EP1904228A1 - Katalysator und verfahren zur hydrierung von carbonylverbindungen - Google Patents

Katalysator und verfahren zur hydrierung von carbonylverbindungen

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Publication number
EP1904228A1
EP1904228A1 EP06777609A EP06777609A EP1904228A1 EP 1904228 A1 EP1904228 A1 EP 1904228A1 EP 06777609 A EP06777609 A EP 06777609A EP 06777609 A EP06777609 A EP 06777609A EP 1904228 A1 EP1904228 A1 EP 1904228A1
Authority
EP
European Patent Office
Prior art keywords
copper
oxidic material
range
catalyst
proportion
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP06777609A
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German (de)
English (en)
French (fr)
Inventor
Christophe Houssin
Henrik Junicke
Ulrich Müller
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
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Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP1904228A1 publication Critical patent/EP1904228A1/de
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
    • C07B41/00—Formation or introduction of functional groups containing oxygen
    • C07B41/02—Formation or introduction of functional groups containing oxygen of hydroxy or O-metal groups
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/889—Manganese, technetium or rhenium
    • B01J23/8892—Manganese
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/03—Precipitation; Co-precipitation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • B01J37/10—Heat treatment in the presence of water, e.g. steam
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
    • C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
    • C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/745—Iron
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/835—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with germanium, tin or lead
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten

Definitions

  • the present invention relates to a process for the hydrogenation of organic compounds which have at least one carbonyl group, using a catalyst which is characterized inter alia in that it consists of copper oxide, aluminum oxide and at least one of the oxides of iron, lanthanum, tungsten, molybdenum, Titanium, zirconium, tin or manganese in addition, and that the treatment with boiling water and / or steam produces a catalyst with high selectivity and high stability.
  • copper powder, copper flakes or cement may be added during its production.
  • catalytic hydrogenation of carbonyl compounds e.g. Carboxylic esters is almost always carried out in fixed bed reactors in industrial processes.
  • fixed-bed catalysts in addition to catalysts of the Raney type, especially supported catalysts, for example copper, nickel or noble metal catalysts are used.
  • US Pat. No. 3,923,694 describes a copper oxide / zinc oxide / alumina type catalyst.
  • the disadvantage of this catalyst is that it is not sufficiently stable mechanically during the reaction and therefore decomposes relatively quickly. This results in a loss of activity and a build-up of differential pressure across the reactor through the disintegrating catalyst moldings. As a result, the system must be shut down prematurely.
  • DE 198 09 418.3 describes a process for the catalytic hydrogenation of a carbonyl compound in the presence of a catalyst which contains a support which contains primarily titanium dioxide and as active component copper or a mixture of copper with at least one of the metals selected from the group consisting of zinc, Aluminum, cerium, a precious metal and a metal of VIII. Subgroup, wherein the copper surface is not more than 10 m 2 / g.
  • Preferred support materials are mixtures of titanium dioxide with aluminum oxide or zirconium oxide or aluminum oxide and zirconium oxide.
  • the catalyst material is deformed with the addition of metallic copper powder or copper flakes.
  • DE-A 195 05 347 describes in general a method of catalyst tablets with high mechanical strength, wherein the tablettirrenden to material a metal powder or a powder of a metal alloy is added.
  • aluminum powder or copper powder or copper flakes are added as metal powder.
  • the addition of aluminum powder in a copper oxide / zinc oxide / alumina catalyst, there is obtained a molded article having a lower side crushing strength than a molded article prepared without adding aluminum powder, and the molded article of the present invention showed inferior conversion activity when used as a catalyst as catalysts prepared without the addition of aluminum powder.
  • a hydrogenation catalyst of NiO, ZrO 2 , MoO 3 and CuO to which Cu powder was mixed in the course of production.
  • DE 256 515 describes a process for the preparation of alcohols from synthesis gas, using catalysts based on Cu / Al / Zn, which are obtained by co-grinding and blending with metallic copper powder or copper flakes.
  • the main focus is on the preparation of mixtures of C 1 to C 2 alcohols, wherein a procedure is chosen in which the reaction reactor in the upper third of the layer contains a catalyst which has a higher proportion of copper powder or copper flakes, and contains a catalyst in the lower third, which has a lower proportion of copper powder or copper flakes.
