EP2501472A1 - Catalyseur multicouche utilisé pour la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique, à l'antimoniate de vanadium dans au moins une couche de catalyseur, et procédé de production d'anhydride d'acide phtalique à basse température en zone de surchauffe maximale - Google Patents

Catalyseur multicouche utilisé pour la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique, à l'antimoniate de vanadium dans au moins une couche de catalyseur, et procédé de production d'anhydride d'acide phtalique à basse température en zone de surchauffe maximale

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Publication number
EP2501472A1
EP2501472A1 EP10781485A EP10781485A EP2501472A1 EP 2501472 A1 EP2501472 A1 EP 2501472A1 EP 10781485 A EP10781485 A EP 10781485A EP 10781485 A EP10781485 A EP 10781485A EP 2501472 A1 EP2501472 A1 EP 2501472A1
Authority
EP
European Patent Office
Prior art keywords
catalyst
vanadium
producing
carboxylic acids
xylene
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Withdrawn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
EP10781485A
Other languages
German (de)
English (en)
Inventor
Stefan Altwasser
Jürgen ZÜHLKE
Frank Rosowski
Cornelia Katharina Dobner
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 EP2501472A1 publication Critical patent/EP2501472A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B01J23/002—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
    • B01J23/20—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
    • 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
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/255—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting
    • C07C51/265—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of compounds containing six-membered aromatic rings without ring-splitting having alkyl side chains which are oxidised to carboxyl 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
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

