• 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:
    Highly pure terephthalic acid is prepared from di-potassium terephthalate. The terephthalic acid so produced aids in the direct production of high quality polyester fiber.
    公开号:SU710514A3
    申请号:SU772480075
    申请日:1977-05-11
    公开日:1980-01-15
    发明作者:Шуле Жан-Клод；Лэли Андре
    申请人:Рон--Пуленк Эндюстри (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the field of organic synthesis, in particular, to an improved method for the production of tereftpsic acid, an important cunemer for the production of polyester fiber. Izvesti is a method of producing terephtheic acid from two-potassium terephthalate, which is obtained in turn by dismutation of potassium benzoate 111. Usually, the conversion of two-stage terephthalate to terephthalic acid is carried out in two stages. At the first stage, the reaction of two-potassium terephthalate is carried out with benzoic acid. In the SECOND stage, the acid terephthalate formed is converted with additional benzoic acid into terephthalic acid. The closest to the invention of the rib technical essence and the achieved results is a method for producing terephthalic acid by reacting a dilute aqueous solution of di-potassium terephthalate, containing 1-15% or 0.04-0.6 mol% per kg of water, with benzoic acid at a healthy ratio of digester tereft - .. lat and acid 1-2.5, at 100-140 ° C, followed by separation at a temperature not higher than 60 ° C formed solid terephthalic acid mixed with benzoic acid, and chicken: 1M potassium tereftapate, which is then subjected myoghratnaya re crystallization from water 2. The content of benzoic acid in terephthalic acid is not less than 100. Acid number 668. A disadvantage of the known method is the need to perform multiple recrystallization of the target product. Even without this, terephthalic acid is not directly suitable for the manufacture of high quality polyester fibers. The purpose of the invention is to simplify the process and improve the quality of the target product. This goal is achieved using a method of producing terephthalic acid by reacting a dilute aqueous solution of di-potassium terephthalate containing 0.1-0.4 mol of salt per 1 kg of sweat,
    with benzoic acid at a molar ratio of acid and dipotassium terephthalate 4-12, in the presence of potassium benzoate in an amount of 0.2-0.8 mol per 1 kg of water, the process is carried out at 90-250 ° C, followed by separation of the resulting solid terephthalic acid at eS -ieo C and a single recrystallization from water.
    Distinctive features of the process are carrying out the interaction in a dilute aqueous solution containing 0.1-0.4 mol, dipotassium tetrate per 1 kg of water and carrying out the process with a molar ratio of benzoic acid and dipotassium terephthalate 4-12 in the presence of potassium lenzoate in the amount of 0.2 -0.8 mol per 1 kg of water, at 90-250 ° C, followed by separation of the formed acid at 85-16 ° C and single recrystallization, which simplifies the process and improves the quality of the target product,.
    The proposed method relates, in particular, to the use of dichloride J p terephthalate obtained by the Hevkep process as a result of dismutation of potassium benzoate. However, it is possible to use two-potassium terephthalate, obtained by another way.
    Components can be entered into the reaction zone in any way. The download may, for example, be carried out in three streams. The first stream is an aqueous solution of two-potassium terephthalate obtained as a result of dismutation of potassium benzoate, the second stream is benzoic acid and the third water containing the required amount of potassium benzoate.
    If the reaction zone consists of several zones (a series of reactors or a reactor with several compartments), then the flow of individual streams can be fractionated. In all cases, however, the required amount of potassium benzoate must be introduced into the first reaction zone.
    At the exit of the reaction zone, the terephthalic acid is separated by any known method, for example, filtration or centrifugation. The separation is carried out at temperatures above 80 ° C, preferably at 85-160 ° C. Next, terephthalic acid is purified by any known method. Purification can, for example, be carried out with organic solvents, such as alcohol, ketone, an aromatic hydrocarbon, but it is preferable to use an aqueous treatment. Terephthalic acid crystals can, for example, be heated with hot water (the temperature usually is 80-250 ° C, preferably 90-150 ° C. Terephthalic acid crystals can be suspended in hot water, and this operation is carried out in several stages : You can dissolve the crystals in 5 hot water, followed by cooling the solution. In all cases of use for water treatment the water can be recycled to the reaction zone. At the same time, potassium benzoate is returned.
