EP3107654A1 - Système catalyseur pour l'oxydation d'o-xylène et/ou de naphtalène en anhydride phtalique - Google Patents

Système catalyseur pour l'oxydation d'o-xylène et/ou de naphtalène en anhydride phtalique

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Publication number
EP3107654A1
EP3107654A1 EP15706733.1A EP15706733A EP3107654A1 EP 3107654 A1 EP3107654 A1 EP 3107654A1 EP 15706733 A EP15706733 A EP 15706733A EP 3107654 A1 EP3107654 A1 EP 3107654A1
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EP
European Patent Office
Prior art keywords
catalyst
crystallite size
weight
primary crystallite
antimony trioxide
Prior art date
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Application number
EP15706733.1A
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German (de)
English (en)
Inventor
Nico Frederik FISCHER
Diana Carolina GALEANO NUNEZ
Michael Krämer
Markus Schubert
Jürgen ZÜHLKE
Hans-Martin Allmann
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BASF SE
Original Assignee
BASF SE
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Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP3107654A1 publication Critical patent/EP3107654A1/fr
Withdrawn legal-status Critical Current

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    • 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
    • B01J35/19—Catalysts containing parts with different compositions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
    • C07D307/77—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom ortho- or peri-condensed with carbocyclic rings or ring systems
    • C07D307/87—Benzo [c] furans; Hydrogenated benzo [c] furans
    • C07D307/89—Benzo [c] furans; Hydrogenated benzo [c] furans with two oxygen atoms directly attached in positions 1 and 3
    • 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
    • B01J23/18—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
    • 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
    • B01J23/20—Vanadium, niobium or tantalum
    • B01J23/22—Vanadium
    • 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
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/195—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with vanadium, niobium or tantalum
    • B01J27/198—Vanadium
    • 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
    • B01J35/70—Catalysts, in general, characterised by their form or physical properties characterised by their crystalline properties, e.g. semi-crystalline
    • B01J35/77—Compounds characterised by their crystallite 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G30/00—Compounds of antimony
    • C01G30/004—Oxides; Hydroxides; Oxyacids
    • C01G30/005—Oxides
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/06—Details of tube reactors containing solid particles
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2002/00—Crystal-structural characteristics
    • C01P2002/60—Compounds characterised by their crystallite size