  • JP-A 50-99987 describes increasing the mechanical stability of special Raney catalysts, which may be copper based, by water or steam treatment.
  • SU-A 728 908 discloses the curing of alumino-copper-zinc catalysts for methanol synthesis by water treatment. The selectivity or activity is not reported in either literature.
  • An object of the present invention was to provide a process and a catalyst which do not have the disadvantages of the prior art and to provide processes for the catalytic hydrogenation of carbonyl compounds and catalysts, which catalysts have both high mechanical stability and high hydrogenation activity and selectivity.
  • the present invention relates to a process for the hydrogenation of an organic compound having at least one carbonyl group, in which the organic compound is brought into contact in the presence of hydrogen with a shaped article which can be prepared according to a process in which
  • powdery metallic copper, copper flakes, powdered cement or graphite or a mixture thereof can be added to the oxidic material
  • the shaped body is treated with boiling water and / or steam.
  • iron oxide is meant Fe (III) oxide.
  • the shaped bodies according to the invention are used as full, impregnating, shelling and precipitation catalysts.
  • the catalyst used in the process according to the invention is characterized in that the active component copper, the component aluminum and the component of at least one of the oxides of iron, lanthanum, tungsten, molybdenum, titanium, zirconium, tin or manganese preferably simultaneously or sequentially with a soda solution be precipitated, then dried, calcined, tableted and calcined again.
  • Solution containing copper salt and at least one salt of iron on a prefabricated alumina carrier This is in a particularly preferred embodiment as a powder in an aqueous suspension.
  • the carrier material can also be present as spheres, strands, chippings or tablets.
  • Support material used alumina.
  • Precipitated precipitates resulting from A) or B) are filtered in a conventional manner and preferably washed alkali-free, as described for example in DE 198 09 418.3.
  • Both the end products of A) and those of B) are dried at temperatures of 50 to 150 ° C, preferably at 120 0 C and then optionally preferably 2 hours at generally 200 to 600 0 C, in particular from 300 to 500 Calcined ° C.
  • starting materials for A) and / or B) can in principle all soluble in the solvents used in the application of Cu (I) and / or Cu (II) salts, such as nitrates, carbonates, acetates, oxalates or ammonium complexes, analog Aluminum salts and salts of iron are used. Particularly preferred for processes according to A) and B) copper nitrate is used.
  • the above-described dried and optionally calcined powder is preferably processed into tablets, rings, ring tablets, extrudates, honeycomb bodies or similar shaped bodies.
  • all suitable from the prior art methods are conceivable.
  • Particular preference is given to using a shaped catalyst body or a catalyst extrudate having a diameter d and a height h ⁇ 5 mm, catalyst spheres having a diameter d ⁇ 6 mm or catalyst honeycomb bodies having a cell diameter r z ⁇ 5 mm.
  • the composition of the oxide material is generally such that the proportion of copper oxide in the range of 40 to 90 wt .-%, the proportion of oxides of iron, lanthanum, tungsten, molybdenum, titanium, zirconium, tin or manganese in the range of 0 to 50 wt .-% and the proportion of aluminum oxide in the range up to 50 wt .-%, each based on the total weight of the sum of the above-mentioned oxidic constituents, wherein these three oxides together at least 80 wt .-% of the oxidic After calcination, cement is not attributed to the oxidic material in the above sense.
  • the present invention therefore relates to a method as described above, which is characterized in that the oxidic material
  • the process according to the invention and the catalysts according to the invention are distinguished by the fact that the treatment of the shaped body with boiling water and / or steam achieves a high stability of the shaped body used as a catalyst and at the same time increases the hydrogenation activity and selectivity of the catalyst.
  • the molded article dried and cal- cined as described above is covered with a Cr to C 4 alcohol such as methanol, ethanol or butanol in a sufficient amount of water or an aqueous-alkolic solution to completely cover the catalyst.
  • the aqueous-alcoholic solutions have a maximum alcohol concentration of 30 wt .-%.
  • the pH is adjusted to 4 to 9, preferably to 6 to 8.5, with the aid of mineral acids such as nitric acid, sulfuric acid or hydrochloric acid or sodium carbonate or sodium hydroxide solution.
  • the catalysts are at 100 to 14O 0 C and a pressure from 1 to 30 bar, preferably at 1 to 3 bar, from 1 to 48 h, preferably 5 to 20 h, treated with water or the aqueous-alkolic solution.
