Method for the hydrogenation of aromatic nitro compounds
The present invention relates to a process for the preparation of an aromatic amine by hydrogenation of an aromatic nitro compound, comprising the following steps: (I) providing a copper tetramine salt-based impregnation catalyst, in particular an impregnation catalyst obtainable by the incipient wetness method, comprising a metal or metal oxide on a support as a hydrogenation catalyst. At least metallic or oxidic copper (in particular CuO) is present and the mole fraction of Cu based on all metals present is in the range of 075 to 1, and wherein the support comprises shaped silicon-dioxide shaped bodies or silicon-carbide shaped bodies; (II) optionally, activating the hydrogenation catalyst by treating with hydrogen in the absence of the aromatic nitro compound; and (III) reacting the aromatic nitro compound with hydrogen in the presence of the, optionally activated, hydrogenation catalyst to obtain the aromatic amine.
1 . A process for preparing an aromatic amine by hydrogenating an aromatic nitro compound, comprising:
(I) providing a tetraamminecopper salt-based impregnated catalyst comprising a metal or metal oxide on a support as hydrogenation catalyst, where at least metallic or oxidic copper is present and the molar proportion of copper, based on all metals present on the catalyst, is 0.75 to 1, and where the support comprises discrete particles of silicon dioxide or silicon carbide having an average diameter of 4.0 mm to 15 mm;
(II) optionally activating the hydrogenation catalyst by treating with hydrogen in the absence of the aromatic nitro compound; and
(III) reacting the aromatic nitro compound with hydrogen in the presence of the optionally activated hydrogenation catalyst to obtain the aromatic amine,
wherein the hydrogenation catalyst comprises a tetraamminecopper carbonate-based impregnated catalyst, and
wherein the aromatic nitro compound is of the formula:
in which R1 and R2 are hydrogen.
2 . The process as claimed in claim 1 , in which step (II) is conducted and the treatment with hydrogen is effected at a temperature of 180° C. to 240° C.
3 . The process as claimed in claim 1 , in which step (III) is conducted:
adiabatically at a temperature of 160° C. to 500° C.,
or
isothermally at a temperature of 180° C. to 550° C.
4 . The process as claimed in claim 1 , in which step (III) is conducted:
adiabatically at a molar ratio of hydrogen to nitro groups of 10 to 200,
or
isothermally at a molar ratio of hydrogen to nitro groups of 3 to 100.
5 . The process as claimed in claim 1 , in which the proportion by mass of copper compounds, calculated as metallic Cu, in the hydrogenation catalyst provided in (I), based on the total mass thereof, is 3% to 35%.
6 . The process as claimed in claim 1 , in which the hydrogenation catalyst used comprises a tetraamminecopper carbonate/ammonium carbonate-based impregnated catalyst or a tetraamminecopper carbonate/ammonium acetate-based impregnated catalyst.
7 . The process as claimed in claim 1 , in which step (I) comprises:
(a) dissolving a copper carbonate in aqueous ammonia to obtain an ammoniacal copper carbonate solution;
(b) impregnating the support with the ammoniacal copper carbonate solution obtained in (a), followed by drying of the impregnated support thus obtained to obtain a catalyst precursor, and
(c) calcining the catalyst precursor obtained in (b) to form the tetraamminecopper-based impregnated catalyst.
8 . The process as claimed in claim 7 , in which the ammoniacal copper carbonate solution used for impregnation has a pH at 20° C. of 7.0 to 14.
9 . The process as claimed in claim 7 , in which the support in step (b) is impregnated with the ammoniacal copper carbonate solution obtained in (a) in such a way as not to exceed the maximum absorptivity of the support determined by means of saturation with water.
10 . The process as claimed in claim 9 , in which the maximum absorptivity of the support is undershot by not more than 5%.
11 . The process as claimed in claim 9 , in which the maximum absorptivity of the support is undershot by at least 2%.
12 . The process as claimed in claim 10 , in which the maximum absorptivity of the support is undershot by at least 2%.
13 . The process as claimed in claim 1 , in which the discrete particles are in the form of cylinders, aggregates of cylinders, or are of a spherical form, where the average diameter in the case of cylinders refers to a cylinder's base and in the case of aggregates of cylinders refers to a theoretical circle's diameter encircling the base of an aggregate of cylinders, where the length of a cylinder is greater than its diameter.
14 . The process as claimed in claim 1 , in which step (III) is conducted adiabatically at a temperature of 160° C. to 500° C.
15 . The process as claimed in claim 1 , in which step (III) is conducted adiabatically at a molar ratio of hydrogen to nitro groups of 10 to 200.
16 . The process as claimed in claim 1 , wherein the reacting is conducted in the gas phase and the optionally activated hydrogenation catalyst is disposed in a fixed catalyst bed.