operation, after another 16.5 hours, an additional 10 parts by weight are introduced into the autoclave. phthalic anhydride. After another 2.5 hours of additional heating, the total amount of N-methylphthalimide equal to 8.6 hours is recovered. The mixture thus obtained is cooled to room temperature. The contents of the autoclave are further distilled at 250 ° C. and a pressure of 60 mmHg. The result is 2,2-bcc / 4- (3,4-dicarboxyphenoxy) phenyl / propane dianhydride in an amount of 99% of the theoretical yield.
    G
    PRI me R 2. In example 1, download into the autoclave reactor for 27 hours
    2,2-bis14- (3,4-dicarboxyphenoxy) phenyl / propane 'bis-N-methylimide, 29 hours phthalic anhydride, 200 parts of water and 200 parts of propionic acid. Then the autoclave reactor is tightly closed and its contents are heated to 200 ° C with stirring. After heating the reaction mixture for one hour, the purge valve is opened. The vapor mixture is removed from the autoclave reactor at a speed of 10-15 parts by weight. per minute (by condensate) and sent to the refrigerator, as a result, the formation of condensate, consisting of water, propionic acid and N-methylphthalimide and phthalic acid in a molar ratio of 20: 1. The solids were separated and the filtrate was returned to a container, from where it was using noxy) phenyl / propane bis-N-methylimide, 17 parts phthalic anhydride, 300 parts water and 56 parts tri-M-butylamine. Removal of N-methylphthalimide is carried out using a bleed valve 5 (Fig. 1). A mixture consisting of water: and tributylamine, containing traces of phthalic acid, is returned to the autoclave with a feed rate practically equivalent to the blow-off speed. A quantitative yield10 of 2,2-bms- / 4- (3,4-dicarboxy-phenoxy) -phenyl / / propane was achieved after a heating time of 10-20 h.
    PRI me R 4. Cap distillation column. (Fig. 2) is heated in section C to a temperature sufficient to maintain a temperature above 200 ° C through section B. The molten 2,2-bis / 4- (3,4-dicarboxyphenoxy) phenyl / propane bis-N- methyl mid is pumped to the distillation column at point E1. At the same time, molten phta 'left anhydride is pumped to the distillation column at point E 2 . Additionally, steam is supplied to point E 3 of the distillation column. The vapor mixture is discharged through valve 25 (V t ), passes through the refrigerator and, as a result, a mixture is formed consisting of N-methylphthalimide, phthalic acid and water. The molten 2,2-bms / 4 - (3,4-dicarboxyphenoxy) phenyl / pronan-bcc-anhydride is periodically collected in a collection (Lig. 2).
    权利要求:
    Claims (3)
    [1]
    A - organophthalimide; B - phthalic anhydride; B - bisanhydride or tetraacid. An optimal conversion of the bimimide to the tetraacid can be achieved as a result of the exchange reaction if the imide formed during the process is selectively removed. It was found that the imide can be removed by stripping part of the vapor phase of the reactive mixture consisting of the liquid and vapor phases. It turned out that the vapor phase consists practically of water and N-organophthalimide and soderhot only a small part of phthalic acid. Thus, the wire is continuously blown off, and the reaction is shifted to the right, which allows the initial bimimide to be converted to the corresponding acid or bis anhydride without turning off the reactor or recycling the excess phthalic acid. FIG. Figure 1 shows the scheme for implementing the proposed method using a batch process; an autoclave is used as the reactor; pas figs. 2 - the same, with the aid of a continuous process, a disgillation column is used as a reactor. Tank 1 (Fig. 1) is intended for storing water or an aqueous catalyst solution. The aqueous solution of the organic carboxylic acid used in the implementation of the proposed method, the concentration of the order of from 0.01 to 80 wt.