Definitions

  • the present invention relates to a catalyst system for the oxidation of o-xylene and / or naphthalene to phthalic anhydride (PSA), which comprises a plurality of catalyst layers arranged one behind the other in the reaction tube, for the preparation of which an antimony trioxide was used, which contains a significant proportion of Senarmontit whose primary crystallites have a size of less than 200 nm.
  • PSA phthalic anhydride
  • the present invention relates to a process for gas phase oxidation in which a gas stream comprising at least one hydrocarbon and molecular oxygen is passed through a catalyst system which comprises a plurality of catalyst layers arranged one behind the other in the reaction tube and for the production of which an antimony trioxide has been used Contains a proportion of Senarmontit whose primary crystallites have a size of less than 200 nm.
  • a variety of carboxylic acids and / or carboxylic anhydrides are produced industrially by the catalytic gas phase oxidation of hydrocarbons such as benzene, the xylenes, naphthalene, toluene or durene in fixed bed reactors. You can in this way z.
  • a mixture of an oxygen-containing gas and the starting material to be oxidized is passed through tubes containing a bed of catalyst. For temperature control, the tubes are surrounded by a heat transfer medium, for example a molten salt.
  • coated catalysts have proven effective for these oxidation reactions, in which the catalytically active material is coated in a dish-shaped manner on an inert carrier material, such as steatite.
  • the catalysts have a cup-shaped active mass layer of substantially homogeneous chemical composition.
  • one or more successive two or more active mass layers can be applied to a support. It is then spoken of a two- or multi-layer catalyst (see, for example, DE 19839001 A1).
  • Titanium dioxide and vanadium pentoxide are generally used as the catalytically active constituents of the catalytically active composition of these shell catalysts. Furthermore, a small number of other oxidic compounds which, as promoters, influence the activity and selectivity of the catalyst, including cesium, phosphorus and antimony oxides, can be present in the catalytically active composition in small amounts.
  • Catalysts with a particularly high PSA yield can be obtained according to EP 1636161 if certain V20s / Sb203 ratios are set and the antimony trioxide has a defined average particle size.
  • the presence of antimony oxides leads to an increase in PSA selectivity, the cause being seen in a separation of the vanadium centers.
  • the antimony oxides used in the active composition of the catalysts may be different antimony (III), antimony (IV) or antimony (V) compounds, most often antimony trioxide or antimony pentoxide are used.
  • EP 522871 describes the use of antimony pentoxide
  • US 2009/306409 and EP 1636161 disclose the use of antimony trioxide.
  • Antimony trioxide has the property of spreading better on titanium dioxide compared to antimony oxide and antimony pentoxide, so that a significantly better distribution on the catalyst is achieved.
  • phase-pure Senarmontit used (see, Schubert, U. -A. et al., Topics in Catalysis, 2001, Vol. 15 (2-4), pages 195 to 200).
  • Valentinit orthorhombic modification of the antimony drug, which is called Valentinit (Golunski, S.E. et al., Appl. Catal., 1989, Vol. 48, pages 123 to 135).
  • catalysts for gas phase oxidations which have the highest possible conversion at high selectivity.
  • a catalyst system for the oxidation of o-xylene and / or naphthalene to phthalic anhydride which comprises a plurality of catalyst layers arranged one behind the other in the reaction tube, for its preparation, an antimony trioxide was used which contains a significant proportion of Senarmontit whose Primärkristallite partially a size of less than 200 nm.
  • the invention thus relates to a catalyst system for the oxidation of o-xylene and / or naphthalene to phthalic anhydride, which comprises a plurality of catalyst layers arranged one behind the other in the reaction tube, for the preparation of which an antimony trioxide having a Senarmontitge is used of at least 20 wt .-% and the Senarmontitprimärkristallite have a polymodal size distribution, wherein between 10 and 80 wt .-% have a Primärkristallit- size of ⁇ 200 nm and a mean primary crystallite size of ⁇ 150 nm.
  • the antimony trioxide having the above-described properties to be used in the present invention can be used for the production of one or more catalyst layers.
  • the catalyst system has three, four or five layers, antimony trioxide having the properties described above being used to produce at least one layer.
  • the antimony trioxide used to prepare the catalyst system according to the invention has a Senarmontitgehalt of at least 50 wt .-%.
  • Senarmontitprimärkristallite in the antimony trioxide used in the preparation of the catalyst system according to the invention has a primary crystallite size of ⁇ 200 nm and an average primary crystallite size of ⁇ 100 nm, most preferably of ⁇ 50 nm.