Definitions

  • the present invention relates to a catalyst system for the production of
  • Carboxylic acids and / or carboxylic anhydrides which has a plurality of catalyst layers arranged one above the other in the reaction tube, wherein in at least one of the catalyst layers Vanadiumantimonat is introduced into the active composition.
  • the present invention relates to a process for gas phase oxidation in which a gaseous stream comprising at least one hydrocarbon and molecular oxygen, passes through several catalyst layers and the maximum
  • Hotspot temperature is below 425 ° C.
  • 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 one to be oxidized is passed
  • the catalysts used in the process according to the invention are generally coated catalysts in which the catalytically active composition is applied in the form of a dish on an inert support.
  • the layer thickness of the catalytically active composition is generally 0.02 to 0.25 mm, preferably 0.05 to 0.15 mm.
  • the proportion of the active material in the catalyst is usually 5 to 25 wt .-%, usually 7 to 15 wt .-%.
  • the catalysts have a cup-shaped active mass layer of substantially homogeneous chemical composition. Further, on a carrier can also
  • Steatite is preferred in the form of spheres with a diameter of 3 to 6 mm or of rings with an outer diameter of 5 used to 9 mm, a length of 4 to 7 mm and an inner diameter of 3 to 7 mm.
  • 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 sources are vanadium pentoxide or ammonium meta vanadate.
  • Antimony sources are various antimony oxides.
  • Phosphorus source are in particular phosphoric acid, phosphorous acid, hypophosphorous acid, ammonium phosphate or phosphoric acid esters and especially ammonium dihydrogen phosphate into consideration.
  • the 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,
  • 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 are 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,
  • 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.
  • suspensions are organic binders, preferably copolymers, advantageously in the form of an aqueous dispersion of acrylic acid / maleic acid,
  • the binders are commercially available as aqueous dispersions, with a
  • Binder dispersions is generally 2 to 45 wt .-%, preferably 5 to 35 wt .-%, particularly preferably 7 to 20 wt .-%, based on the weight of
  • 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, the
  • a suitable fluidized bed apparatus is z. As described in DE-A 4006935.
  • coating temperatures of 20 to 500 ° C are used, whereby the coating can be carried out under atmospheric pressure or under reduced pressure.
  • the coating is carried out at 0 ° C to 200 ° C, preferably at 20 to 150 ° C, especially at 60 to 120 ° C.
  • 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 takes place in situ in the gas phase oxidation reactor.
  • Japanese Patent Laid-Open No. 180430/82 discloses two-layer catalysts for the oxidation of o-xylene to phthalic anhydride, which include titanium dioxide and titanium dioxide
  • Vanadium antimonate as catalytically active components.
  • the possible o-xylene loadings as well as the space velocities are at these
  • the hotspot temperatures for example, in the oxidation of o-xylene too
  • Phthalic anhydride are at loadings between 80 and 100 g o-xylene / Nm 3 usually above 440 ° C.
  • High hotspot temperatures are an expression of an excessive increase in the total oxidation of o-xylene to CO, CO2 and water and are associated with increased damage to the catalyst. The aim is therefore to have the lowest possible hotspot temperatures.
  • the object of the present invention was to provide an improved catalyst for the production of carboxylic acids and / or carboxylic anhydrides, in particular to develop an improved catalyst for the partial oxidation of o-xylene to PSA for o-xylene loadings of at least 80 g / Nm 3 .
  • the solution of the problem is a multi-layer catalyst for the production of
  • the hotspot temperature of such a catalyst is significantly lower than in the case of a comparative catalyst prepared without the addition of vanadium antimonate; the carboxylic acid or carboxylic acid anhydride yields are significantly higher.
  • the vanadium antimonate introduced in the active composition of at least one layer can be prepared by reacting any vanadium and antimony compounds.
  • Vanadium antimonate may have different molarity
  • Antimony compounds are used.
  • the preparation of the vanadium antimonate can be characterized, for example, by reaction of the oxides in aqueous solution or else by the use of hydrogen peroxide. In the latter case, for.
  • Connection can be reacted with antimony trioxide to Vanadiumantimonat.
  • the catalysts of the invention comprise in a preferred
  • Embodiment three, four or five layers can, for example, to avoid high hotspot temperatures in conjunction with suitable pre and / or
  • the pre and / or reposting and the intermediate layers can usually consist of catalytically inactive or less active material.
  • Another object of the invention is a method for producing a
  • Carboxylic anhydrides with at least 3 layers characterized in that at least one catalyst layer, a vanadium antimonate is added.
  • Another object of the invention is a process for the gas phase oxidation of hydrocarbons in a multi-layer catalyst with at least 3 layers, at whose preparation at least one catalyst layer, a vanadium antimonate is added.
  • the inventive method is preferably suitable for
  • a preferred embodiment of the method according to the invention is characterized in that the hotspot temperature is above 425 ° C in any of the catalyst layers.