  • the steaming may be carried out with 100% steam with vapor mixtures of water vapor and inert gases, such as nitrogen, with an inert gas content of up to 90% by weight, and / or with vapors of compounds under the reaction conditions
  • the steam treatment water is formed, such as the Cr to C 4 alcohols such as methanol, ethanol or butanol, with an alcohol content of at most 90 wt.%, Are performed.
  • the steam treatment is carried out with pure steam.
  • the treatment of the catalyst body with steam is carried out at 100 to 300 0 C, preferably at 100 to 15O 0 C generally at atmospheric pressure, but also an elevated pressure of 1 to 20 bar, preferably 1 to 2 bar possible.
  • the steam treatment is usually carried out for at least 1 h, with 10 to 48 h of treatment being preferred.
  • the catalyst form body is again dried at temperatures of 120 0 C, preferably 2 h at generally 5 to 300 0 C, and optionally calcined.
  • the oxidic material is powdered copper, copper flakes or powdered cement or graphite or a mixture thereof in the range of 1 to 40 wt .-%, preferably in the range of 2 to 20 wt .-% and particularly preferably in the range of 3 to 10 Wt .-%, each based on the total weight of the oxidic material containing.
  • the cement used is preferably an alumina cement. More preferably, the alumina cement consists essentially of alumina and calcia, and more preferably consists of about 75 to 85 weight percent alumina and about 15 to 25 weight percent calcium oxide. Further, a cement based on magnesia / alumina, calcia / silica and calcia / alumina / iron oxide may be used.
  • the oxidic material in a proportion of at most 10 wt .-%, preferably at most 5 wt .-%, based on the total weight of the oxidic material, have at least one further component which is selected from the group consisting of the elements Re, Fe, Ru, Co, Rh, Ir, Ni, Pd and Pt.
  • the oxidic material before it is shaped into a shaped article, is added in addition to the copper oxide.
  • ferro powder, the copper flakes or the cement powder or the mixture thereof graphite added.
  • so much graphite is added that the deformation can be better performed to form a molded body.
  • the present invention also relates to a process as described above, characterized in that the oxidic material or the mixture resulting from (ii) contains graphite in a proportion in the range from 0.5 to 5% by weight, based on the total weight of the oxidic material is added.
  • the present invention also relates to a shaped body, treated with boiling water and / or steam and comprising
  • the shaped body obtained after the deformation is optionally calcined at least once over a period of generally 0.5 to 10 h, preferably 0, 5 to 2 hours.
  • the temperature in this at least one calcination step is common general in the range of 200 to 600 0 C, preferably in the range of 250 to 500 0 C and more preferably in the range 270-400 0 C.
  • the shaped body before being charged with the hydrogenation with reducing gases for example hydrogen, preferably hydrogen inert gas mixtures, in particular hydrogen / nitrogen mixtures at temperatures in the range of 100 to 500 ° C, preferably in the range of 150 Pre-reduced to 350 ° C and in particular in the range of 180 to 200 0 C.
  • reducing gases for example hydrogen, preferably hydrogen inert gas mixtures, in particular hydrogen / nitrogen mixtures at temperatures in the range of 100 to 500 ° C, preferably in the range of 150 Pre-reduced to 350 ° C and in particular in the range of 180 to 200 0 C.
  • the shaped body according to the invention is activated prior to use as a catalyst in a manner known per se by treatment with reducing media.
  • the activation takes place either in advance in a reduction furnace or after installation in the reactor. If the reactor has been activated in advance in the reduction furnace, it is installed in the reactor and charged directly under hydrogen pressure with the hydrogenation solution.
  • the preferred field of use of the shaped bodies produced by the process according to the invention is the hydrogenation of carbonyl-containing organic compounds in a fixed bed.
  • the hydrogenation can be carried out in the gas phase or in the liquid phase.
  • the hydrogenation is carried out in the liquid phase, for example in trickle or sump mode.
  • trickle mode the liquid starting material containing the carbonyl compound to be hydrogenated is allowed to trickle over the catalyst bed arranged in the reactor, which is under hydrogen pressure, whereby a thin liquid film is formed on the catalyst.
  • hydrogen gas is introduced into the reactor flooded with the liquid reaction mixture, the hydrogen passing through the catalyst bed in ascending gas beads.
