• 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 relates to catalytic processes of the main organic synthesis, in particular, catalyst (Kt) based on manganese and cobalt acetates from dimethyl terephthalate (OSDMT) production residues. To simplify the process and improve the degree of excretion of CT, the initial HMDC is processed under other conditions. First, the SMTP is subjected to extraction at 85-1OO C with reaction water (PB) containing acetic and formic acids at a weight ratio of 1: 0.27-0.80 to obtain a wave phase containing Kt and an organic phase. The latter is mixed with PB in the above ratio at 85-00 ° C for 0.1-120 s. After separation, the water phase is fed to the extraction of the SMTP, and the organic is removed from the process. The degree of satisfaction is 99.8%. 1 il. (Y) 2 liters; about 05 cm
    公开号:SU1251796A3
    申请号:SU853885102
    申请日:1985-04-26
    公开日:1986-08-15
    发明作者:Бюнгер Гейнрих；Кордес Рудольф；Гоффманн Герхарт
    申请人:Динамит Нобель Аг (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to a method for separating a metal catalyst from a residue, in particular, to a method for separating a catalyst based on cobalt and manganese acetates from a residue of dimethyl terephthalate production.
    The aim of the invention is to simplify the process and increase the degree of catalyst allocation.
    The drawing shows the technological scheme of the proposed method.
    The method is carried out as follows.
    The pipeline 1 into the mixer 2 serves the remainder of the production of dimethyl terephthalate. In the mixer 2 through the pipeline 3 serves the aqueous phase obtained by separation in the sump 4. Obtained in the mixer 2, the emulsion is fed through the pipeline 5 to the separation in the sump 6. This produces a catalyst phase containing the catalyst, which is removed from the process by pipeline 7, and an organic phase, which is withdrawn through conduit 8 and fed to the suction pipe 9 of the pump 10, into which an extractant, reaction water containing acetic and formic acids is fed through conduit I1. The resulting mixture is fed through a pipe duct 12 D sump 4 in which the separation is carried out into the aqueous phase supplied via conduit 3 to mixer 2, and the organic residue withdrawn from the process via conduit 13.
    The invention is illustrated by the following examples.
    In npifMepax, the residue produced by D1-1methyl terephthalate contains 0.40% by weight cobalt and 400 ppm manganese. It is obtained by the liquid-phase oxidation of p-xylol and p-toluic acid methyl ester with oxygen at 150–170 ° C and a pressure of 5–8 bar in the presence of a solution of cobalt and manganese acetates in the reaction water obtained as a condensate of secondary vapors. and containing on average wt.%: acetic acid 2.5, formic acid 1.5; methanol 6.0 and formaldehyde 0.8, - and in the oxidation product a steady-state concentration of about 90 ppm of cobalt is established and at 171796i
    approximately 10 ppm manganese, subsequent esterification of the oxidation product with methanol at 250-280 ° C and a pressure of 20-25 bar and separation of the product
    5 etherification and two-stage vacuum distillation. The yield of pure dimethyl terephthalate is 89.5-90 mol%.
    Example 1. 800 kg / h residue
    10 of the production of dimethyl terephthalate, containing 0.40 wt.% (3.2 kg) of cobalt and DOS ppm (0.32 kg) of manganese, is continuously fed into a mixer 2 equipped with a stirrer, in which
    15, the residue is mixed with 213 kg / h of the aqueous phase discharged from the settling tank 4 at 94 ° C for 4 hours. The ratio of the residue to the reaction water, which is the extractant, is 1: 0.27. 1013 kg / h of the emulsion are continuously drained from the mixer through the valve in the bottom into the sump 6. In this sump, the emulsion is divided into 210 kg / h of the aqueous phase, containing 25 wt.% (3.14 kg) of cobalt, 0.15 wt.% (0.314 kg) of manganese, 0.74 wt.% of trimethyltitol acid and 230 ppm of iron, and 803 kg / h of the organic phase, consisting of a residue of 30k and containing 0.0075 wt.% (0.06 kg ) cobalt, 0,003 wt.% (0,006 kg) manganese and 0.35 wt.% water. The separation process is carried out at 94 ° C for 20 hours.
