EP1912737A1 - Catalyseur plein, fabrication et utilisation dans un procede d'oxydation d'ammonium - Google Patents

Catalyseur plein, fabrication et utilisation dans un procede d'oxydation d'ammonium

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Publication number
EP1912737A1
EP1912737A1 EP06777717A EP06777717A EP1912737A1 EP 1912737 A1 EP1912737 A1 EP 1912737A1 EP 06777717 A EP06777717 A EP 06777717A EP 06777717 A EP06777717 A EP 06777717A EP 1912737 A1 EP1912737 A1 EP 1912737A1
Authority
EP
European Patent Office
Prior art keywords
range
catalyst
diameter
compound
ammoxidation
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Withdrawn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
EP06777717A
Other languages
German (de)
English (en)
Inventor
Sabine Huber
Randolf Hugo
Kirsten Dahmen
Thomas Preiss
Hartmut Hibst
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP1912737A1 publication Critical patent/EP1912737A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C253/00—Preparation of carboxylic acid nitriles
    • C07C253/24—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons
    • C07C253/28—Preparation of carboxylic acid nitriles by ammoxidation of hydrocarbons or substituted hydrocarbons containing six-membered aromatic rings, e.g. styrene
    • 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
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • 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
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/28—Molybdenum
    • 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
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/30—Tungsten
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • 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
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • 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
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/20—Carbon compounds
    • B01J27/22—Carbides
    • B01J27/224—Silicon carbide
    • B01J27/228—Silicon carbide with phosphorus, arsenic, antimony or bismuth
    • 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
    • B01J37/0027—Powdering
    • B01J37/0045—Drying a slurry, e.g. spray drying
    • 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
    • B01J37/0201—Impregnation
    • 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
    • B01J37/04—Mixing

