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WO2012001620A1 - Catalyseur multicouche servant à préparer de l'anhydride phtalique et procédé de préparation d'anhydride phtalique - Google Patents

Catalyseur multicouche servant à préparer de l'anhydride phtalique et procédé de préparation d'anhydride phtalique Download PDF

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Publication number
WO2012001620A1
WO2012001620A1 PCT/IB2011/052831 IB2011052831W WO2012001620A1 WO 2012001620 A1 WO2012001620 A1 WO 2012001620A1 IB 2011052831 W IB2011052831 W IB 2011052831W WO 2012001620 A1 WO2012001620 A1 WO 2012001620A1
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WIPO (PCT)
Prior art keywords
alkali metal
catalyst layer
catalyst
metal content
layer
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.)
Ceased
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PCT/IB2011/052831
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German (de)
English (en)
Inventor
Stefan Altwasser
Jürgen ZÜHLKE
Hans-Martin Allmann
Frank Rosowski
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 China Co Ltd
BASF SE
Original Assignee
BASF China Co Ltd
BASF SE
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Priority to DE112011102205T priority Critical patent/DE112011102205A5/de
Priority to CN201180032801.0A priority patent/CN102958605B/zh
Priority to JP2013517626A priority patent/JP5879342B2/ja
Publication of WO2012001620A1 publication Critical patent/WO2012001620A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • 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
    • 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
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/613—10-100 m2/g
    • 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
    • B01J37/0211—Impregnation using a colloidal suspension
    • 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
    • B01J37/0215—Coating
    • B01J37/0219—Coating the coating containing organic compounds
    • 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
    • B01J37/0234—Impregnation and coating simultaneously
    • 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
    • B01J37/024—Multiple impregnation or coating
    • B01J37/0244—Coatings comprising several layers