    35 Both phases are continuously withdrawn from the settler 6, the organic phase being fed to the settling tank 4 by means of a vane pump 10, into the suction pipe 9 of which, simultaneously with
    40 organic phase serves 210 kg / h of reaction water. At the same time, the ratio of the organic phase and the reaction water, which serves as the extractant, is 1: 0.27, and their average
    The 45 residence time in the vane pump 10 is 1.2 s. The mixture obtained in the pump is fed to a settling tank 4, in which the separation into 213 kg / h of the aqueous phase supplied
    50 to mixer 2, and to 800 kg / h of organic residue containing 0.00088% by weight (0.007 kg} of cobalt and 0.88 ppm (0.0007 kg) of manganese, which is removed from the process. 55 carried out at 94 ° C for 10 hours. i
    The degree of cobalt and manganese is 99.8%.
    3
    EXAMPLE 2 Example 1 is repeated, with the difference that the solution flowing out of the sump 6 is filtered using coarse-grained active carbon. The results are the same as in example 1, with the difference that the content of the glands in the resulting solution is 15 ppm.
    Example 3. Example I is repeated, with the difference that the mixing and separation processes are carried out at 85 C.
    The degree of improvement of the catalyst is 99.6%.
    EXAMPLE 4 Example 1 is repeated, with the difference that the mixing and separation processes are carried out at 100 ° C.
    The catalyst recovery rate is 99.85%.
    EXAMPLE 5 An example is repeated with the difference that the residence time of the phases in the vane pump is 0.1 s.
    The degree of catalyst utilization is 99 EXAMPLE 6. An example is repeated with the difference that the mixing and separation processes are carried out at 100 ° C and the residence time of the phases in the vane pump is 120 s.
    Catalyst Degree 99.95%.
    Example. Example 1 is repeated with the difference that the processes of mixing and separation are carried out at a ratio of the reaction water to the initial residue and the organic phase equal to 0.8: 1, and the organic phase is mixed with the reaction water at 94 ° C for 120 s.
    The catalyst recovery rate is 99.96%.
    An example (comparative. Repeat example 1 with the difference that the processes of mixing and separation are carried out at 80 C.
    The degree of release of the catalyst is 93.5%.
    PRI me R 9 Comparative). Example 1 is repeated, with the difference that the residence time of the phases in the vane pump is 0.05 s.
    Catalyst recovery rate 94
    PRI me R 10 (comparative). Example 1 is repeated, with the difference that the mixing and separation processes are carried out at 110 ° C, and the residence time of the phases in the hazardous pump
    five
    Q
    five
    0
    5 o

    d
    five
    0
    7964
    lt 1 30 s. The degree of separation of the catalyst is 99.95%,
    The regenerated catalyst of Example 1 is used in the production of dimethyl terephthalate.
    权利要求:
    Claims (1)
    [1]
    Example 11 80 kg / h of p-xylol and 93 kg / h of p-toluic acid methyl ester are subjected to liquid phase oxidation with 60 nm / h of air at 160 ° C and a pressure of 8 bar in the presence of regenerated ca- , a tapiser of example 1, consisting of 20 g of cobalt and 15 g of manganese in the form of acetates dissolved in 2% aqueous acetic acid. The resulting oxidation product is subjected to esterification of 80 kg / h of methanol at 250 ° C and a pressure of 25 bar. The esterification product is subjected to continuous two-stage fractional distillation, and in the first stage they operate at a temperature in the cube of 150 ° C, a pressure of 15 mbar and a reflux number of 0.3, and in the second stage - at a temperature in the cube of 90 ° C, a pressure of 100 mbar mbar and reflux ratio 1.0. With this, 237 kg / h (89.7 mol.%) Of dimethyl terephthalate are obtained with a mp of 140.62 ° C (almost 100% purity). The remainder of the re-race serves to release the catalyst. Invention Formula
    A method for separating a catalyst based on cobalt and manganese acetates from a dimethylterapaphate production residue by extracting the residue with reaction water containing acetic and formic acid at a temperature of 85-1OO C and separating it into an aqueous phase containing cobalt and manganese acetates and the organic phase containing the residue This is due to the fact that, in order to simplify the process and increase the degree of catalyst separation, the residue is extracted with reaction water at a mass ratio of residue and reaction water I : (0.27-0.8), the organic phase obtained as a result of the extraction is mixed with reaction water containing acetic and formic acids, in a mass ratio of the organic phase and the reaction water 1: (0.27-0.8) at a temperature 85-100 ° C for 0.1-120 seconds, followed by separation of the resulting mixture into the aqueous phase, which is fed to the extraction of the initial residue, and the organic residue that is removed from the process.