  • between 10 and 50 wt .-% of Senarmontitprimärkristallite in the antimony trioxide used in the preparation of the catalyst system according to the invention has a primary crystallite size of ⁇ 200 nm and an average primary crystallite size of ⁇ 150 nm.
  • Senarmontitprimärkristallite in the antimony trioxide used to prepare the catalyst system according to the invention has a primary crystallite size of ⁇ 200 nm and a mean primary crystallite size of ⁇ 100 nm, in particular ⁇ 50 nm.
  • the catalyst systems according to the invention can be used, for example, to avoid high hotspot temperatures also in conjunction with suitable precursors and / or replenishers and together with intermediate layers, the precursors and / or replenishments and the intermediate layers usually being of catalytically inactive or less can consist of active material.
  • the catalysts according to the invention are generally what are known as shell catalysts in which the catalytically active composition is applied in the form of a dish on an inert carrier material.
  • Virtually all support materials of the prior art, which are advantageously used in the preparation of shell catalysts for the oxidation of aromatic hydrocarbons to aldehydes, carboxylic acids and / or carboxylic anhydrides, can be used as the inert support material, for example quartz (S1O2), porcelain, magnesium oxide , Tin dioxide, silicon carbide, rutile, alumina (Al 2 O 3), aluminum silicate, steatite (magnesium silicate), zirconium silicate, cerium silicate or mixtures of these support materials.
  • the catalyst carriers can be used, for example, in the form of spheres, rings, tablets, spirals, tubes, extrudates or chippings.
  • catalyst supports are usually those used to prepare shell catalysts for the gas phase reactions.
  • Steatite is preferably used in the form of spheres with a diameter of 3 to 6 mm or of rings with an outer diameter of 5 to 9 mm and a length of 3 to 8 mm and a wall thickness of 1 to 2 mm.
  • the catalysts according to the invention comprise a catalytically active composition which, in addition to antimony trioxide, comprises at least vanadium oxide and titanium dioxide and can be applied to the support material in one or more layers. Different layers can differ in their composition.
  • the catalytically active composition based on the total amount of the catalytically active composition, contains 1 to 40% by weight of vanadium oxide, calculated as V2O5, and 60 to 99% by weight of titanium oxide, calculated as T1O2.
  • the catalytically active composition in preferred embodiments may additionally contain up to 1% by weight of a cesium compound, calculated as Cs, up to 1% by weight of a phosphorus compound, calculated as P, and up to 10% by weight of antimony oxides, calculated as Sb 2 C All information on the composition of the catalytically active material refers to its calcined state, eg after calcination of the catalyst for one hour at 450 ° C.
  • titanium dioxide is used in the anatase form for catalytically active material.
  • the titanium dioxide preferably has a BET surface area of from 15 to 60 m 2 / g, in particular from 15 to 45 m 2 / g, particularly preferably from 13 to 28 m 2 / g.
  • the titanium dioxide used may consist of a single titanium dioxide or a mixture of titanium dioxides. In the latter case, the value of the BET surface area is determined as a weighted average of the contributions of the individual titanium dioxides.
  • the titanium dioxide used is z. B. advantageous from a mixture of a T1O2 with a BET surface area of 5 to 15 m 2 / g and a T1O2 with a BET surface area of 15 to 50 m 2 / g.
  • Vanadium pentoxide or ammonium metavanadate are particularly suitable as the vanadium source.
  • Suitable antimony sources are various antimony trioxides, an antimony trioxide having a senarmontite content of at least 20% by weight being used according to the invention as described above.
  • the phosphorus source in particular phosphoric acid, phosphorous acid, hypophosphorous acid, ammonium phosphate or phosphoric acid esters and especially Ammoniumdihydrogenphosphat come into consideration.
  • Suitable sources of cesium are the oxides or hydroxide or the salts which can be thermally converted into the oxide, such as carboxylates, in particular the acetate, malonate or oxalate, carbonate, bicarbonate, sulfate or nitrate.
  • a small number of other oxidic compounds which, as promoters, influence the activity and selectivity of the catalyst, for example by lowering or increasing its activity, can be present in the catalytically active composition in small amounts.
  • promoters examples include the alkali metals, in particular lithium, potassium and rubidium in addition to the said cesium, most commonly used in the form of their oxides or hydroxides, thallium (I) oxide, alumina, zirconia, iron oxide, nickel oxide, cobalt oxide, manganese oxide, tin oxide, silver oxide, copper oxide, chromium oxide, molybdenum oxide, tungsten oxide, iridium oxide, tantalum oxide, niobium oxide, arsenic oxide, antimony tetroxide Called antimony pentoxide and ceria.
  • I thallium
  • alumina zirconia
  • iron oxide nickel oxide