% - acid relative to the weight of water. The container 1 is equipped with a valve 2. FIG. Also shown is a dosing pump, which is capable of feeding the catalyst mixture, in the required amount to the reactor 3, which can operate under a pressure greater than atmospheric, i.e. about 15 atm or less, about 70.3 atm. A pressure gauge 4 and a valve 5 for sampling the water flow are also shown in FIG. 1. The reactor 3, designed to carry out the process at high pressure, is an autoclave or a thick-walled cylinder (Parr bomb), is equipped with a valve 6 on the pipeline at the day of the liquid flow entry. OTHERS, as well as an interchangeable device 7, a dip tube 8 and a jacket for heating 9. A mixture consisting of bisimide and phthalic anhydride or phthalic acid is loaded into the reactor. The drain valve 10 is designed to regulate the passage of vaporous materials leaving the reactor, and the cooler 11 is designed to cool the vaporous reaction products such as water and N-organophthalimide. FIG. 2 shows a distillation column. This distillation column is divided into three sections: section A, section B, and section C. Heater A jacket (not shown) is used to maintain a temperature in the column in the range from 100 to during the reaction. In addition, the capacity 13, which is the source of the heated bimimide, i.e. maintained at the temperature at which it is in the molten state, a pump designed to supply molten bismimide from tank 13 to the distillation column (point EI), tank 19 for storing phthalic anhydride, which can be fed in the molten state to the column distillation using a pump to a point EZ. Water from the tank 15 is pumped into the Distillation column (point E.,). The reaction between the bismimide and phthalic anhydride protrudes in section B of the distillation column as a result of contact between the molten bisimide as it passes down the column and phthalic anhydride as it rises up the distillation column. At the same time, the water or the water catagasate mixture is continuously supplied by the pump to the zone in which the mixture of components is formed, i.e. to point bj. The reaction product, tetraacid or its bisanhydride, is formed continuously, as a melt in section C. Valve Vj. (Lig. 2) is designed so that the bisanhydride can be at least intermediate, introduced in the required amount. At the top of the distillation column, in Section A, N-organophthalimide and water, along with other volatile components, are discharged from the distillation column using a variable speed Vi valve. The discharged reaction product then goes to the cooler 11, and the mixture consisting of N-organophthalimide and water is recovered in receiver A (Fig. 2). Example 1. In an autoclave reactor load 20 hours of 2.2-byc / 4- (3,4-dicarboxyphenoxy) phenyl / propane 0-c-N-methylimide, 22.75 parts of phthalic anhydride and 250 hours of water. The autoclave reactor is then tightly closed and heated with stirring at a pressure in the order of 14.06 kg / cm. After the load, the reaction mixture obtained in this way for one hour, the blow-off valve is opened, and the steam mixture flows through the pipeline to the refrigerator at a speed of 2-8 parts by weight. per minute. The solid residue, separated from the aqueous distillate, is further removed by filtration. The solid effluent is N-methylphthalimide. The water condensate is recycled to the reaction mixture via a high pressure pump. After heating for 14.2 g., The resulting mixture is cooled to room temperature of perragura. Next, 20 parts by weight are additionally added to the autoclave. phthalic anhydride. After this operation, after 16.5 hours, an additional 10 parts by weight are introduced into the autoclave. phthalic anhydride. After another 2.5 hours of additional heating, the total amount of N-methylphthalimide is recovered, equal to 8.6 hours. The mixture thus obtained is cooled to room temperature. The contents of the autoclave are further distilled at 250 ° C and a pressure of 60 mm Hg. As a result, 2,2-bis / 4- (3,4-dicarboxyphenoxy) -phenyl / propane dianhydride was obtained in an amount of 99% of the theoretical yield. EXAMPLE 2 In Example 1, a 27 hour 2.2-bis / 4- (3,4-dicarboxyphenoxy) fe1shl / propane bis-M-methylimide was charged to the autoclave reactor 27 hours. phthalic anhydride 200 parts of water and 200 parts of propionic acid. Then the autoclave reactor tightly closed and its contents are heated to 200 ° C with stirring. After heating the reaction mixture for one hour, the blow valve is opened. The steam