    eleven
    Compiled by N.Putov
    Editor L. Veselovska Tekhred L. Serdyukova Proofreader E. Rothko
    Order 4428/60 Circulation 527 Subscription
    VNIIPM USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Ra t1ska nab. D. 4/5
    Production and printing company, Uzhgorod, st. Project, 4
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    同族专利:
    公开号 | 公开日
    IN155427B|1985-01-26|
    JPS57119841A|1982-07-26|
    EP0053241B1|1984-09-12|
    DE3166060D1|1984-10-18|
    BR8107823A|1982-09-08|
    US4464477A|1984-08-07|
    DE3045332A1|1982-06-03|
    JPS609865B2|1985-03-13|
    DE3045332C2|1982-11-25|
    EP0053241A1|1982-06-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    PL70344B1|1971-10-28|1974-02-28|
    DD104973A5|1972-09-12|1974-04-05|
    JPS522896B2|1973-01-18|1977-01-25|
    DE2427875C3|1974-06-10|1980-03-20|Dynamit Nobel Ag, 5210 Troisdorf|Process for the production of dimethyl terephthalate and of intermediates in dimethyl terephthalate manufacture|
    US4096340A|1975-06-03|1978-06-20|Teijin Hercules Chemical Co., Ltd.|Process for the preparation of dimethyl terephthalate|
    DE2923681C2|1979-06-12|1981-11-05|Dynamit Nobel Ag, 5210 Troisdorf|Process for the recovery and reuse of heavy metal oxidation catalyst from the Wittem DMT process|
    US4353810A|1981-01-21|1982-10-12|Hercofina|Minimizing iron in recovered oxidation catalyst material in DMT process|US4868324A|1988-05-24|1989-09-19|Celanese Engineering Resins, Inc.|Purification of diphenyl phthalates|
    DE4026732A1|1990-08-24|1992-02-27|Huels Chemische Werke Ag|METHOD FOR CLEANING AN OXIDATION EXHAUST GAS WITH ENERGY RECOVERY|
    US5414106A|1994-02-14|1995-05-09|Hoechst Celanese Corporation|Process for recovering dimethyl terephthalate|
    DE19530970A1|1995-08-23|1997-02-27|Huels Chemische Werke Ag|Process for processing residues from crude ester distillation in the production of dimethyl terephthalate |
    DE19618152C1|1996-05-07|1997-08-14|Huels Chemische Werke Ag|Energy-saving separation of crude di:methyl terephthalate fraction under mild conditions|
    KR100450528B1|1996-12-19|2004-11-26|에스케이케미칼주식회사|Method for recoveringcatalytic material for oxidation with high purity from sludges generated fromdimethylterephthalate manufacturing process|
    KR19990025109A|1997-09-10|1999-04-06|조민호|Recovery of Cobalt Catalyst from Terephthalic Waste Sludge|
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    CN105017022A|2015-07-20|2015-11-04|浙江大学|Method for methyl esterification recovery and recycle of PTA oxidation residue|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE3045332A|DE3045332C2|1980-12-02|1980-12-02|Process for the recovery and reuse of heavy metal oxidation catalyst from residues in the Witten DMT process|
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