Synthetic resins or natural rubbers -- part of the class 520 ser – Redox catalyst
Reexamination Certificate
2002-11-06
2004-11-16
Davis, Brian (Department: 1621)
Synthetic resins or natural rubbers -- part of the class 520 ser
Redox catalyst
C564S421000, C564S422000, C564S423000
Reexamination Certificate
active
06818720
ABSTRACT:
The invention relates to a supported hydrogenating catalyst in powder form, a process for its production and its use in the catalytic hydrogenation of nitroaromatics.
The hydrogenation of aromatic nitro-compounds to amines is one of the major ways of producing amines in industrial chemistry. Today, aromatic amines are central components in the prodution of fine, speciality and even bulk chemicals. Examples in the field of bulk chemicals, in particular, are aniline and toluenediamines (TDA). The catalytic hydrogenation of nitrobenzene to aniline replaced the old Bechamps reduction method, making an important contribution to sustained development. TDA can be regarded as an intermediate for the production of polyurethane foams, being converted in a phosgenation reaction to toluene diisocyanate (TDI), which is processed together with polyalcohols to produce polyurethane foams.
Various processes and catalysts are known for the production of aromatic amines by hydrogenation of the corresponding aromatic nitro-compounds. In addition to the hydrogenation of nitrobenzene to aniline in the gas phase, there are a number of other processes, all of which work in the liquid phase. In addition to supported non-precious metal catalysts and Raney-type catalysts, supported catalysts containing precious metals are also used.
A number of catalysts are known for the catalytic hydrogenation of nitroaromatics, in particular of dinitrotoluene, in the suspension phase.
U.S. Pat. No. 2,823,235 discloses palladium, platinum and palladium-platinum catalysts on black, which are doped with iron.
Very similar catalysts, which contain blacks as supports, are disclosed in U.S. Pat. No. 3,127,356.
U.S. Pat. No. 4,256,671 discloses, in addition to Pd and Pt, also Ni, Ru and Rh as a precious metal component for catalysts used in the catalytic hydrogenation of dinitrotoluenes to toluenediamines.
U.S. Pat. No. 6,096,924 discloses, as a catalytically active component, Rh, Ru, Ir, Pt, Pd, Ni and Co. These metals are applied to powder-form supports. V is used as a doping metal.
DE 199 11 865 A1 discloses a similar system with Ir as the precious metal and V as the doping metal.
Whilst the stated printed publications disclose Pd-, Ir- or Pd—Pt-catalysts, U.S. Pat. No. 4,212,824 discloses a Pt-catalyst on black, which is doped with Fe. Fe and V are the non-precious metals used by far the most frequently for doping.
It is also known that the addition of a few mol-percent of platinum (for example 15 mol %) to supported palladium catalysts produces a positive synergetic effect on activity. This is disclosed in
Pol. Chem. Stosow
. 1981, 25(1), 53-68 or in
Chin. Chem. Lett
. 1996, 7(7), 663-664.
The former printed publication shows that platinum may be present only in a smaller molar quantity than palladium. The optimum is ca. 20 mol % Pt in relation to Pd. If a larger quantity of Pt is used, lower activity is determined.
The object of the present invention is to improve the selectivity and activity of the catalytic hydrogenation of nitroaromatics to aminoaromatics, i.e. to reduce the formation of by-products and to increase the yield of the desired product, through the selection and production of a hydrogenating catalyst.
The invention provides a supported hydrogenating catalyst in powder form, which contains, as catalytically active components, a mixture of a primary precious metal component, a secondary precious metal component and one or more non-precious metal components, wherein either Pt is used as the primary precious metal component with Pd, Ru, Rh as the secondary precious metal component and V, Fe, Mn, Ce and/or Cr as the non-precious metal component, or Pd is used as the primary precious metal component with Ru, Rh as the secondary precious metal component and V, Fe, Mn, Ce and/or Cr as the non-precious metal component or Pd is used as the primary precious metal component with Pt as the secondary precious metal component and Ce and/or Cr as the non-precious metal component.
The hydrogenating catalyst according to the invention can contain, per 100 g dry hydrogenating catalyst, 10 to 50 mmol of the primary precious metal component. The proportion of the secondary precious metal component can be 1 to 60 mol % in relation to the primary precious metal component, preferably 8 to 12 mol % in relation to the primary precious metal component and that of the non-precious metal component 1-700 mol %, preferably 100-600 mol % in relation to the primary precious metal component.
The formation of by-products is influenced only slightly by the ratio of primary to secondary precious metal components which, however has a strong influence on the activity of the catalyst.
As doping metals for the combination Pt as primary precious metal component and Pd, Ru, Rh as secondary precious metal component, V, Fe, Mn, Ce and/or Cr are particularly suitable as the non-precious metal component.
As doping metals for the combination Pd as primary precious metal component and Ru, Rh as secondary precious metal component, V, Fe, Mn, Ce and/or Cr are particularly suitable as the non-precious metal component.
As a doping metal for the combination Pd as primary precious metal component and Pt as secondary precious metal component, Ce and/or Cr are particularly suitable as the non-precious metal component.
Whilst the secondary precious metal component is responsible for the high activity of the catalyst, the non-precious metal component is decisive for selectivity.
The hydrogenating catalyst according to the invention can contain, per 100 g dry hydrogenating catalyst, 15 to 20 mmol of the primary precious metal component, 8 to 12 mol %, in relation to the primary precious metal component, of the secondary precious metal component, and 1 to 600 mol %, in relation to the primary precious metal component, of cerium.
Supports in powder form are used as supports, and these powder supports may be physically activated carbons, chemically activated carbons, blacks, aluminium oxides or silicon oxides, preferably physically activated carbons, chemically activated carbons or blacks.
The invention further provides a process for the production of the hydrogenating catalyst according to the invention, which is characterised in that an aqueous solution containing the primary and secondary precious metal components and the non-precious metal component in dissolved form is added to a suspension of a powder-form support material in water, the primary and secondary precious metal components and the non-precious metal component are deposited on the powder-form support using a base and reduction is optionally carried out using a reducing agent such as for example formaldehyde, hydrazine, hydrogen, sodium tetrahydroborate, formic acid or sodium formate.
Reduction can be carried out at a temperature of 0 to 100° C.
The order in which the support material, water, metal salt solutions and reducing agents are added can also be varied. Optionally, reduction can take place with hydrogen on the dried catalyst. The use of a reducing agent is optional, i.e. the catalyst according to the invention can be separated out from the reaction mixture by filtration, without the addition of a reducing agent, after the primary and secondary precious metal and non-precious metal components have been deposited on the support.
The catalyst according to the invention can be used for the hydrogenation of nitroaromatics. The catalyst according to the invention can be used in particular for the hydrogenation of nitrobenzene to aniline and for the hydrogenation of dinitrotoluenes to toluenediamines.
The catalytic hydrogenation of the nitro-compound can be carried out in the liquid phase as a continuously or discontinuously operated process at pressures of 1 to 100 bar and temperatures of 0 to 250° C. in the presence of the catalyst according to the invention.
The catalytic hydrogenation of the nitro-compound in the liquid phase can be carried out as a continuously or discontinuously operated process at pressures of 1 to 100 bar and temperatures of 0° C. to 200° C. in the presence of the cataly
Göttlinger Markus
Gross Michael
Krauter Jürgen
Packruhn Uwe
Davis Brian
Degussa - AG
Venable LLP
Wiseman Thomas G.
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