• 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:
    A method of recovering the catalyst in active form from the acetic mother liquors from the synthesis of terephthalic acid. From said mother liquors, after removal of water, there is removed by evaporation an amount of from 70 to 90% of the CH3COOH present therein. The concentrated liquor is cooled below 60 DEG C. and the solid which precipitates is collected and recycled for reuse in the systhesis. The liquid phase is extracted with water or with an aqueous acetic acid solution in the presence of particular coadjuvants such as isobutyl acetate, and the aqueous phase, which contains the recovered catalyst, is recycled to the original synthesis.
    公开号:SU1194260A3
    申请号:SU813263198
    申请日:1981-01-22
    公开日:1985-11-23
    发明作者:Рофья Паоло；Калини Пьеранджело；Тонти Серджо
    申请人:Монтэдисон С.П.А.(Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods for the recovery of catalysts for the synthesis of terephthalic acid.
    The aim of the invention is to increase the purity of the available
    certain
    catalyst due to the extraction conditions.
    Example 1. A. Oxidation of p-xylene and separation of the catalyst from a concentrated solution.
    720 g of acetic acid 1, containing 0.67 g of cobalt acetate tetrahydr., Cobalt acetate, 1.99 g of manganese acetate tetrahydrate and 1.23 ml of an aqueous solution containing 40 mA (°, HBg, are loaded into a 2 l titanium autoclave supplied with thermally heated and equipped with a stirrer and reflux condenser. The resulting solution is heated to 220 ° C, maintaining a nitrogen pressure of 24 kg / cm in the autoclave. In the autoclave maintaining a stirring speed of 660 rpm, 200 m of solution is introduced, 79% by wt. xylene in acetic acid and some amount of air needed to increase neither the oxygen concentration in the purge gas, which is continuously fed to maintain
    pressure on the peruver level equal to 24 kg / cm initially up to about 2-2.5% by volume. After two hours, the reaction mixture is cooled and the suspension of terephthalic acid is separated by filtration of the mother liquor, washed with acetic acid and water, and dried in a drying cabinet under vacuum at 100 ° C. The output of p-xylene 94J8%. Polygraphic (analysis indicates the presence of 400 ppm of 4-carboxybenzaldehyde (4-CBA), optical transmittance of a 15% jHoro solution of the product in 2N hydrate of sodium oxide at 340 nm of 78%. The mother liquor remaining after filtration is dispersed after distilling off about 90% of the solvent residue
    subjected to secondary distillation
    at 25 ° C, creeping out
    solid phase precipitate, consisting mainly of terephthalic acid (68 wt.%), p-toluic acid; 1 (15%), .4-CBA (10%) and benzoic acid (3%), also containing 30% of the total the amount of manganese and 15% of the total amount of cobalt used in o.pyte. The residue is filtered off and 100 g of p-xylene is added to the filtrate, which contains most of the catalyst and undesirable by-products of the synthesis (mass ratio: liquid phase: acetic acid: p-xylene: 100: 94: 104). presented in table. 1.
    The heavy phase (27.56 g) containing the major part of the catalyst is recycled to the oxidation step. The aqueous phase, consisting of acetic acid and p-xylene, is accelerated to separate the volatile components. The residue, consisting of a small portion of the catalyst and by-products, is decomposed.
    Thus, the following table. 1, the method has maximum efficiency with respect to the selective isolation of virtually all of the catalytic components in the heavy phase (water — acetic acid), which contains the minimum amount (4%) of all impurities present in the system. The heavy phase can be recycled to the oxidation stage without further processing, and this light phase results in practically all the quantities of impurities present in the system in addition to the minor amount of catalytic components
    B. Reuse of the isolated catalyst in the secondary oxidation reaction.
    27.56 g of the heavy phase is made up of 0.66 g of Mn (CH3COO) and 4H20. 0.157 g of Co (CH, COO) g of 4H20 and 0.242 ml of an aqueous solution containing 40% by weight of HBg and loaded into an autoclave together with 700 g of acetic acid. The resulting mixture is heated at a pressure of 24 kg / cm, with stirring at a speed of 600 rpm, after which a solution containing 79% by weight of p-xylene in acetic acid is added at an injection rate of 200 MP / h. Air is continuously supplied to the purge gas, bringing its oxygen content to 2-2.5% by volume and. . maintaining a pressure of 24 kg / cm.