Definitions

  • the present invention relates to a multi-layer catalyst for the production of
  • Phthalic anhydride which several in the reaction tube arranged one behind the other
  • the present invention relates to a process for the oxidation of naphthalene or o-xylene / naphthalene mixtures in such a multi-layer catalyst and the use of such multi-layer catalysts for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride.
  • carboxylic acids and / or carboxylic anhydrides are technically characterized by the catalytic gas-phase oxidation of hydrocarbons, such as benzene, the xylenes,
  • Naphthalene, toluene or durene produced 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.
  • the tubes are surrounded by a heat transfer medium, for example a molten salt.
  • coated catalysts have proven suitable for these oxidation reactions, in which the catalytically active material is shell-shaped on an inert
  • Carrier material such as steatite, is applied.
  • catalytically active components of the catalytically active composition of these shell catalysts are generally titanium dioxide and
  • Vanadium pentoxide used. Furthermore, a small number of other oxidic compounds which may be present in the catalytically active composition in small amounts
  • Promoters influence the activity and selectivity of the catalyst.
  • Reactive gas contained aromatic hydrocarbon is reacted at maximum yield.
  • three- to five-layer catalyst systems are used, in particular three- and four-layer catalyst systems.
  • o-xylene to phthalic anhydride (PSA) on vanadium oxide / titanium dioxide catalyst systems is usually carried out with air quantities of about 4 Nm 3 / h and o-xylene. Xylene loadings of up to 100 g / Nm 3 operated.
  • the catalysts are typically developed so that they are particularly well suited for a particular o-xylene / naphthalene mixing ratio or a narrow range of o-xylene / naphthalene mixing ratios.
  • EP 539878 describes a process for the oxidation of o-xylene / naphthalene mixtures on a two-ply catalyst. Mixture ratios of 10/90 to 90/10 wt .-% are used, the maximum total load in the straight pass is 70 g / Nm 3 at a space velocity (GHSV) of 3000 r 1 .
  • the PSA yields are, depending on the catalyst and o-xylene / naphthalene mixing ratio between 98.5 and 1 1 1, 5 wt .-%.
  • the two-layer catalysts in EP 286448 were operated with 70 g / Nm 3 of naphthalene and a GHSV of 3000 r 1 . However, the o-xyol / naphthalene ratios were determined for individual
  • Catalysts varied from 100: 0 to 50:50 or from 50:50 to 0: 100. A broader variation of the mixing ratios using the same catalyst is not
  • Catalysts with more than two catalyst layers are for the oxidation of o-xylene too
  • Phthalic anhydride even at very high loadings of o-xylene of up to 100 g / Nm 3 at 4 Nm 3 / h air described.
  • An example of this is a three-layer catalyst system for the o-xylene oxidation to PSA according to EP 1084115.
  • these catalysts are not for the oxidation of o-xylene / naphthalene mixtures at total loadings of at least 80 g / Nm 3 at about 4 Nm 3 / h Air with a wide variation of o-xylene / naphthalene ratio suitable.
  • This object is achieved by a multi-layer catalyst for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride, in which each catalyst layer
  • the invention thus relates to a multi-layer catalyst for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride, comprising at least three catalyst layers, each containing vanadium oxide and titanium dioxide and whose alkali metal contents are chosen such that a) the alkali metal content of a catalyst layer A highest is
  • a catalyst layer Z which follows the catalyst layer A in the flow direction, has an alkali metal content of 0 to 10% of the alkali metal content of the catalyst layer A, and
  • the catalyst layers located between the catalyst layers A and Z have an alkali metal content of 30 to 90% of the alkali metal content of the catalyst layer A, wherein the alkali metal content of each catalyst layer is higher than the alkali metal content of their respective subsequent flow in the catalyst layer.
  • the multilayer catalyst has three, four or five layers. Particularly preferred are three- and four-layer catalysts.
  • the multi-layer catalysts according to the invention can be used, for example, to avoid high hot-spot temperatures, also in conjunction with suitable pre-and / or final fillings and together with intermediate layers, the pre-and / or
  • Residuals and the intermediate layers can usually consist of catalytically inactive or less active material.
  • a further preferred embodiment of the invention is a four-layer catalyst for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride, in which each catalyst layer contains vanadium oxide and titanium dioxide and the alkali metal contents of the catalyst layers are selected such that a) the alkali metal content of a catalyst layer A am highest
  • a catalyst layer B which follows the catalyst layer A in the flow direction, has an alkali metal content of 60 to 90% of the alkali content of the catalyst layer A
  • a catalyst layer C which follows the catalyst layer B in the flow direction, has an alkali metal content of 30 to 59% of the alkali metal content of the catalyst layer A
  • a catalyst layer Z which follows the catalyst layer C in the flow direction, an alkali metal content of 0 to 10% of the alkali metal content of the catalyst layer A.
  • 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.
  • Carboxylic anhydrides are used, such as quartz (S1O2), porcelain, magnesium oxide, tin dioxide, silicon carbide, rutile, alumina (AI2O3),
  • the catalyst supports can be used, for example, in the form of spheres, rings, tablets, spirals, tubes, extrudates or chippings.
  • the dimensions of these catalyst supports are those commonly used to prepare shell catalysts for the gas phase reactions of aromatic hydrocarbons
  • 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 contain a catalytically active composition which 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 may in preferred embodiments 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 oxide, calculated as Sb 2 C 3. 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 in the anatase form is used for catalytically active material
  • 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 consist of single titanium dioxide or a mixture of titanium dioxides.
  • 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. advantageously 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 oxides, in particular antimony trioxide.
  • Vanadium and antimony can also be in the form of a
  • Vanadiumantimonatucun be used.
  • the vanadium antimonate introduced in the active composition of at least one layer can be prepared by reacting any vanadium and antimony compounds. Preference is given to the direct reaction of the oxides to give a mixed oxide or vanadium antimonate.
  • the vanadium antimonate may have different molar ratios of vanadium to antimony and possibly also contain other vanadium or antimony compounds and mixed with other vanadium or
  • Antimony compounds are used.
  • phosphorus source in particular phosphoric acid, phosphorous acid,
  • the oxides or hydroxide or the thermally convertible into the oxide salts such as carboxylates, in particular the acetate, malonate or oxalate, carbonate, bicarbonate, sulfate or nitrate into consideration.
  • a small number of other oxidic compounds can be contained in the catalytically active material in small amounts, which as promoters influence the activity and selectivity of the catalyst, for example by lowering or increasing its activity.
  • promoters examples include the alkali metals, in particular other than said cesium, lithium, potassium and rubidium, which are usually used in the form of their oxides or hydroxides, thallium (I) oxide, alumina, zirconium oxide, 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 oxide called ceria