  • cobalt oxide manganese oxide
  • tin oxide silver oxide
  • copper oxide copper oxide
  • chromium oxide molybdenum oxide
  • tungsten oxide iridium oxide
  • tantalum oxide niobium oxide
  • arsenic oxide antimony tetroxide Called antimony pentoxid
  • the oxides of nitrobenzene and tungsten in amounts of from 0.01 to 0.50% by weight, based on the catalytically active material, are also suitable as additives.
  • the application of the layer (s) of the coated catalyst is expediently carried out by spraying a suspension of ⁇ 2 and V2O5, which optionally contains sources of the abovementioned promoter elements, onto the fluidized support.
  • the suspension is preferably kept sufficiently long, e.g. B. 2 to 30 hours, in particular 12 to 25 hours, stirred to break agglomerates of the suspended solids and to obtain a homogeneous Sus- pension.
  • the suspension typically has a solids content of from 20 to 50% by weight.
  • the suspension medium is generally aqueous, e.g., water itself or an aqueous mixture with a water-miscible organic solvent such as methanol, ethanol, isopropanol, formamide and the like.
  • organic binders preferably copolymers, advantageously in the form of an aqueous dispersion of acrylic acid / maleic acid, vinyl acetate / vinyl laurate, vinyl acrylate, styrene / acrylate and vinyl acetate / ethylene are added to the suspension.
  • the binders are commercially available as aqueous dispersions, with a solids content of, for. B. 35 to 65 wt .-%.
  • the amount of such binder dispersions used is generally from 2 to 45% by weight, preferably from 5 to 35% by weight, particularly preferably from 7 to 20% by weight, based on the weight of the suspension.
  • the carrier is in z.
  • a fluidized bed or fluidized bed apparatus in an ascending gas stream in particular air, fluidized.
  • the apparatuses usually consist of a conical or spherical container in which the fluidizing gas is introduced from below or from above via a dip tube.
  • the suspension is sprayed via nozzles from above, from the side or from below into the fluidized bed.
  • a centrally or concentrically arranged around the dip tube riser Within the riser there is a higher gas velocity, which transports the carrier particles upwards. In the outer ring the gas velocity is only slightly above the loosening speed. So the particles are moved vertically in a circle.
  • a suitable fluidized bed apparatus is z. As described in DE-A 4006935.
  • coating temperatures of 20 to 500 ° C. are generally used, whereby the coating can be carried out under atmospheric pressure or under reduced pressure. Generally done the coating at 0 ° C to 200 ° C, preferably at 20 to 150 ° C, in particular carried out at 60 to 120 ° C.
  • the layer thickness of the catalytically active composition is generally 0.02 to 0.2 mm, preferably 0.05 to 0.15 mm.
  • the active mass fraction of the catalyst is usually 5 to 25 wt .-%, usually 7 to 15 wt .-%.
  • thermal treatment of the pre-catalyst thus obtained at temperatures above 200 to 500 ° C escapes the binder by thermal decomposition and / or combustion of the applied layer.
  • the thermal treatment is preferably carried out in situ in the gas phase oxidation reactor.
  • a further subject of the invention is a process for gas-phase oxidation in which a gas stream comprising at least one hydrocarbon and molecular oxygen is passed through a catalyst, for the production of which an antimony trioxide having a senarmontite content of at least 20% by weight is used and the Senarmontitprimärkristallite have a polymodal size distribution, wherein between 10 and 80 wt .-% have a Primärkristal- litstand of ⁇ 200 nm and a mean primary crystallite size of ⁇ 150 nm, preferably ⁇ 100 nm, more preferably ⁇ 50 nm.
  • a preferred embodiment of the invention is a process for the gas-phase oxidation of o-xylene and / or naphthalene to phthalic anhydride, wherein a gas stream comprising at least o-xylene and / or naphthalene and molecular oxygen is passed through a catalyst system comprising several in the reaction tube
  • An antimony trioxide with a Senarmontitgehalt of at least 20 wt .-% is used and the Senarmontitprimärkristallite have a polymodal size distribution, wherein between 10 and 80 wt .-%, a primary crystallite size of ⁇ 200 nm and a mean Primary crystallite size of ⁇ 150 nm, preferably ⁇ 100 nm, more preferably ⁇ 50 nm have.
  • the primary crystallite size is the maximum expansion of the primary crystallites over the three spatial directions.
  • the determination was carried out by means of X-ray powder diffractometry.
  • the antimony trioxide powder was measured in an X-ray powder diffractometer from Bruker of the type "D8 Advance.” The measurement parameters were as follows: Circular diameter 500 mm
  • the catalytic oxidation of o-xylene to phthalic anhydride was carried out in a salt bath-cooled tubular reactor having a tube internal diameter of 25 mm and a length of 350 cm. From reactor inlet to reactor outlet 130 cm KL1, 70 cm KL2, 60 cm KL3 and 60 cm KL4 were filled. The tubular reactor was surrounded by a molten salt for temperature control, a 4 mm outer diameter thermowell with built-in tension element was used for the catalyst temperature measurement.