  • the solution to be hydrogenated is pumped in a straight pass over the catalyst bed.
  • a portion of the product is withdrawn continuously after passing through the reactor as a product stream and optionally passed through a second reactor, as defined above.
  • the other part of the product is recycled to the reactor together with fresh reactant containing the carbonyl compound. This procedure is referred to in the following as Kreislauffahrweise.
  • the circulation mode of operation is preferred. It is further preferred to work in a circulation mode using a main reactor and a secondary reactor.
  • the process according to the invention is suitable for the hydrogenation of carbonyl compounds, such as e.g. Aldehydes and ketones, carboxylic acids, carboxylic acid esters or carboxylic anhydrides to the corresponding alcohols, wherein aliphatic and cycloaliphatic saturated and unsaturated carbonyl compounds are preferred.
  • carbonyl compounds such as e.g. Aldehydes and ketones, carboxylic acids, carboxylic acid esters or carboxylic anhydrides to the corresponding alcohols, wherein aliphatic and cycloaliphatic saturated and unsaturated carbonyl compounds are preferred.
  • aromatic carbonyl compounds unwanted by-products may be formed by hydrogenation of the aromatic nucleus.
  • the carbonyl compounds may carry other functional groups such as hydroxy or amino groups. Unsaturated carbonyl compounds are usually hydrogenated to the corresponding saturated alcohols.
  • the process according to the invention is preferably used for the hydrogenation of aliphatic aldehydes, hydroxyaldehydes, ketones, acids, esters, anhydrides, lactones and sugars.
  • Preferred aliphatic aldehydes are branched and unbranched saturated and / or unsaturated aliphatic C 2 -C 3 -o-aldehydes, as obtained, for example, by oxo Synthesis of linear or branched olefins with internal or terminal double bond are available. Furthermore, it is also possible to hydrogenate oligomeric compounds which also contain more than 30 carbonyl groups.
  • long-chain aliphatic aldehydes are particularly suitable, as can be obtained, for example, by oxo-synthesis from linear ⁇ -olefins.
  • enolization products e.g. 2-ethylhexenal, 2-methylpentenal, 2,4-diethyloctenal or 2,4-dimethylheptenal.
  • Preferred hydroxyaldehydes are C 3 -C 2 -hydroxy aldehydes, as are obtainable, for example, by aldol reaction from aliphatic and cycloaliphatic aldehydes and ketones with themselves or formaldehyde.
  • Examples are 3-hydroxypropanal, dimethylolethanal, trimethylolethanal (pentaerythritol), 3-hydroxybutanal (acetaldol), 3-hydroxy-2-ethylhexanal (butylaldol), 3-hydroxy-2-methylpentanal (propienaldol), 2-methylolpropanal, 2,2- Dimethylolpropanal, 3-hydroxy-2-methylbutanal, 3-hydroxypentanal, 2-methylolbutanal, 2,2-dimethylolbutanal, hydroxypivalaldehyde.
  • Particularly preferred are hydroxypivalaldehyde (HPA) and dimethylolbutanal (DMB).
  • ketones are acetone, butanone, 2-pentanone, 3-pentanone, 2-hexanone, 3-hexanone, cyclohexanone, isophorone, methyl isobutyl ketone, mesityl oxide, acetophenone, propiophenone, benzophenone, benzalacetone, dibenzalacetone, benzalacetophenone, 2,3-butanedione, 2 , 4-pentanedione, 2,5-hexanedione and methyl vinyl ketone.
  • carboxylic acids and derivatives thereof preferably those having 1-20 C atoms can be reacted.
  • carboxylic acids and derivatives thereof preferably those having 1-20 C atoms can be reacted.