    The method can be carried out continuously or intermittently.
    Example 1 Into a stirred reactor, the temperature of which is maintained at 160 ° C, is continuously fed in 1 hour;
    1.67 kg of two-exalted terephthalate (6.872 mol)
    5.49 kg of benzoic acid (45 mol) 01, 00 Kg of benzoate
    potassium (6.25 mol)
    22.4 kg of water.
    Thus, 0.307 ml of dipotassium tereft and 0.279 mol 5 of potassium benzoate per kg of water are introduced; the molar ratio of benzoic acid and dipotassium. TereLtalata is equal to 6.548,
    After the reaction, the mixture is sent to a dryer that operates in an isothermal mode at, 1.18 kg of terephthalic acid containing 20% water is recovered. The terephthalic acid crystals are washed, c. the dryer is hot water at the rate of 5–2 kg / h.
    These flush waters are recycled. As a result, after drying, 0.98 kg / h of pure terephthalic acid is obtained. (The acid number is 675; the content of benzoic acid is 100 million; the content of other benzenecarboxylic acids, potassium and slags is lower than 10 million.
    Example 2. In a stirred reactor, the temperature in which is maintained is continuously fed at 1 hour:
    1.62 kg of terephthalate dipotassium (6.666 mol)
    8.34 kg benzoic
    -acids (68.32 mol)
    0.74 kg benzoate
    potassium (4.625 mol)
    21.45 kg of water
    0.311 moles of two-potassium terephthalate and 0.216 mol of 5 potassium benzoate per 1 kg of water are introduced; the molar ratio of benzoic acid and dipotassium terephthalate is 10.254.
    Potassium terephthalate comes from the dismutation stage. Wash water from the purification stage is used, as well as 3% stock solution obtained after separation of the crystals of terephthalic acid.
    After the reaction, the mixture is directed to a 5 to 5 dryer operating in an isothermal mode at 150 ° C. The mother liquor and 1055 g / h of tereft of the left acid, containing 18.5% of water, are separated. Then, terephthalic acid crystals are suspended in 2000 g of hot water (1050 g / wet terephthalic acid is recovered. After drying, 0.87 kg / h of terephthalic acid is obtained with the following characteristics: Acid number Benzoic acid content, mp Content of other benol carboxylic acids, ppm Potassium content, Average granulometric composition, (99% of the mass has a granulometric composition above 25 µm. Example 3. The reaction is carried out in three reactors with agitators, the temperature of which is maintained at 220, 180 and 150 ° C, respectively. In the first p the actor serves an aqueous solution of potassium terephthalate obtained at the dismutation stage, water after purification of terephthalic acid crystals and 37 wt% of the mother liquor obtained after separation of terephthalic acid.Benzoic acid is fed into each reactor at the rate of 4.67 kg / h the first reactor and 1.98 kg / h to the remaining reactors. The feed at the level of the first reactor is as follows: Two-potassium tere2, 17 kg / h phthalate (8.930 mol 4.67 kg / h Benzoic acid (38.279 mo 2.54 kg / potassium benzoate (15.875 mo of water; 69.5 kg / h. Thus, 0.128 moles of two-potassium terephthalate and 0.2 28 mo of kgshe benzoate per 1 kg of water; the molar ratio of benzoic acid. and dipotassium terephthalate is 4.286. After the reaction, the mixture leaving the third reactor is sent to a dryer. Separate the mother liquor, part of which is recycled to the first reactor, and 1.35 kg / h of moist terephthalic acid containing approximately 16% of water is