    Two hours after the introduction of the reagents, the reaction mixture is cooled, the terephthalic ACID is separated by filtration, washed with acetic acid and water, and dried in a drying cabinet at 100 ° C under vacuum. Yield 94.8% 4-CBA content in the product 420 ppm and the transmittance at 340 nm is 77%. When using a catalyst consisting of 80% of the catalyst isolated from the process and 20% of a freshly prepared catalyst, the yield and quality of terephthalic acid is fully equivalent to the corresponding values obtained using only a freshly prepared catalyst. Example 2 (comparative). Directly recycling the dehydrated stock solution. The oxidation process is carried out similarly to Example 1 (A) And with the same results. The mother liquor is separated by filtration of terephthalic acid and is subjected to distillation to remove the water that is present during the reaction, after which 0.185 mp of an aqueous solution of HBg (40% by weight) for combs is added to the dry solution containing acetic acid, catalyst and intermediate products of the reaction. loss of compensation. This solution in an amount of 725 g is reintroduced into the autoclave and the oxidation process is repeated under the same conditions. After cooling, the terephthalic acid is separated by filtration, washed and dried. The yield is 95.4%, the content of 4-KB is 50 ppm, and the transmittance at. 340 nm (for a 15% solution in 2 N. KOI) is 60%. Example 3. The oxidation process is repeated as in Example 1, wherein, after distillation, 7.4 g of solid phase consisting of terephthalic acid, intermediate reaction products and part of the catalyst are distilled from the mother liquor. By adding 100 g of p-xylene to the remaining solution (mass ratio liquid phase: acetic acid: p-xylene 100: (94: 104), 25 g of a heavy phase containing 66% of the initial. Manganese, 7-4% from the initial amount of cobalt and 85% of the initial amount of bromine. The solid and heavy phases are combined and 0.0796 g of Mn () 2411 0, 0.0737 Co (CH3SOO) -41120 and 0.177 ml solution of HBg are added to the mixture. (40 wt.%), After which it is introduced into the autoclave together with 700 g of acetic acid. The repeated process of the oxide is carried out at 220 ° C and a pressure of 24 kg / cm, supplied at Into the autoclave, a stream of air and a 79% solution of p-xylene in acetic acid supply rates of 650 l / h and 200 ml / h, respectively. After 2 h, the solution is cooled and the terephthalic acid is extracted under normal conditions, and then dried it is in the substantial cabinet at 100 ° C. The yield is 96.2%, the content of 4-CBA is 430 MD, and the transmission of terephthalic acid at 340 nm for a 15% solution in 2 N. NaOH is 78%. Example 4. 3600 g of a solution containing 3.35 g of Co (C1TCOO) 2-4H20 3.35 g G9, 95 g of (C1TCOO) 2-4H20, and 6.15 mp ++ / aqueous 40% (by weight) solution of HBg, are introduced in a titanium autoclave with a capacity of 5 liters, equipped with Alcoy,, a heat exchanger for heating and reflux. The reaction mixture is heated under nitrogen at a pressure of 24 kg / cm while stirring at a speed of 600 rpm and a 1000 ml / h solution containing 79 wt.% Of p-xylene in acetic acid is added to it. At the same time, air is supplied in such an amount that the oxygen content in the purge gas is 2-2.5% by volume at constant pressure. After 2 hours from the start of the process, the reaction mixture is cooled to 20 ° C and the terephthalic acid is separated by filtration. The product, washed with acetic acid and water and dried in an oven at 100 ° C in a vacuum, contains 420 ppm. 4-CBA and has a transmission (in the form of a solution in sodium hydrate), equal to 76%. Yield 94.5%. The mother liquor is dispersed to 90% acetic acid before transfer to the gas phase, then cooled to., The solid phase is separated by filtration and precipitated, then 500 g of isobutyl acetate and 300 ml of water are added to the filtrate (mass ratio liquid phase: acetic acid : isobutyl acetate 100: 153: 100}, The composition of the phases and the distribution coefficient are given in Table 2. B. Prepare 220 g of the indicated heavy phase from 4.38 g (,: 1.072 g (1) and 1, 86 ml of hydrobromic acid) (40 wt.