  • the oxides of niobium and tungsten in amounts of from 0.01 to 0.50% by weight, based on the catalytically active composition, are also suitable as additives.
  • the application of the layer (s) of the coated catalyst is expediently carried out by spraying a suspension of T1O2 and V2O5, which optionally contains sources of the abovementioned promoter elements, onto the fluidized carrier.
  • the suspension is preferably kept sufficiently long, e.g. B. 2 to 30 hours, especially 12 to 25 hours, stirred to break up agglomerates of the suspended solids and a to obtain homogeneous suspension.
  • the suspension typically has a solids content of from 20 to 50% by weight.
  • the suspension medium is generally aqueous, e.g. For example, water itself or an aqueous mixture with a water-miscible organic solvent such as methanol, ethanol, isopropanol, formamide and the like.
  • suspension organic binders preferably copolymers, advantageously in the form of an aqueous dispersion of acrylic acid / maleic acid, vinyl acetate / vinyl laurate,
  • the binders are commercially available as aqueous dispersions, with a solids content of z. 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
  • Coating can be carried out under atmospheric pressure or under reduced pressure. in the
  • the coating is carried out at 0 ° C to 200 ° C, preferably at 20 to 150 ° C, in particular 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 .-%.
  • the bed length of the catalyst layer A is preferably in the range of 10 to 50%, more preferably in the range of 15 to 30% of the total Katalysator spalliere in the reactor.
  • the bed height of the catalyst layers A and B or A, B and C is advantageously in the range of 60 to 95% of the total Katalysator spalliere.
  • Typical reactors have a filling height of 250 cm to 350 cm. If appropriate, the catalyst layers can also be distributed over several reactors.
  • the catalysts of the invention are particularly suitable for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride with a total loading in the range of 80 to 100 g / Nm 3 with an air flow of about 4 Nm 3 / h.
  • Another object of the invention is a process for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride with a multi-layer catalysts comprising at least three catalyst layers, each containing vanadium oxide and titanium dioxide and whose alkali metal contents are selected such that a) the alkali metal content of a Catalyst layer A is highest,
  • a catalyst layer Z which follows the catalyst layer A in the flow direction, has an alkali metal content of 0 to 10% of the alkali metal content of the catalyst layer A, and
  • the catalyst layers located between the catalyst layers A and Z have an alkali metal content of 30 to 90% of the alkali metal content of the catalyst layer A, wherein the alkali metal content of each catalyst layer is higher than the alkali metal content of the respective subsequent catalyst layer in the flow direction.
  • a preferred embodiment of the invention is a process for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride with a four-layer catalyst wherein each catalyst layer contains vanadium oxide and titanium dioxide and the alkali metal contents of the catalyst layers are selected such that a) the alkali metal content of a catalyst layer A is highest,
  • a catalyst layer B which follows the catalyst layer A in the flow direction, an alkali metal content of 60 to 90% of the alkali content of the catalyst layer A
  • a catalyst layer C which follows the catalyst layer B in the flow direction, an alkali metal content of 30 to 59% of Alkali metal content of the catalyst layer A has,
  • a catalyst layer Z which follows the catalyst layer C in the flow direction, an alkali metal content of 0 to 10% of the alkali metal content of the catalyst layer A.
  • Another object of the invention is the use of a multi-layer catalysts, comprising at least three catalyst layers, each containing vanadium oxide and titanium dioxide and whose alkali metal contents are selected so that a) the alkali metal content of a catalyst layer A is the highest
  • a catalyst layer Z which follows the catalyst layer A in the flow direction, has an alkali metal content of 0 to 10% of the alkali metal content of the catalyst layer A, and
  • the catalyst layers located between the catalyst layers A and Z have an alkali metal content of 30 to 90% of the alkali metal content of the catalyst layer A, wherein the alkali metal content of each catalyst layer is higher than the alkali metal content of each downstream in the flow direction catalyst layer for the oxidation of naphthalene or o Xylene / naphthalene mixtures to phthalic anhydride
  • Alkali metal contents of the catalyst layers are chosen so that
  • a catalyst layer B which follows the catalyst layer A in the flow direction, an alkali metal content of 60 to 90% of the alkali content of the catalyst layer A
  • a catalyst layer C which follows the catalyst layer B in the flow direction, an alkali metal content of 30 to 59% of Alkali metal content of the catalyst layer A has,
  • a catalyst layer Z which follows the catalyst layer C in the flow direction, an alkali metal content of 0 to 10% of the alkali metal content of the catalyst layer A, for the oxidation of naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride.
  • the catalytically active composition applied in this way consisted of 0.03% by weight of phosphorus (calculated as P), 4.22% by weight. Vanadium (calculated as V2O5), 0.87 wt.% Cesium (calculated as Cs), 0.2 wt.% Nb (calculated as Nb 2 O 5 ), 0.04 wt.% K (calculated as K ) and 94.68 weight percent titanium dioxide.
  • the active material content after 1 h calcination at 450 ° C was 8.9%.
  • Preparation of the second catalyst layer KL2 Preparation of the second catalyst layer KL2:
  • the catalyst was prepared by varying the composition of the suspension compared to KL1.
  • the catalytically active mass applied in this manner consisted of 0.03 wt% phosphorus (calculated as P), 4.22 wt% vanadium (calculated as V2O5), 0.67 wt% cesium (calculated as Cs ), 0.2 wt% Nb (calculated as Nb 2 0 5 ), 0.03 wt% K
  • the catalyst was prepared by varying the composition of the suspension compared to KL1.
  • the catalytically active mass applied in this way consisted of 0.03% by weight of phosphorus (calculated as P), 4.22% by weight of vanadium (calculated as V 2 O 5 ), 0.45% by weight of cesium ( calculated as Cs), 0.2 wt% Nb (calculated as Nb 2 O 5 ), 0.02 wt% K
  • the catalyst was prepared by varying the composition of the suspension compared to KL1.
  • the catalytically active composition applied in this way consisted of 0.02% by weight of phosphorus (calculated as P), 4.22% by weight of vanadium (calculated as V 2 O 5 ), 0.00% by weight of cesium ( calculated as Cs), 0.2 wt.% Nb (calculated as Nb 2 O 5 ), 0.00 wt.% K
  • the reactor tube was equipped with a
  • Thermocouple equipped. 4.0 Nm 3 air per hour with o-xylene (purity about 99 wt .-%) or naphthalene (purity about 97.5 wt .-%) of 0 to 85 g / Nm 3 passed through the tubes.
  • the PSA yields were measured in the reactor starting gas and are in wt .-% (kg PSA per kg of reacted o-xylene or naphthalene) based on 100% o-xylene or 100% naphthalene indicated. Results and examples
  • Example 1 Laying length distribution steatite pre-packing / KL1 / KL2 / KL3 / KL4 5 cm / 80 cm / 80 cm / 90 cm / 90 cm / 90 cm
  • a PSA yield of 1 1 1, 0 wt .-% and a phthalide and naphthoquinone content of 0.1 1 and 0.34 wt .-% was achieved.
  • Total loading of at least 80 g / Nm 3 at 4 Nm 3 / h air was the o-xylene / naphthalene ratio thus at high PSA yield and good product spectrum (low yields of phthalide and naphthoquinone) varies between 0: 100% and 65:35% become.
  • Hotspot temperatures were below 450 ° C for all feed compositions.