separated. Then, terephthalic acid crystals are injected into the shilk with hot water at a rate of 2.5 k. These wash waters are recycled to the first reactor. As a result, after drying, 1.13 kg / h of pure terephthalic acid is obtained (acid number 675 ; content of benzoic acid 900 ppm. Example 4 Into a reactor with a blender, the temperature of which is maintained at 160 ° C, is continuously fed to 1 h: 1.34 kg of double-potassium (5.514 mol) terephthalate 4.03 kg of benzoic (33.033 mol) acid 1 , 85 kg of benzoate (11.562 mol) of 22 kg of water. Thus, 0.251 mol of terephthalate and 0 are added, 525 mol of potassium benzoate per 1 kg of water; the molar ratio of benzoic acid and two-potassium terephthalate is 5.99. After the reaction, the mixture is sent to a dryer operating in isothermic mode at. Separating 2.06 kg / h of terephthalic acid containing 20% water, Kpistal tt terephthalic acid is treated with 2.5 kg of hot water. After separation and drying, 0.85 kg / h of terephthalic acid is obtained, having characteristics identical to those given in Example 2, Example 5, To a stirred reactor whose temperature is maintained at 90 ° C, continuously are introduced: 0.567 kg / h two-potassium (2.333 mol) terephthalate 1.147 kg / h benzoic (9.402 mol) -acids 0.760 kg / h benzoate (4.752 mol) 21.8 kg / h of water Thus, 0.107 mol of two-potassium terephthalate and 0.218 mol are introduced potassium benzoate per 1 kg of water; The mol mol of the ratio of benzoic acid and dipotassium terephthalate is 4.03. After the reaction, the mixture is sent to a dryer operating at. The acid is separated as indicated in Example 4. 0.455 kg / h is obtained (this acid contains 20% water). Recrystallized from hot water, terephthalic acid containing at least 100 benzoic acid is obtained. acid. Example 6, the reaction is carried out analogously to example 3, the temperature in the three reactors is maintained at 250, 210 and 180 ° C, respectively, 1.10 kg / h of pure terephthalic acid is obtained (acid number 675; benzoic acid content is 90 million. Example 7. Reaction wire t as in example 1; the temperature is maintained at 220 ° C.
    2.102 kg / h of two-potassium g of terephthalate (8.650 mol), 7.176 kg / h of benzoic acid (58.82 mol), 0.780 kg / h of benoate. potassium (17.081 mol) 21.9 kg / h of water. Thus, 0.395 mol of two-potassium terephthalate and 0.780 mb of potassium beozoate per 1 kg molar ratio of benzoic acid and, two-potassium terephthalate are equal to 6.8 ...
    The terephthalic acid is separated, as indicated in example 1, is recrystallized from hot water and 1.35 kg / h of acid is obtained (acid number 675; benzoic acid content 90)
    权利要求:
    Claims (2)
    [1]
    Invention Formula
    The method of producing Torephthalic acid by reacting a dilute aqueous solution of dihs terephthalate with benzoic acid when heated, followed by isolation and recrystallization of the target product differs in that, in order to simplify the process and improve the quality of the target product, the aqueous solution containing 0.1-0.0 4 mol of dikshy terephthalate per 1 kg of water, and the process is carried out at a molar ratio of benzoic acid and dicalnaterter Fgttata 412, in the presence of potassium benzoate in an amount of 0.2-0.8 mol 1 kg of water at 90-250®S, followed by isolation of the resulting acid with 85-1bO C and holding single kristgshlizatsii.
    Sources of information taken into account in the examination of 1, USSR Copyright Certificate 168680, c. 07 C 63/26, 1962.