Definitions

  • the present invention relates
  • a support material selected from alumina, silica, aluminum silicate, magnesium silicate, titanium dioxide, zirconia, thorium dioxide, silicon carbide or mixtures thereof, and b) vanadium (V) and antimony (Sb) and at least one element selected from molybdenum (Mo ) and / or tungsten (W), each in oxidic form, as active components,
  • the ammoxidation of Ci-4-alkyl iso and heteroaromatics, such as toluene, the xylenes or the picolines, represents a technically conventional method for the synthesis of the corresponding aromatic nitriles.
  • the reaction is usually carried out in the gas phase with the concomitant use of supported catalysts, in addition Vanadium other elements such as antimony, chromium, molybdenum or phosphorus in oxidic form.
  • the carriers used are mainly inert metal oxides, such as aluminum oxide, silicon dioxide, titanium oxide or zirconium dioxide, and mixtures of these oxides.
  • the highly exothermic ammoxidation is technically usually carried out in fluidized bed reactors.
  • EP-A2-699 476 (BASF AG) relates to supported catalysts suitable for ammoxidation from a) a spherical or approximately spherical support material consisting essentially of alumina, silica, titania and / or zirconia and whose bulk density is 0.6 to 1.2 kg / l, and b) an active material which contains as essential components vanadium and antimony in oxidic form.
  • a spherical or approximately spherical support material consisting essentially of alumina, silica, titania and / or zirconia and whose bulk density is 0.6 to 1.2 kg / l
  • an active material which contains as essential components vanadium and antimony in oxidic form.
  • EP-A1-767 165 (BASF AG) describes a process for the preparation of aromatic or heteroaromatic nitriles using a supported catalyst containing vanadium and wherein the supported catalyst consists of two to thirty grain fractions of certain median diameter with a specific bulk density. These catalysts are also suitable in particular for a fluidized bed process and, according to example catalyst A, have a diameter of about 0.15 mm (due to the selected aluminum oxide Puralox®).
  • EP-A2-930 295 (Mitsubishi Gas) teaches an ammoxidation process for the preparation of aromatic nitriles on certain V-, Cr- and B-containing catalysts in the fluidized bed.
  • a disadvantage of the fluidized bed process is due to the catalyst discharge (fine catalyst dust due to catalyst abrasion) from the vortex zone of the reactor, therefore the need for a cyclone and problems with optionally occurring catalyst dusts in the product.
  • JP-A-2003 267942 (Mitsubishi Gas) relates to an ammoxidation process using certain chromium-, vanadium-, molybdenum- and iron-containing catalysts with alumina or titania as support material which can be used as a fixed bed.
  • a problem with the fixed-bed ammoxidation process is the difficulty of carrying out and controlling the hot spot formation in the fixed catalyst bed associated with the highly exothermic reaction. Therefore, u.a. the educt concentration in the feed are kept low.
  • the process should be flexible in terms of adjusting the activity of the catalyst, allowing for lower reactor temperatures and high reactant concentrations in the reactor feed, and providing the process products in high yields, space-time yields and selectivities.
  • the catalyst used should have a high stability (measured, for example, as lateral compressive strength in Newtons (N)), service life and tolerance to water. [Space-time yields are reported in amount of product / (catalyst volume • time) "(kg / (I cat. • h)) and / or product / (reactor volume • time)" (kg / (l Re actuator • H)].
  • a support material selected from alumina, silica, aluminum silicate, magnesium silicate, titanium dioxide, zirconia, thorium dioxide, silicon carbide or mixtures thereof, and b) vanadium (V) and antimony (Sb) and at least one element selected from molybdenum (Mo ) and / or tungsten (W), each in oxidic form, as active components, found,
  • the support material is spherical or approximately spherical, with a diameter in the range of 2 to 10 mm, or tubular or strand-shaped, with an (outer) diameter in the range of 1 to 10 mm and a length in the range of 2 to 20 mm, or split-shaped, with a maximum diameter in the range of 2 to 20 mm.
  • a process has been found for producing such a full catalyst, which is characterized in that the spherical or approximately spherical, tubular, strand-like or particle-shaped carrier material with a solution or suspension of a vanadium compound and an antimony compound and a molybdenum and / or tungsten compound and optionally an alkali metal compound impregnated, from the resulting mixture excess liquid separated, dried and calcined under oxidizing conditions.
  • An advantage of the catalyst according to the invention is the high activity and mechanical stability.
  • the spherical or approximately spherical support material has a diameter in the range of 2.5 to 8 mm, in particular 3 to 7 mm, very particularly 3.5 to 6 mm, e.g. 4 to 5 mm, on.
  • tubular (also hollow cylindrical) carrier material this preferably has an inner diameter in the range of 1 to 7 mm, an external diameter. knife in the range of 2 to 8 mm and a tube length in the range of 2 to 8 mm, in particular an inner diameter in the range of 2 to 6 mm, an outer diameter in the range of 3 to 7 mm and a tube length in the range of 3 to 7 mm , more particularly an inner diameter in the range of 3 to 5 mm, an outer diameter in the range of 4 to 6 mm and a tube length in the range of 4 to 6 mm.
  • this preferably has a diameter in the range of 2 to 5 mm and a length in the range of 5 to 10 mm.
  • this preferably has a maximum diameter in the range of 3 to 18 mm, especially in the range of 4 to 16 mm.
  • the spherical or approximately spherical carrier material as such is z. known and also commercially available (in the case of alumina, for example, types from the company Sasel Germany GmbH).
  • Suitable spherical or approximately spherical particles preferably have an average form factor of F> 85%.
  • the form factor is as
  • Ui is the circumference of a particle cross section Q and U2 is the circumference of a circle of equal cross-sectional area Q.
  • the condition of a minimum form factor is met if no cross-section of the particle corresponds to a smaller value, as can be determined statistically.
  • tubular carrier material as such is z. known and also commercially available (in the case of aluminum oxide, for example types under the trade name PURAL® and CATAPAL® aluminas from Sasol Germany GmbH).