mixture is removed from the autoclave reactor at a rate of 10-15 parts by weight. per minute (by condensation) and sent to the refrigerator, as a result, condensation is formed, consisting of water, propionic acid and N-methylphthalimide and phthalic acid in a molar ratio of 20: 1. The solid products are separated and the filtrate is returned to the tank, from where it is pumped back into the autoclave reactor with a pump at a speed approximately equivalent to the speed of stripping volatile components from the reaction mixture. This process is continued for 12 hours, after which the autoclave is allowed to reach room temperature. 175 parts by weight are contained in the cooled autoclave reactor. liquids, of which 99% (from theoretical yield) is 2.2-5MC / 4- (3.4- iHKap6oKCHphenoxy) phenyl / propane. Their identity is confirmed by both the acquisition method and their infrared spectrum. The use of propionic acid as an acid catalyst in an exchange reaction significantly increases the rate of this reaction. For a reaction that provides a 99% yield (theoretical), 50 hours are required, but only 12 hours are needed to obtain an equivalent amount of tetraacid ripH using propionic acid as a catalyst when using BaifflH of the same product recovery procedure. EXAMPLE 3 The process of Example 2 is repeated with the exception that it uses 32 hours. 2.2- &amp; ms / 4- (3,4-dacarboxy-noxy) -phenyl / propane bns-L- methylimide, 17 parts of phthalic anhydride, 300 parts of water and 56 parts of tri-M-6-utilamine. Removal of 1M-methylft; p1 No. yes is carried out using a blower} valve (Fig. 1). A mixture consisting of water of 3-5 lamine containing cjiejbi phthalic acid returns to the anclave with an input rate almost equal to 1 hA of the blow rate. A quantitative yield of 2,2-bis-14- (3,4-dicarboxisenoxy) fesch / / propane was achieved after a heating time of 10-20 ha per ha. EXAMPLE 4 KolPachkova distillation column. (Fig. 2) 1 is heated in sec. 1 C to a temperature sufficient to maintain temperatures above 200 ° C through section B. The molten 2,2-bis / 4- (3,4-dicarboxxy-phenoxy) -phenyl / propane bis-N- methylimide is pumped to the distillation column at point E ,. Simultaneously, the molten phthalic anhydride is pumped into the distillation column at point EJ. Additionally, steam is supplied to the point EZ of the distillation column. The vapor mixture is discharged through a valve (Vi), passes through a cooler and, as a result, a mixture is formed consisting of N-methylphthalimide, phthalic acid and water. Molten 2,2-6wc / 4 - (3,4-dicarboxyphenoxy) -phenyl / propane-bg with anhydride; period; assembled in the assembly (Lig. 2). Claim 1. Method for preparing 2 2-by-4- (3,4; dicarboxy-phenoxy) -phenyl-Zyropane dianhydride by treating with water corresponding to heating, characterized in that, in order to simplify the process, the treatment is subjected to 2,2-bis1-4- (3,4-dicarboxyphenoxy) fennl / propan-bms-N-methylimide prn weight ratio water: imide 7.5-12: 1 in the presence of phthalic anhydride at a weight ratio imidgangidrnd 0.5-2.0 in a closed system at 100- 300 ° C, followed by separation of the side-forming N-phthalim by the vapor phase.
    [2]
    2. The method according to claim 1, wherein the process is carried out in the presence of a catalyst, N-aminobutyl or propionic acid.
    [3]
    3. Method according to paragraphs. 1 and 2, that is, with the fact that after separating N-phthalimide, water and phthalic anhydride are introduced into the reaction mass. Sources of information accepted in the United States of America during expert 1. US Patent No. 3957862, cl. 260-520, pub. 1.976 (npoTOTim).
    If
    f (/ & /
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    引用文献:
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    US3879428A|1973-03-30|1975-04-22|Gen Electric|Method for making aromatic biss|
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    US4329291A|1981-04-03|1982-05-11|General Electric Company|Method for making aromatic biss|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US05/729,127|US4116980A|1976-10-04|1976-10-04|Method for making aromatic bisor aromatic bis s|
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