Production of acrolein and acrylic acid by catalytic oxidation of propane

    公开(公告)号:DE19807079A1

    公开(公告)日:1999-08-26

    申请号:DE19807079

    申请日:1998-02-20

    Applicant: BASF AG

    Abstract: Heterogeneous, catalytic, gas-phase oxidation of propane to acrolein and/or acrylic acid comprises passing a mixture of propane, oxygen and optionally an inert gas, at 300-500 deg C, over a two-part fixed-bed catalyst, each part containing different, specific mixed metal oxide phases. The catalyst in the first bed (A) has the formula M a Mo1-bM b Ox (I) M = cobalt, nickel, magnesium, manganese and/or copper; M = wolfram, vanadium, tellurium, niobium, phosphorus, chromium, iron, antimony, cerium, tin and/or lanthanum; a = 0.5-1.5; b = 0-0.5; x = a number required to satisfy the valencies of the other components and the catalyst in the second bed (B) has formula Bia,Mob, X c, X d, X e, X f, X g, X h, Ox, (II) X = wolfram, vanadium and/or tellurium; X = alkaline earth metal, cobalt, nickel, zinc, manganese, copper, cadmium, tin and/or mercury; X = iron, chromium and/or cerium; X = phosphorus, arsenic, antimony and/or boron; X = alkali metal, thallium and/or tin; X = rare earth metal, titanium, zirconium, niobium, tantalum, rhenium, ruthenium, rhodium, silver, gold, aluminum, gallium, indium, silicon, germanium, thorium and/or uranium; a' = 0.01-8; b' = 0.1-30; c', d' and e' = 0-20; f' = 0-6; g' = 0-4; h' = 0-15 The starting mixture of reactants contains at least 5 volume % propane, at least 15 volume % oxygen and 0-35 volume % inert gas and it passes through layer A first, then through B.

    REACTOR AND PROCESS FOR PREPARING HYDROGEN SULFIDE

    公开(公告)号:CA2675506A1

    公开(公告)日:2008-07-24

    申请号:CA2675506

    申请日:2008-01-14

    Applicant: BASF AG

    Abstract: The invention relates to a reactor (1) and a method for continuously prod ucing H2S by reacting a feedstock mixture essentially containing gaseous sul fur and hydrogen on a catalyst. The reactor (1) comprises a sulfur melt (9), at least in a bottom subarea (8) of the reactor (1) into which gaseous hydr ogen is introduced. The catalyst is arranged in at least one U-shaped tube ( 21) that is in partial contact with the sulfur melt (9). The at least one U- shaped tube (21) has at least one inlet (23) on a leg (26) above the sulfur melt (9), the feedstock mixture being able to penetrate from a feedstock zon e (10) of the reactor (1) into the U-shaped tube (21) through said inlet (23 ). The at least one U-shaped tube (21) also has an internal flow path, along which the feedstock mixture can be reacted in a reaction zone containing th e catalyst (22), and at least one outlet (24) in another leg (27), a product being able to be discharged into a product zone (7) through said outlet (24 ).

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