  • the following are to be mentioned:
  • Carboxylic acids such as formic acid, acetic acid, propionic acid, butyric acid, isobutyric acid, n-valeric acid, trimethylacetic acid ("pivalic acid”), caproic acid, enanthic acid, caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, acrylic acid, methacrylic acid, oleic acid , Elaidic acid, linoleic acid, linolenic acid, Cyclohexanecarboxylic acid, benzoic acid, phenylacetic acid, o-toluic acid, m-toluic acid, p-toluic acid, o-chlorobenzoic acid, p-chlorobenzoic acid, o-nitrobenzoic acid, p-nitrobenzoic acid, salicylic acid, p-hydroxybenzoic acid, anthranilic acid, p-aminobenzoic acid, Oxa
  • Carboxylic esters e.g. the C 1 -C 10 -alkyl esters of the abovementioned carboxylic acids, in particular methyl formate, ethyl acetate, butyric acid butyl ester, phthalic acid, isophthalic acid, terephthalic acid, adipic acid, maleic acid dialkyl esters, such as e.g. the dimethyl esters of these acids, (meth) acrylic acid methyl ester, butyrolactone, caproiactone and polycarboxylic acid esters, e.g. Polyacrylic and polymethacrylic acid esters and their copolymers and polyesters, e.g. Polymethylmethacrylat, terephthalic acid esters and other engineering plastics, in particular hydrogenolyses, ie the implementation of esters to the corresponding acids and alcohols are carried out;
  • Carboxylic acid anhydrides e.g. the anhydrides of the above carboxylic acids, especially acetic anhydride, propionic anhydride, benzoic anhydride and maleic anhydride;
  • Carboxylic acid amides e.g. Formamide, acetamide, propionamide, stearamide, terephthalic acid amide.
  • hydroxycarboxylic acids e.g. Lactic, malic, tartaric or citric acid
  • amino acids e.g. Glycine, alanine, proline and arginine, and peptides are reacted.
  • Particularly preferred organic compounds are hydrogenated saturated or unsaturated carboxylic acids, carboxylic acid esters, carboxylic anhydrides or lactones or mixtures of two or more thereof.
  • the present invention also relates to a process as described above, which is characterized in that the organic compound is a carboxylic acid, a carboxylic acid ester, a carboxylic acid anhydride or a lactone.
  • Examples of these compounds include maleic acid, maleic anhydride, succinic acid, succinic anhydride, adipic acid, 6-hydroxycaproic acid, 2-cyclo- dodecylpropionic acid, the esters of the abovementioned acids, for example methyl, ethyl, propyl or butyl esters. Further examples are ⁇ -butyrolactone and caprolactone.
  • the present invention relates to a method as described above which is characterized in that the organic compound is adipic acid or an adipic acid ester.
  • the carbonyl compound to be hydrogenated may be supplied to the hydrogenation reactor alone or as a mixture with the product of the hydrogenation reaction, which may be done neat or using additional solvent.
  • additional solvent In particular, water, alcohols such as methanol, ethanol and the alcohol which is formed under the reaction conditions are suitable as additional solvents.
  • Preferred solvents are water, THF and NMP, more preferably water.
  • the hydrogenation in both the bottoms and in trickle in each case preferably operated in circulation mode, is generally carried out at a temperature in the range of 50 to 350 0 C, preferably in the range of 70 to 300 ° C, more preferably in the range of 100 to 270 0 C and a pressure in the range of 3 to 350 bar, preferably in the range of 5 to 330 bar, more preferably in the range of 10 to 300 bar by.
  • the catalysts of the invention are used in processes for the preparation of hexanediol and / or caprolactone, as described in DE 196 07 954, DE 196 07 955, DE 196 47 348 and DE 196 47 349.
  • the catalysts according to the invention have a high chemical and mechanical stability.
  • the present invention relates to the use of a treatment with boiling water and / or steam in the preparation of a catalyst for increasing both the mechanical stability and the activity and the selectivity of the catalyst.
  • the present invention relates to a use as described above, which is characterized in that the catalyst comprises copper as the active component.
  • the mechanical stability of solid catalysts and especially of the catalysts according to the invention is described by the parameter lateral pressure resistance in various states (oxidic, reduced, reduced and suspended underwater).
  • the lateral compressive strength in the context of the present application was determined using a Z 2.5 / T 919 device from Zwick Roll (Ulm) Both in the case of the reduced and the used catalysts, the measurements were carried out in methanol under a nitrogen atmosphere, to avoid re-oxidation of the catalysts.
  • Solution 1 A mixture of 12.41 kg of a 57% copper nitrate solution, and 12.78 kg of a 33% Alurniniumnitratains and 0.48 kg of a 40% lanthanum nitrate solution x 6H2O were dissolved in 2 l of water (solution 1).
  • Solution 2 includes 60 kg one
  • Solution 1 and Solution 2 were passed through separate lines into a precipitation vessel provided with a stirrer and containing 10 L heated to 8O 0 C water. By adjusting the feed rates of solution 1 and solution 2, the pH was brought to 6.2.