%) And injected into the autoclave together with 3500 g of acetic acid. The oxidation reaction is carried out at those as before, with a yield of 94.5%, a 4-CBA 430 MP content, a transmittance of 75%. Example 5. A. The process is repeated as in Example 4 (A), but only 50% of the stock solution concentrate, cool, filter and extract. The remaining 50% is directly loaded into the autoclave without any treatment and oxidized according to the very large method (B). B, 50% of the raw stock solution obtained according to the method, and 110 g t phase obtained by treating a concentrated solution of 250 g of isobutyl acetate (mass fraction Liquid phase: acetic acid: isobutyl acetate 100: -53: 1 00) is charged to an autoclave and re-oxidized. The concentration of manganese5 cobalt and bromine is brought to the initial value and oxidation is carried out under the same conditions as before, obtaining a yield of 95.2%, a content of 550 ppm, a transmittance of 72%. Example 6: The operations are repeated as in Example 4, however, second butyl acetate is used together with isobutyl acetate, and similar results are achieved, for example, 7 (comparative). A In a temperature-controlled titanium autoclave, on a 6 liter tank, equipped with a stirrer and reflux condenser, 2500 g of a solution of the following composition, wt.%, Are added: Hydroxy acid 88 Cobalt - 0, 0180 the mixture is stirred and heated until 220 ° C, after which 6,500 g / h of a mixture consisting of 75% by weight of the solution of this composition and 25% by weight of xylene are added to it. At the same time, air is supplied to the reactor with a flow rate of 6,500 l / h. The resulting pressure is adjusted to a value of j equal to 24 kg / cm, and the oxygen concentration in the purge gases is 3 vol.%. At the same time, the suspension of terephthalic acid is continuously withdrawn and the process is continued for 10 hours. The product is continuously extracted, cooled, filtered, washed with acetic acid and water, and finally dried under vacuum at 10 hours after the resulting terephthalic acid (yield 93.5%) contains 2100 ppm 4-CBA and has a pass5 of 45%. 60a B. By filtering the product obtained in A, a stock reaction solution is obtained, which is dispersed in a dehydration column. A dehydrated solution in acetic acid, containing only 3% by weight of water, the whole amount of cobalt and manganese, is returned to the reaction, and some of the bromine remains as residual. the product, the rest of the bromine is removed in various ways, for example in the form of methyl bromide mixed with vapors during distillation. The reactor was charged with 2500 g of fresh catalytic solution having the same composition as in A, and 6,500 g / h of a mixture consisting of 25% by weight of P xylene and 75% of the anhydrous solution (obtained during the distillation of uterine solution). To the mixture is added. proper amounts of bromine ion to compensate for losses. The process is carried out according to the described method (A) and, after 10 hours, receive terephthalic acid (yield 94.5%) containing 3500 ppm, 4-CBA and having a transmittance reduced to 30%, which indicates a negative effect recycled impurities contained in a dehydrated mother liquor. Example 8. The stock solution obtained by filtration according to Example 7 is divided into two equal parts (H) and (K). One of them - (H) is dehydrated and the bromine ion is added anapogically as in Example 7 (c), and the second (K) is heated in an evaporator until 90% of acetic acid is transferred to the gas phase. The residue after distillation is cooled. to 25 ° C and the solid phase, which precipitates upon cooling, is separated from the liquid phase, which is transferred to an extraction device. Lastly, isobutyl acetate and water were introduced in a liquid phase: water mass ratio; isobutyl acetate 100: 146: 170. Almost immediately, two immiscible phases are formed, the compositions of which and the distribution coefficient are given in Table. 3, the T-phase containing catalyst 5, in which there are no impurities, is shifted with a portion (H) of the mother liquor that does not undergo an extraction treatment. After filling up the losses, the working mixture containing 25 wt.% P-xipol is again subjected to oxidation in similar
    71
    conditions After 10 h, terephthalic acid is obtained (yield 94%) containing 2400 ppm. 4-CBA and 45% transmittance. From the results of the experiment it follows that satisfactory results can be obtained even when more than 90% of cobalt and manganese recycled to the oxidation zone is used in the synthesis without prior annealing of the Co and Mp compounds or without any complex treatment with their acids, bases, or ion exchange resins.