  • the tubular reactor was every hour from top to bottom with 4.0 Nm 3 of air having loadings of 99 to 99.4 wt .-% sodium o-xylene of 30 to 100 g 0 - flows through xylene / Nm 3 i_uft.
  • Example 1 (according to the invention):
  • the antimony trioxide used for the KL1, KL2 and KL3 was a material from Gredmann, Taiwan (batch number CAK1 1 1 T2), which consists of 99% by weight of senarmontite and 1% by weight of Valentinit.
  • the Senarmontitprimärkristallite characterized by a bimodal size distribution, wherein 27 wt .-% have a primary crystallite size of ⁇ 200 nm and a mean primary crystallite size of 35 nm.
  • Table 1 Catalytic Performance of the Catalyst System Example 1 at a
  • the antimony trioxide used for the KL1, KL2 and KL3 was a material company Gredmann, Taiwan (batch number B4K021 T2), which consists of 78% by weight of senarmontite and 22% by weight of Valentinit.
  • the Senarmontitprimärkristallite characterized by a bimodal size distribution, wherein 14 wt .-% have a primary crystallite size of ⁇ 200 nm and a mean primary crystallite size of 32 nm.
  • Table 2 Catalytic performance of the catalyst system Example 2 with a total air flow of 4 Nm 3 / h.
  • the antimony trioxide used for the KL1, KL2 and KL3 was a material company Gredmann, Taiwan (batch number CBK101 T2), which consists of 67% by weight of senarmontite and 33% by weight of Valentinit.
  • the Senarmontitprimärkristallite characterized by a bimodal size distribution, wherein 1 1 wt .-% have a primary crystallite size of ⁇ 200 nm and an average primary crystallite size of 27 nm.
  • Table 3 Catalytic Performance of the Catalyst System Example 3 at a
  • the antimony trioxide used for the KL1, KL2 and KL3 was a material from Merck KGaA, Germany (batch number K40961235), which consists of 77% by weight of senarmontite and 23% by weight of Valentinit.
  • the Senarmontitprimäre crystallites have no bimodal size distribution, but have a mean primary crystallite size of 156 nm.
  • Table 4 Catalytic performance of the catalyst system Example 4 at a total air flow of 4 Nm 3 / h.
  • the antimony trioxide used for the KL1, KL2 and KL3 was a material from Merck KGaA, Germany (batch number K43228935), which consists of 99% by weight of senarmontite and 1% by weight of Valentinit.
  • the Senarmontitprimärekristallite no bimodal size distribution, but have a mean primary crystallite size of> 200 nm.
  • Vanadium pentoxide and another liter of demineralized water was added and stirred at 90 ° C for 25 hours. Subsequently, the suspension was cooled to 80 ° C and per Spray drying dried. The inlet temperature was at 340 ° C, the
  • Vanadium antimonate (synthesized as described above from Animontrioxid Gredmann (lot number CAK1 11 T2) with 1% by weight of Valentinit) was suspended in 1583 g of demineralized water and stirred for 18 hours to obtain a homogeneous distribution.
  • organic binder consisting of a copolymer of vinyl acetate and vinyl laurate in the form of a 50 wt .-% aqueous dispersion was added.
  • 750 g of this suspension were sprayed onto 2 kg of steatite (magnesium silicate) in the form of rings with dimensions of 7 mm ⁇ 7 mm ⁇ 4 mm and dried.
  • the applied to the steatite rings active composition was 8.5 wt .-%.
  • the analyzed composition of the active composition consisted of 7, 1 wt .-% V 2 0 5 , 4.5 wt .-% Sb 2 0 3 , 0.50 wt .-% Cs, balance Ti0 2 .
  • Composition of the active composition consisted of 7.1 wt .-% V2O5, 1, 8 wt .-% Sb203, 0.38 wt .-% Cs, balance Ti0 2nd
  • Composition of the active composition consisted of 7.95 wt .-% V2O5, 2.7 wt .-% Sb203, 0.31 wt .-% Cs, balance Ti0 2nd
  • Composition of the active composition consisted of 7.1 wt .-% V2O5, 2.4 wt .-% Sb203, 0.09 wt .-% Cs, remainder Ti0 2nd
  • salt bath cooled tubular reactor with a tube internal diameter of 25 mm and a length of 350 cm performed. From reactor inlet to reactor outlet 80 cm KL1, 60 cm KL2, 70 cm KL3, 50 cm KL4 and 60 cm KL5 were filled. The tube reactor was to
  • Example 6 (according to the invention):
  • the antimony trioxide from Gredmann, Taiwan (batch number CAK1 11 T2) was used, which consists of 99% by weight of senarmontite and 1% by weight of Valentinit.
  • the Senarmontitprimärkristallite characterized by a bimodal size distribution, wherein 27 wt .-% have a primary crystallite size of ⁇ 200 nm and a mean primary crystallite size of 35 nm.
  • the antimony trioxide used for the KL2, KL3 and KL4 was a material from Merck KGaA, Germany (batch number K40961235), which consists of 77% by weight of senarmontite and 23% by weight of Valentinit.
  • the Senarmontitprimäre crystallites have no bimodal size distribution, but have a mean primary crystallite size of 156 nm.
  • the antimony trioxide from Merck KGaA, Germany (batch number K43228935) was used, which consists of 99% by weight of senarmontite and 1% by weight of Valentinit.
  • the Senarmontitprimärekristallite no bimodal size distribution, but have a mean primary crystallite size of> 200 nm.
  • KL2 an antimony trioxide from Merck KGaA, Germany