  • the spherical or approximately spherical or tubular carrier material by subjecting the solution or suspension of an aluminum, silicon, titanium, thorium and / or zirconium compound to spray-drying.
  • spherical particles eg with a diameter in the range of 0.1 to 200 microns
  • spray drying of solutions of the corresponding compounds are, for example alcoholates such as ethanolates and isopropylates, carboxylates such as acetates, sulfates and nitrates and as suspended compounds hydroxides and oxide hydrates .
  • the desired particle size and bulk density can be adjusted in a manner known per se.
  • the resulting particles are converted into an oxygen-containing gas stream at a temperature in the range of, for example 500 to 1200 0 C in the oxides.
  • Spheres or tubes in the desired diameters and lengths are obtained subsequently or after the spray-drying by pressing (tableting) and subsequently calcined / annealed.
  • the particles obtained by spray-drying are first calcined, then subjected to compression and then calcined again.
  • the particles obtained by spray-drying are first pressed without prior calcination and then calcined.
  • the unsupported catalysts of the invention can be prepared by impregnation of the support material.
  • the (optionally calcined) support material is impregnated with a solution or suspension of compounds of the metals of the active composition.
  • the intimate mixing of the starting compounds takes place in wet form.
  • the starting compounds are mixed together in the form of an aqueous solution and / or suspension.
  • the solvent used is preferably water.
  • the mass thus obtained is dried in a manner known per se and dried under oxidizing conditions, e.g. in the air stream, calcined.
  • the temperatures are preferably 100 to 300 0 C and for the calcination at 400 to 750 0 C, in particular 450 to 600 ° C.
  • aqueous solutions or suspensions of the compounds of the active catalyst components it is preferable to use aqueous solutions or suspensions of the compounds of the active catalyst components, but in principle any liquids are suitable.
  • the impregnation solution or suspension is not used in a greater amount than is absorbed by the carrier material Otherwise, during drying, agglomerates are obtained which first have to be comminuted again, with the result that particles can form which do not have the desired spherical or tubular shape. You can make the impregnation after each intermediate drying in several steps.
  • the active components are preferably used in the form of aqueous solutions of their salts, in particular of salts of organic acids which decompose without residue in the oxidative calcination.
  • their salts in particular of salts of organic acids which decompose without residue in the oxidative calcination.
  • the oxalates especially in the case of vanadium
  • the tartrates and acetates especially in the case of antimony
  • the tartrates also being in the form of mixed salts, e.g. with ammonium ions, may be present.
  • the vanadium compounds used may also be a nitrate or a vanadate.
  • the antimony compound used may also be an antimonate.
  • Molybdenum and tungsten are each preferably used in the form of complex compounds with tartaric acid, oxalic acid or citric acid or in the form of a molybdate or tungstate.
  • Metallic W and / or Mo can be oxidized by H2O2 and transferred to the solution.
  • the shaping of the unsupported catalysts can take place before or after the thermal treatment has been carried out.
  • solid catalysts can be prepared from the powder form of the multielement oxide active composition according to the invention or its precursor material (the intimate dry mixture) which has not yet been thermally treated by compacting to the desired catalyst geometry (sphere, tube, strand, eg by tabletting, extrusion or extrusion), with optional diluents such as For example, S1O 2 , adjuvants such as graphite or stearic acid as lubricants and / or molding aids and reinforcing agents such as microfibers of glass, asbestos, silicon carbide or potassium titanate can be added.
  • diluents such as For example, S1O 2 , adjuvants such as graphite or stearic acid as lubricants and / or molding aids and reinforcing agents such as microfibers of glass, asbestos, silicon carbide or potassium titanate can be added.
  • the calcination atmosphere can be realized in a simple manner, for example, by calcining in an oven, through which a 0 2 -containing gas mixture, eg air, leads.
  • the calcination temperature is preferably in the range of 400 to 750 0 C.
  • the amount of vanadium, calculated as metal, in the catalyst is preferably 0.5 to 50 wt .-%, particularly 0.7 to 10 wt .-%, preferably 1, 0 to 7 wt .-%, more particularly 1.5 to 6 wt .-%, and calculated for the antimony, also as a metal, the amounts are preferably 0.5 to 50 wt .-%, particularly 1 to 20 wt .-%, preferably 2 to 10 wt .-%.
  • the catalysts in a preferred embodiment additionally contain preferably 0.01 to 5.0% by weight, in particular 0.1 to 3% by weight, e.g. 0.15 to 2 wt .-%, alkali metal, ie Li, Na, K, Rb and / or Cs, preferably cesium and / or rubidium, each calculated as metal.
  • alkali metal ie Li, Na, K, Rb and / or Cs, preferably cesium and / or rubidium, each calculated as metal.
  • the catalysts additionally contain preferably 0.05 to 12 wt .-%, in particular 0.1 to 3 wt .-%, preferably 0.01 to 2.5 wt .-%, Mo and / or W, each calculated as metal.
  • Preferred catalysts contain, based on the mass of the unsupported catalyst, from 1 to 50% by weight, in particular from 5 to 25% by weight, very particularly from 7 to 20% by weight, of the active components.
  • the catalyst may contain other active components, e.g. Compounds of titanium, iron, cobalt, nickel, manganese and / or copper.
  • the catalyst contains no iron (Fe), no chromium (Cr) and / or no boron (B), each in oxidic form.
  • a particularly preferred catalyst according to the invention is a full catalyst comprising
  • Alox as a spherical or approximately spherical support material having a diameter in the range of 2 to 10 mm, in particular 4 to 6 mm, and b) an active mass, the vanadium (V) and antimony (Sb) and tungsten (W) and cesium (Cs), each in oxidic form, and no chromium (Cr) and no iron
  • novel catalysts are suitable for the novel ammonium oxidation reactions in a fixed bed.
  • Preferred fixed bed reactors are tube reactors and tube bundle reactors, as described, for example, in Ulimann's Encyclopedia of Industriai Chemistry, 6th Ed., Keyword "fixed bed reactors".
  • the Feststoffkatalysator forung is located in the metal tubes of the tube bundle reactor and the metal tubes or the tempering are performed (in more than one temperature zone, a corresponding number of spatially separated tempering is performed around the metal tubes).