    Example 9. All operations are repeated as in Example 8, but with -substituted isobutyl acetate with p-xylene, using the mass ratios for liquid phase: water: p-xylene 100: 85: 134, After 10 h, terephthalic acid is obtained (c, yield 94 %), containing 2350 m, d, 4-CBA and having a transmittance of 45%. The composition and distribution between phases during extraction are given in Table 4.
    Thus, the proposed method allows to select a catalyst in an amount exceeding 80% of the total amount of catalytic components (cobalt, bromine, manganese, while its activity is kept at the initial level and allocated 608
    The catalyst can be directly recycled, in whole or in part) to the oxidation zone of p-xylene.
    The proposed method can be easily implemented, it eliminates the problem of accumulation of by-products that are catalytic. dami, makes the catalyst recyclization process virtually unlimited in terms of the multiplicity, and a high degree of recyclization is achieved without adversely affecting
    oxidation process and product quality. Termination of the solvent distillation (acetic acid) after distillation of 70-90% of its initial amount allows the release of terephthalic acid.
    the acid passing through the centrifugation stage, as well as the intermediate reaction products present in solid form in the final fractions remaining during the distillation of the solvent,
    no by-products that remain in the liquid phase. Thus, it is possible to recyclize terephthalic acid and its intermediate products.
    thesis, which also increases the yield
    target product.
    Spreadsheets
    18.14
    9.79 67.84
    acid 0.44 1.082 1.982
    cue side
    0.696
    97.3
    78
    10 A, 5 5.5
    96
    Water
    Acetic acid
    Isobutyl acetate
    Cobalt
    Manganese
    Bromine
    Organic impurities
    Table
    权利要求:
    Claims (1)
    [1]
    METHOD FOR REMOVING THE TERPHTHALIC ACID SYNTHESIS CATALYST based on cobalt acetate, manganese acetate and bromine from the mother liquor obtained after separation of terephthalic acid, including distillation of up to 70-90% acetic acid and water from the mother liquor, characterized in that, in order to increase the purity of the precipitated catalyst hydrochloric acid or water in the presence of an additive - p-xylene or isobutyl acetate, or sec-butyl acetate at a weight ratio of the liquid phase of acetic acid or water and an addition of 100: (85-153) :( 100-170) at 20- 45 ° С followed by separation of the solid phase and its return to the synthesis zone.
    SU_. 1194260>
    1 1194260
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    同族专利:
    公开号 | 公开日
    IT1129759B|1986-06-11|
    GB2067563B|1984-03-21|
    JPS56113346A|1981-09-07|
    ES498729A0|1982-04-01|
    FR2473903A1|1981-07-24|
    BR8100324A|1981-08-11|
    DE3101672A1|1981-11-26|
    IT8019393D0|1980-01-23|
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    ES8203323A1|1982-04-01|
    CA1152481A|1983-08-23|
    US4356319A|1982-10-26|
    GB2067563A|1981-07-30|
    BE887212A|1981-07-23|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    IT19393/80A|IT1129759B|1980-01-23|1980-01-23|METHOD TO RECOVER IN ACTIVE FORM THE COMPONENTS OF THE CATALYTIC SYSTEM OF THE SYNTHESIS OF TEREPHTHALIC ACID|
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