  • the filter cake was dried for 16 h at 12O 0 C and then calcined at 600 0 C for 2 h.
  • the catalyst powder thus obtained is precompacted with 1% by weight of graphite.
  • the compact obtained is mixed with 5% by weight of Cu-sheet Unicoat and then with 2% by weight of graphite and pressed into tablets of 3 mm in diameter and 3 mm in height.
  • the tablets were finally calcined for 2 hours at 35O 0 C.
  • the catalyst thus prepared has the chemical composition
  • the side crushing strength was 25 N as shown in Table 1.
  • T4489 catalyst composition of 60% CuO / 30% Al 2 O 3/10 MnO 2 sold by the company. Südchemie.
  • the commercial catalyst of composition 60% CuO / 30% AbO 3/10 MnO 2 (trade name T4489 Fa. Südchemie) 20 was treated hours at a pressure of 1, 3 bar with 100% water vapor and then at 12O 0 C for 4 h long dried.
  • the test duration was a total of 7 days.
  • Table 1 The test results are summarized in Table 1.

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  • Chemical Kinetics & Catalysis (AREA)
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  • Thermal Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
EP06777609A 2005-07-13 2006-07-06 Katalysator und verfahren zur hydrierung von carbonylverbindungen Withdrawn EP1904228A1 (de)

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DE200510032726 DE102005032726A1 (de) 2005-07-13 2005-07-13 Katalysator und Verfahren zur Hydrierung von Carbonylverbindungen
PCT/EP2006/063958 WO2007006719A1 (de) 2005-07-13 2006-07-06 Katalysator und verfahren zur hydrierung von carbonylverbindungen

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JP5693561B2 (ja) * 2009-04-08 2015-04-01 ビーエーエスエフ ソシエタス・ヨーロピアＢａｓｆ Ｓｅ １，６−ヘキサンジオールをオリゴ−およびポリエステルの水素化によって製造する方法
TWI490034B (zh) * 2009-11-17 2015-07-01 Basf Se 製備具有增強氫化活性之經承載氫化觸媒之方法
WO2012032002A2 (de) 2010-09-08 2012-03-15 Basf Se VERFAHREN ZUR HERSTELLUNG VON ε-CAPROLACTON UND 1,6-HEXANDIOL
DE102012012510B4 (de) 2012-06-22 2018-12-06 Clariant International Ltd. Graphithaltiger Katalysatorformkörper, dessen Herstellverfahren sowie Verwendung
TW201536734A (zh) 2014-03-12 2015-10-01 Basf Se 甲酸鹽的分解
WO2017017074A1 (de) * 2015-07-29 2017-02-02 Basf Se Verfahren zur herstellung von monoethylenglykol
CN107285997B (zh) 2016-03-30 2022-04-22 长春美禾科技发展有限公司 一种改善乙二醇紫外透过率的方法
CN107930638B (zh) * 2016-10-13 2020-02-18 中国石油化工股份有限公司 丙酮一步法合成甲基异丁基酮的铜基催化剂
CN107930635B (zh) * 2016-10-13 2020-02-18 中国石油化工股份有限公司 联产甲基异丁基酮和二异丁基酮的催化剂
DE102016225172A1 (de) * 2016-12-15 2018-06-21 Clariant International Ltd Tablettierter Katalysator mit erhöhter Stabilität gegenüber Säureeinwirkung
JP7472133B2 (ja) 2018-12-03 2024-04-22 ビーエーエスエフ ソシエタス・ヨーロピア 銅を含む触媒組成物の存在下で１－（４－イソブチルフェニル）エタノンの水素化により１－（４－イソブチルフェニル）エタノールを製造する方法
EP4069418A1 (de) 2019-12-03 2022-10-12 Basf Se Verfahren zur herstellung von aminen an einem kupferhaltigen katalysator
CN115445629B (zh) * 2022-08-23 2024-02-27 万华化学集团股份有限公司 一种苯乙酮加氢制α-苯乙醇的催化剂及其制备方法与应用

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CA2614520A1 (en) 2007-01-18
CN101309749A (zh) 2008-11-19
KR20080039411A (ko) 2008-05-07
DE102005032726A1 (de) 2007-01-18
WO2007006719A1 (de) 2007-01-18

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