  • the tempering medium is preferably a molten salt. Through the contact tubes, the reaction mixture is passed.
  • the catalyst tubes are usually made of ferritic steel and typically have a wall thickness of 1 to 3 mm. Its inner diameter is preferably 12 to 30 mm, often 14 to 26 mm. Their length is appropriate 3 to 6 m.
  • the number of catalyst tubes accommodated in the tube bundle container is expediently at least 5,000. Often the number of catalyst tubes accommodated in the reactor container is 10,000 to 30,000. Tube bundle reactors having a number of contact tubes above 40,000 tend to be the exception.
  • the contact tubes are normally arranged homogeneously distributed (preferably 6 equidistant neighboring tubes per contact tube), wherein the distribution is expediently chosen so that the distance of the central inner axes of closest contact tubes (the so-called contact tube pitch) is 35 to 45 mm (cf., for example, EP-A-468 290).
  • Particularly suitable as a heat exchange medium is the use of melts of salts such as potassium nitrate, potassium nitrite, sodium nitrite and / or sodium nitrate, or of low-melting metals such as sodium, mercury and alloys of various metals.
  • salts such as potassium nitrate, potassium nitrite, sodium nitrite and / or sodium nitrate
  • low-melting metals such as sodium, mercury and alloys of various metals.
  • the full catalyst is diluted in the reactor with an inert material, whereby the activity of the catalyst can be adjusted specifically.
  • the inert material may be e.g. steatite spheres, steatite tubes, alumina spheres, alumina tubes, silica spheres and / or silica tubes.
  • the inert material is preferably identical to the carrier material of the unsupported catalyst used.
  • the inert material preferably has a similar or the same geometry (diameter, length) as the carrier material of the unsupported catalyst used.
  • the dilution of the catalyst with the inert material sets a dilution profile over the reactor length.
  • a dilution profile over the reactor length.
  • Zones eg, 2, 3 or 4 zones, for example, each resulting from the equal parting of
  • a zone with a higher dilution than at the reactor end is set at the reactor inlet.
  • two zones can be formed, wherein in the zone at the reactor inlet the catalyst with 10 to 90 wt .-%, preferably 20 to 50 wt .-%, inert material is diluted, and in the zone at the reactor end of the catalyst with 0 to 90 wt. -%, preferably 1 to 30 wt .-%, inert material is diluted.
  • the percentages by weight are in each case based on the total weight of used unsupported catalyst and inert material in the respective zone.
  • the height of the inert feed in the reactor tube is in the range of 5 to 100 cm, that of the backfill in the range of 0 to 100 cm.
  • the feed ensures the heating of the reaction gas in the pre-reaction space, the repatriation ensures that catalyst abrasion is retained and does not enter the following reaction stages.
  • the inert beds also prevent the catalyst from lifting and wandering if a surge occurs; Also cavities and dead volume is / are avoided.
  • OPDN o-phthalodinitrile
  • IPDN isophthalodinitrile
  • benzonitrile from toluene and from nicotinic acid nitrile from beta-metal
  • the ammoxidation of the first methyl group is faster than that of the second, so that also slightly partial ammoxidation products can be obtained, e.g. p-methylbenzonitrile from p-xylene.
  • the aromatic starting materials may carry substituents which are inert under the conditions of the ammoxidation, ie, for example, halogen or the trifluoromethyl-nitro, amino or cyano group.
  • Non-inert substituents may also be considered if they are converted into desired substituents under conditions of ammoxidation, for example the aminomethyl or the hydroxymethyl group.
  • the ammoxidation process of the invention is preferably performed at a temperature ranging from 300 to 550 C, in particular 350 to 500 0 C, particularly 380-490 0 C., for example to 480 ° C, carried out 420th
  • the organic starting compound to be oxidized is preferably taken up in a gas stream of ammonia and an oxygen-containing gas such as air, the concentration of the starting compound in the gas stream advantageously being 0.1 to 10% by volume, preferably 0.1 to 5% by volume. is set.
  • the oxygen content of the gas used for the ammoxidation is preferably in the range from 0.1 to 25% by volume, in particular in the range from 3 to 15% by volume.
  • the catalysts of the invention allow a load of the full catalyst in the range of 0.1 to 2 kg of the starting compound per kg of catalyst and per hour.
  • Unreacted ammonia is advantageously recycled to the reaction.
  • solution B was added to solution A with stirring.
  • the resulting mixture was heated to 9O 0 C and heated for 2 hours at this temperature. Subsequently, the solution C was added to the resulting mixture and heated for a further hour with stirring at 9O 0 C.
  • the resulting black powder had a BET surface area of 165 m 2 / g.
  • the obtained black powder showed the crystal structure of tetragonal
  • the catalyst split from Example 1 was diluted with 90% by weight of 2-3 mm steatite balls.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un catalyseur plein contenant a) un matériau support choisi parmi dioxyde d'aluminium, dioxyde de silicium, silicate d'aluminium, silicate de magnésium, dioxyde de titane, dioxyde de zircon, dioxyde de thorium, carbure de silicium ou des mélanges de ceux-ci, et b) du vanadium (V), de l'antimoine (Sb) et au moins un élément choisi parmi molybdène (Mo) et/ou tungstène (W), respectivement sous forme oxydique, en tant que composants actifs. Le matériau support est sphérique ou approximativement sphérique avec un diamètre de 2 à 10 mm, ou tubulaire ou en forme de barre avec un diamètre extérieur de 1 à 10 mm et une longueur de 2 à 20 mm, ou en forme de gravillons avec un diamètre maximal de 2 à 20 mm. L'invention concerne également un procédé de fabrication dudit catalyseur et son utilisation dans un procédé d'oxydation d'ammonium.
EP06777717A 2005-07-20 2006-07-12 Catalyseur plein, fabrication et utilisation dans un procede d'oxydation d'ammonium Withdrawn EP1912737A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102005033825A DE102005033825A1 (de) 2005-07-20 2005-07-20 Vollkatalysator, seine Herstellung und seine Verwendung in einem Ammonoxidationsverfahren
PCT/EP2006/064134 WO2007009921A1 (fr) 2005-07-20 2006-07-12 Catalyseur plein, fabrication et utilisation dans un procede d'oxydation d'ammonium

