PREPARATION OF POLYPHENYLENE ETHERS, AND AN APPARATUS FOR THIS PURPOSE

    公开(公告)号:CA1263992A

    公开(公告)日:1989-12-19

    申请号:CA495489

    申请日:1985-11-15

    Applicant: BASF AG

    Abstract: Disclosed is a process of preparation of polyphenylene ethers from monohydric phenols, which possess alkyl substituents in the two ortho-positions and, if desired, in the meta-position, but not in the para-position, by an oxidative coupling reaction with oxygen at from 15 to 50.degree.C and under from 1 to 10 bar in the presence of a catalyst complex, of a solvent and, if required, of an activator. In this process,the conversion of the phenols is carried out in two or more reaction zones. Some or all of the solvent, catalyst complex phenols and where relevant, activator are initially added to one of the reaction zones and are circulated in the other reaction zone and about 60-100% of the stoichiometric amount of oxygen required for the oxidative coupling is introduced into the first reaction zone and from 0 to about 40% of the said stoichiometric amount is introduced into the second reaction zone. This process is interesting in that it makes it possible to carry out oxidative coupling of phenols with oxygen in a very economic and reliable manner, with very high space-time yields, formation of only a small amount of by-products, and minimum emissions of gas and volatile components.

    Polyphenylene ether(s)] prodn. - by continuous two=stage oxidative coupling of phenol(s) in a reactor with full back-mixing followed by a reactor with partial back-mixing

    公开(公告)号:DE4209633A1

    公开(公告)日:1993-09-30

    申请号:DE4209633

    申请日:1992-03-25

    Applicant: BASF AG

    Abstract: A process is claimed for producing polyphenylene ethers (I) by continuous 2-stage catalytic reaction of oxygen with aromatic mono-hydroxy cpd(s). (II). Stage (1) is carried out in a reactor with largely complete back-mixing, and stage (2) in a reactor with partial back-mixing. Also claimed in an appts. for the process, with 2 reactor (systems) as above. Pref. stage 1 is carried out in a ga/liq. reactor (jet reactor) with a jacket tube which is blanked off at the top and in which one or more downwardly directed liq. jets are mounted at the highest point and fed from a liq. pump circuit, so that a gas phase is entrained with and then completely dispersed in the liq.; before starting the liq. circulation, the static reactor is filled with only enough liq. to leave a gas space at the top of the reactor corresp. to the subsequent hold-up under operating conditions, this gas space is filled with inert gas at pressure pl, and the gaseous reactants are only introduced into the reactor when the action of the liq. jets has produced a dispersion of inert gas such that a coherent gas phase no longer exists. The reactor system in stage 1 consists of a jet reactor, a circulating pump and a heat exchanger. Stage 2 is carried out in a continuous flow-tube reactor. USE/ADVANTAGE - The process enables the prodn. of (I) with higher space-time yields (w.r.t. prior-art processes for PPE with comparable mol. wt.), shorter residence times, smaller amts. of off-gas and reduced by-prod. formation

    4.
    发明专利
    未知

    公开(公告)号:DE3578428D1

    公开(公告)日:1990-08-02

    申请号:DE3578428

    申请日:1985-11-07

    Applicant: BASF AG

    Abstract: Polyphenylene ethers are prepared from monohydric phenols, which possess alkyl substituents in the two ortho-positions and, if desired, in the meta-position, but not in the para-position, by an oxidative coupling reaction with oxygen at from 15 DEG to 50 DEG C. and under from 1 to 10 bar in the presence of a catalyst complex, of a solvent and, if required, of an activator, by a method in which the conversion of the phenols is carried out in two more reaction zones, in which some or all of the solvent, the catalyst complex and the phenols and, where relevant, the activator is initially taken and is circulated by means of a conveying unit, and about 60-100% of the stoichiometric amount of oxygen required for the oxidative coupling is introduced into the first reaction zone and from 0 to about 40% of the said stoichiometric amount is introduced into the second reaction zone.

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