    [2]
    2. US patent 2846468, cl. 260-52Ь, published. 1958 (prototype).
    类似技术:
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    同族专利:
    公开号 | 公开日
    IL52051D0|1977-07-31|
    FR2351081A1|1977-12-09|
    PL102649B1|1979-04-30|
    DD129440A5|1978-01-18|
    PL198010A1|1978-01-02|
    JPS5610901B2|1981-03-11|
    BR7703022A|1977-12-20|
    ATA324377A|1978-11-15|
    SE7705464L|1977-11-12|
    CH599094A5|1978-05-12|
    LU77293A1|1978-06-26|
    AR213522A1|1979-02-15|
    CS193574B2|1979-10-31|
    DE2721255A1|1977-11-17|
    NL7705158A|1977-11-15|
    ZA772788B|1978-04-26|
    GB1542182A|1979-03-14|
    AT350534B|1979-06-11|
    BR7703021A|1977-12-20|
    JPS537635A|1978-01-24|
    FR2351081B1|1980-09-19|
    BE854469A|1977-11-10|
    ES458631A1|1978-02-16|
    AU2501677A|1978-11-16|
    US4212991A|1980-07-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2846468A|1957-03-08|1958-08-05|Hercules Powder Co Ltd|Recovery of terephthalic acid|
    GB975113A|1961-02-01|1964-11-11|Teikoku Jinzo Kenshi Kk|Process for the preparation of terephthalic acid from dialkali metal terephthalates|
    BE788314A|1971-06-01|1973-03-01|Phillips Petroleum Co|PROCESS FOR RECOVERY OF TEREPHTHALIC ACID AND NEW PRODUCT THUS OBTAINED|
    JPS608623B2|1975-10-28|1985-03-04|Mitsubishi Electric Corp|JPS5965702U|1982-10-27|1984-05-02|
    US4540493A|1983-11-30|1985-09-10|Ecolochem, Inc.|Process for treating wash water from the manufacture of terephthalic acid|
    US4675108A|1983-11-30|1987-06-23|Ecolochem, Inc.|Apparatus for treating wash water from the manufacture of terephthalic acid|
    US5074756A|1988-05-17|1991-12-24|Patient Solutions, Inc.|Infusion device with disposable elements|
    US6426430B1|1999-08-30|2002-07-30|Mossi & Ghisolfi Oversears, S.A.|Method for reduction of potassium in an integrated process for the production of 2,6—NDA|
    US6649263B2|2001-11-16|2003-11-18|Honeywell International Inc.|Polyester resin and industrial yarn process|
    US7884231B2|2005-05-19|2011-02-08|Eastman Chemical Company|Process to produce an enriched composition|
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    US7741516B2|2005-05-19|2010-06-22|Eastman Chemical Company|Process to enrich a carboxylic acid composition|
    US20060264656A1|2005-05-19|2006-11-23|Fujitsu Limited|Enrichment process using compounds useful in a polyester process|
    US20060264664A1|2005-05-19|2006-11-23|Parker Kenny R|Esterification of an exchange solvent enriched composition|
    US7897809B2|2005-05-19|2011-03-01|Eastman Chemical Company|Process to produce an enrichment feed|
    US7888529B2|2006-03-01|2011-02-15|Eastman Chemical Company|Process to produce a post catalyst removal composition|
    US7919652B2|2005-05-19|2011-04-05|Eastman Chemical Company|Process to produce an enriched composition through the use of a catalyst removal zone and an enrichment zone|
    US20060264662A1|2005-05-19|2006-11-23|Gibson Philip E|Esterification of an enriched composition|
    US7880031B2|2005-05-19|2011-02-01|Eastman Chemical Company|Process to produce an enrichment feed|
    US7557243B2|2005-05-19|2009-07-07|Eastman Chemical Company|Enriched terephthalic acid composition|
    US7834208B2|2005-05-19|2010-11-16|Eastman Chemical Company|Process to produce a post catalyst removal composition|
    US7432395B2|2005-05-19|2008-10-07|Eastman Chemical Company|Enriched carboxylic acid composition|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    FR7614867A|FR2351081B1|1976-05-11|1976-05-11|
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