Publications (1)

Publication Number Publication Date
EP1912737A1 true EP1912737A1 (fr) 2008-04-23

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EP06777717A Withdrawn EP1912737A1 (fr) 2005-07-20 2006-07-12 Catalyseur plein, fabrication et utilisation dans un procede d'oxydation d'ammonium

Country Status (7)

Country Link
US (1) US20100105940A1 (fr)
EP (1) EP1912737A1 (fr)
JP (1) JP2009501624A (fr)
CN (1) CN101267883A (fr)
DE (1) DE102005033825A1 (fr)
TW (1) TW200719959A (fr)
WO (1) WO2007009921A1 (fr)

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CN102218334B (zh) * 2010-04-15 2013-04-03 中国石油化工股份有限公司 含锑的氨氧化催化剂
CN101851179B (zh) * 2010-06-01 2014-04-09 武汉市银冠化工有限公司 氨氧化法制备邻苯二甲腈的生产工艺
EP3490702A4 (fr) * 2016-07-26 2020-02-26 BASF Corporation Catalyseur supporté, catalyseur de réduction catalytique sélective monolithique (rcs), leur procédé de préparation et procédé d'élimination des oxydes d'azote

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CN101267883A (zh) 2008-09-17
TW200719959A (en) 2007-06-01
US20100105940A1 (en) 2010-04-29
DE102005033825A1 (de) 2007-02-08
JP2009501624A (ja) 2009-01-22

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