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Abstract

La présente invention concerne un système catalyseur destiné à l'oxydation d'o-xylène et/ou de naphtalène en anhydride phtalique (AP), qui comprend une pluralité de couches de catalyseur disposées les unes derrière les autres dans le tube de réaction, pour la production duquel on a utilisé un trioxyde d'antimoine, qui contient une quantité importante de sénarmontite dont les cristallites primaires ont en partie une taille inférieure à 200 nm. La présente invention concerne en outre un procédé d'oxydation en phase gazeuse dans lequel on dirige un flux de gaz, comprenant au moins un hydrocarbure et de l'oxygène moléculaire, à travers un système de catalyseur qui comprend une pluralité de couches de catalyseur disposées les unes derrière les autres dans le tube de réaction, pour la production duquel on a utilisé un trioxyde d'antimoine, qui contient une quantité importante de sénarmontite dont les cristallites primaires ont en partie une taille inférieure à 200 nm.
EP15706733.1A 2014-02-17 2015-02-17 Système catalyseur pour l'oxydation d'o-xylène et/ou de naphtalène en anhydride phtalique Withdrawn EP3107654A1 (fr)

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PCT/EP2015/053267 WO2015121483A1 (fr) 2014-02-17 2015-02-17 Système catalyseur pour l'oxydation d'o-xylène et/ou de naphtalène en anhydride phtalique

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US9914716B2 (en) 2014-02-17 2018-03-13 Basf Se Catalyst system for oxidation of o-xylene and/or naphthalene to phthalic anhydride
EP3047904A1 (fr) 2015-01-22 2016-07-27 Basf Se Système catalyseur pour oxydation d'o-xylène et/ou de naphtalène pour produire de l'anhydride phtalique
WO2016156042A1 (fr) 2015-03-27 2016-10-06 Basf Se Corps moulé catalyseur servant à l'oxydation catalytique de so2 en so3
DE102017202351A1 (de) * 2017-02-14 2018-08-16 Clariant International Ltd Katalysatormaterial zur Oxidation von Kohlenwasserstoffen mit antimondotiertem Titandioxid

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US5235071A (en) 1991-07-10 1993-08-10 Nippon Shokubai Co., Ltd. Catalyst for producing phthalic anhydride and process by using the same
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BR112012011701A2 (pt) * 2009-11-20 2016-03-01 Basf Se catalisador em multicamada, processo para a oxidação de o-xileno em anidrido ftálico, uso de um catalisador, e, processo para produzir um catalisador em multicamada
WO2012014154A1 (fr) * 2010-07-30 2012-02-02 Basf Se Catalyseur pour l'oxydation de o-xylène et/ou de naphthalène en anhydride phtalique
US9029289B2 (en) * 2012-07-16 2015-05-12 Basf Se Catalyst for preparing carboxylic acids and/or carboxylic anhydrides
EP2872251A4 (fr) * 2012-07-16 2016-03-02 Basf Se Catalyseur servant à la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique
US9914716B2 (en) 2014-02-17 2018-03-13 Basf Se Catalyst system for oxidation of o-xylene and/or naphthalene to phthalic anhydride

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WO2015121483A1 (fr) 2015-08-20
JP2017512127A (ja) 2017-05-18
JP6563410B2 (ja) 2019-08-21
US9868713B2 (en) 2018-01-16
CN105992647A (zh) 2016-10-05
US20170008866A1 (en) 2017-01-12

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