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

Abstract

La présente invention concerne un catalyseur multicouche servant à préparer de l'anhydride phtalique et comprenant plusieurs couches de catalyseurs disposées successivement dans le tube de réaction, les couches individuelles de catalyseur présentant des teneurs en métaux alcalins qui vont en diminuant dans le sens d'écoulement. La présente invention concerne, en outre, un procédé d'oxydation de naphtalène ou de mélanges d'o-xylène et de naphthalène sur un tel catalyseur multicouche, ainsi que l'utilisation de tels catalyseurs multicouche pour l'oxydation de naphtalène ou de mélanges d'o-xylène et de naphtalène en vue d'obtenir de l'anydride phtalique.
PCT/IB2011/052831 2010-06-30 2011-06-28 Catalyseur multicouche servant à préparer de l'anhydride phtalique et procédé de préparation d'anhydride phtalique Ceased WO2012001620A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
DE112011102205T DE112011102205A5 (de) 2010-06-30 2011-06-28 Mehrlagenkatalysator zur Herstellung von Phthalsäureanhydrid und Verfahren zur Herstellung von Phthalsäureanhydrid
CN201180032801.0A CN102958605B (zh) 2010-06-30 2011-06-28 用于制备邻苯二甲酸酐的多层催化剂以及制备邻苯二甲酸酐的方法
JP2013517626A JP5879342B2 (ja) 2010-06-30 2011-06-28 無水フタル酸を製造するための多層触媒、及び無水フタル酸の製造方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP10167826 2010-06-30
EP10167826.6 2010-06-30

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WO2012001620A1 true WO2012001620A1 (fr) 2012-01-05

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Cited By (1)

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Publication number Priority date Publication date Assignee Title
EP3470138A1 (fr) * 2017-10-10 2019-04-17 Opti-Innovations Limited Additif de carburant catalytique

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US20060276661A1 (en) * 2003-05-23 2006-12-07 Basf Aktiengesellschaft Three-layered or four-layered catalyst systems for producing phthalic anhydride
US20090163726A1 (en) * 2006-05-19 2009-06-25 Basf Se Catalyst system for preparing carboxylic acids and/or carboxylic anhydrides
US20090318712A1 (en) * 2006-06-20 2009-12-24 Basf Se Catalyst system and method for producing carboxylic acids and/or carboxylic acid anhydrides

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