PRODUCTION OF METHYLGLYOXAL
    42.
    发明专利

    公开(公告)号:JP2000336055A

    公开(公告)日:2000-12-05

    申请号:JP14959699

    申请日:1999-05-28

    申请人: UBE INDUSTRIES

    发明人: SO MAMORU ODAN KYOJI

    摘要: PROBLEM TO BE SOLVED: To produce methylglyoxal useful as a raw material for synthesizing a medicine or the like in high selectivity and high yield by using industrially easily available hydroxyacetone as a raw material, and subjecting the raw material to an oxidative dehydrogenation in the presence of a heteropolyacid compound. SOLUTION: Hydroxyacetone and a molecular oxygen-containing gas are fed to a reactor packed with a heteropolyacid compound of the formula (H1-aAa)3+xPMO12-xVxO40 [A is Li, K, Rb or Cs; (x) is 0-3; and (a) is 0-1], (e.g. H3Mo12O40) to react them in a gas phase to provide the objective methylglyoxal. The molecular oxygen-containing gas is preferably oxygen diluted with an inert gas, or air, and the molecular oxygen, preferably of 0.3-20 mol based on 1 mol hydroxyacetone is fed. The contact time is preferably 0.1-20 sec, and the reaction temperature is preferably 100-300 deg.C.

    CONTINUOUS INDUSTRIAL PRODUCTION OF ALDEHYDE

    公开(公告)号:JPH10338656A

    公开(公告)日:1998-12-22

    申请号:JP14286798

    申请日:1998-05-25

    申请人: BASF AG

    摘要: PROBLEM TO BE SOLVED: To profitably obtain the subject aldehyde in a good yield by subjecting an unsaturated aliphatic alcohol and an oxygen-containing gas to an oxidative dehydrogenation reaction in a bundle reactor. SOLUTION: This method for continuously and industrially producing an aldehyde of formula II comprises passing an oxygen-containing alcohol vapor comprising the vapor of a 3-alkyl-buten-1-ol of formula I (R is H; R is isoprenal, or R and R together forms a prenal group) and an oxygen-containing gas through a silver-carried catalyst layer having a thickness of at least 0.5 cm at a temperature which is higher than the dew point of the alcohol but lower than a reaction-starting temperature, bringing the passed vapor into contact with a silver-carried catalyst in parallel plural reaction pipes each having an inner diameter of about 0.5-3 cm and a length of at least 5 cm and heated with a liquid thermal medium flowing around the reaction pipes at 300-600 deg.C to subject the vapor to an oxidative dehydrogenation reaction, immediately cooling the reaction gas and subsequently separating the aldehyde of formula II from the obtained condensed product.

    47.
    发明专利
    失效

    公开(公告)号:JP2824538B2

    公开(公告)日:1998-11-11

    申请号:JP50737490

    申请日:1990-05-08

    摘要: The method uses a starting material which is a liquid mixture consisting of a formaldehyde proportion comprised between 48 and 55 % by weight, a methanol proportion comprised between 20 and 30 % by weight and a water proportion comprised betweeen 32 and 15 % by weight; the liquid mixture is obtained from a tapping which is effected from a plant for the continuous preparation of urea-formaldehyde resins and glues, immediately after having subjected the methanol to catalytic oxidation via air, condensation of the gases evolving from said catalytic oxidation and separation between condensed products and uncondensed gases. These solutions may be applied to formaldehyde reactions wherein it is of interest to reduce the amount of water present in conventional solutions and also to use the methanol for example as solvent for the final product obtained.

    CATALYST AND PRODUCTION OF UNSATURATED ALDEHYDE AND UNSATURATED ACID

    公开(公告)号:JPH1028877A

    公开(公告)日:1998-02-03

    申请号:JP8462797

    申请日:1997-03-19

    申请人: NIPPON KAYAKU KK

    摘要: PROBLEM TO BE SOLVED: To suppress the heat accumulation of hot spots of a catalyst bed and to obtain an objective product in high yield by supporting a catalytically active component on a carrier and sintering the carrier to obtain a catalyst wherein an average particle size, the average particle size of the carrier, baking temp. and the support amt. of the catalytically active component to the carrier are set to specific ranges. SOLUTION: After a catalytically active component is supported on a carrier, this supported carrier is sintered to obtain a catalyst. In this case, the particle size of the catalyst is set to 4-16mm, the average particle size of the carrier is set to 3-12mm, baking temp. is set to 500-600 deg.C and the support amt. of the catalytically active component to the carrier is set to 5-80wt.%. The compsn. of the catalytically active components is represented by the formula Moa Bib Nic Cod Fef Yg Zh Ox (wherein Y is tin, zinc, tungsten, chromium, manganese or the like, Z is potassium or rubidium, h and x are molybdenum or bismuth, a is 12, b is 0.1-7, (c+d) is 0.5-20, f is 0.5-8, g is 0-2 h is 0-1 and x is a value determined by the oxidized state of respective elements).