US 6,982,347 B2 | ||
Heterogeneously catalyzed partial gas phase oxidation of acrolein to acrylic acid | ||
Martin Dieterle, Mannheim (Germany); Jochen Petzoldt, Mannheim (Germany); Klaus Joachim Müller-Engel, Stutensee (Germany); and Heiko Arnold, Nanjing (China) | ||
Assigned to BASF Aktiengesellschaft, Ludwigshafen (Germany) | ||
Filed on Mar. 23, 2004, as Appl. No. 10/806,460. | ||
Claims priority of provisional application 60/475794, filed on Jun. 05, 2003. | ||
Claims priority of application No. 103 13 211 (DE), filed on Mar. 25, 2003. | ||
Prior Publication US 2004/0192963 A1, Sep. 30, 2004 | ||
This patent is subject to a terminal disclaimer. | ||
Int. Cl. C07C 51/235 (2006.01) |
U.S. Cl. 562—535 | 14 Claims |
1. A process for partially oxidizing acrolein to acrylic acid in the gas phase under heterogeneous catalysis, comprising:
passing a starting gas mixture which comprises acrolein, molecular oxygen and at least one inert gas containing at least 20%
by volume of molecular nitrogen and contains molecular oxygen and the acrolein in a molar O2:C3H4O ratio of ≧0.5 through one reaction stage over a fixed catalyst bed which is arranged in two spatially successive reaction
zones A,B, the temperature of reaction zone A being a temperature in the range from 230 to 320° C. and the temperature of
reaction zone B likewise being a temperature in the range from 230 to 320° C., whose active composition in each reaction zone
is at least one multimetal oxide comprising the elements Mo and V, in such a way that reaction zone A extends to an acrolein
conversion ranging from 45 to 85 mol % and, on single pass of the starting gas mixture through the fixed catalyst bed, the
acrolein conversion is ≧90 mol % and the selectivity to acrylic acid, based on acrolein converted is ≧90 mol %, the chronological
sequence in which the starting gas mixture flows through the reaction zones corresponding to the alphabetic sequence of the
reaction zones, wherein
a) the hourly space velocity of the acrolein contained in the starting gas mixture over the fixed catalyst bed is ≤145 l (STP)
of acrolein/l of fixed catalyst bed·h and ≧70 l (STP) of acrolein/l of fixed catalyst bed·h,
b) the volume-specific activity of the fixed catalyst bed is either constant or increases at least once in the flow direction
of the reaction gas mixture over the fixed catalyst bed, and
c) the difference TmaxA−TmaxB, determined from the highest temperature TmaxA which the reaction gas mixture has within the reaction zone A and the highest temperature TmaxB which the reaction gas mixture has within reaction zone B, is ≧0° C.
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