  • Another object of the invention is the use of a
  • Multi-layer catalyst with at least 3 layers in the preparation of which at least one catalyst layer, a vanadium antimonate is added, for the production of carboxylic acids and / or carboxylic anhydrides.
  • Example 1 (according to the invention):
  • Catalyst layer 1 (KL1) (vanadium antimonate as V and Sb source):
  • the suspension is heated with stirring to 100 ° C and stirred after reaching 100 ° C for 16 hours at this temperature. Subsequently, the suspension was cooled to 80 ° C and dried by spray drying. The inlet temperature was at 340 ° C, the outlet temperature at 1 10 ° C.
  • the spray powder thus obtained had a content of vanadium of 32% by weight and an antimony content of 30% by weight. The so produced
  • Vanadium antimonate had a vanadium oxidation state of 4.24 and a BET surface area of 95 m 2 / g.
  • the applied to the steatite rings active mass was 8.4%.
  • the analyzed composition of the active composition consisted of 7.1% V 2 0 5 , 4.5% Sb 2 0 3 , 0.50% Cs, remainder TiO 2 .
  • vanadium pentoxide and antimony trioxide were used instead of vanadium antimonate in the preparation of KL2, KL3, KL4 and KL5 as source of V or Sb in the suspension batch.
  • Catalyst layer 2 (KL2) (vanadium pentoxide and antimony trioxide as V or Sb source): Preparation analogous to KL1 with variation of the composition of the suspension. After calcination of the catalyst for one hour at 450 ° C, the applied to the steatite rings active mass was 9.1%. The analyzed composition of the active composition consisted of 7.1% V 2 0 5 , 1, 8% Sb 2 0 3 , 0.38% Cs, balance Ti0 2 with a
  • Catalyst layer 3 (KL3) (vanadium pentoxide and antimony trioxide as V or Sb source): Preparation analogous to KL1 with variation of the composition of the suspension. After calcination of the catalyst for one hour at 450 ° C, the applied to the steatite rings active composition was 8.5%. The analyzed composition of the active composition consisted of 7.95% V 2 0 5 , 2.7% Sb 2 0 3 , 0.31% Cs, balance Ti0 2 with a
  • Catalyst layer 4 (vanadium pentoxide and antimony trioxide as V or Sb source): Preparation analogous to KL1 with variation of the composition of the suspension. After calcination of the catalyst for one hour at 450 ° C, the applied to the steatite rings active composition was 8.5%. The analyzed composition of the active composition consisted of 7.1% V 2 0 5 , 2.4% Sb 2 0 3 , 0.10% Cs, balance Ti0 2 with a
  • Oxidation of o-xylene to phthalic anhydride The catalytic oxidation of o-xylene to phthalic anhydride was carried out in a salt bath-cooled tubular reactor with an inner diameter of the tubes of 25 mm. From reactor inlet to reactor outlet, 80 cm KL1, 60 cm KL2, 70 cm KL3, 50 cm KL4 and 60 cm KL5 were introduced into a 3.5 m long iron tube with a clear width of 25 mm. The iron tube was surrounded by a salt melt for temperature control, a 4 mm outer diameter thermowell with built-in tension element was the catalyst temperature measurement.
  • Example 2 (not according to the invention):
  • Example 1 the proportion of xylene and phthalide in the reactor exit gas was below 0.10 and below 0.15 wt%, respectively.
  • the PSA yield in Example 1 is significantly higher than that in Example 2, the hotspot temperature in Example 1 is significantly lower than in Example 2.
  • Catalyst layer 6 (KL6) (vanadium pentoxide and antimony trioxide as V or Sb source): Preparation analogous to KL1 with variation of the composition of the suspension. After calcination of the catalyst for one hour at 450 ° C was on the steatite rings applied active mass 8.5%. The analyzed composition of the active composition consisted of 1 1, 0% V 2 0 5 , 2.4% Sb 2 0 3 , 0.22% Cs, balance Ti0 2 with a
  • Catalyst layer 7 (vanadium antimonate as V and Sb source):
  • the vanadium antimonate was prepared analogously to Example 1 while varying the V / Sb ratio.
  • the spray powder thus obtained had a vanadium content of 28.5% by weight and an antimony content of 36% by weight.
  • Active mass consisted of 7.1% V 2 0 5 , 6.0% Sb 2 0 3 , 0.50% Cs, balance Ti0 2 with an average BET surface area of 20 m 2 / g.
  • Catalyst layer 8 (KL8) (vanadium antimonate as V and Sb source):
  • the vanadium antimonate was prepared analogously to Example 1 while varying the V / Sb ratio.
  • the spray powder thus obtained had a vanadium content of 35% by weight and an antimony content of 25.5% by weight.
  • the applied to the steatite rings active composition was 8.3%.
  • the analyzed composition of the active composition consisted of 7.1% V 2 0 5 , 3.5% Sb 2 0 3 , 0.55% Cs, remainder TiO 2 with an average BET surface area of 20 m 2 / g.
  • Catalyst layer 9 (KL9) (vanadium pentoxide and antimony trioxide as source of V or Sb): Preparation analogous to KL1 with variation of the composition of the suspension.
  • KL9 vanadium pentoxide and antimony trioxide as source of V or Sb
  • the analyzed composition of the active composition consisted of 7.1% V 2 0 5 , 6.0% Sb 2 0 3 , 0.38% Cs, balance Ti0 2 with a
  • PSA amount means the resulting phthalic anhydride in weight percent based on 100% o-xylene).

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

Abstract

L'invention concerne un système catalyseur utilisé pour la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique, qui présente plusieurs couches de catalyseur disposées superposées dans un tube à réaction, système dans lequel, pour au moins l'une des couches de catalyseur, de l'antimoniate de vanadium est introduit dans la masse active. L'invention concerne en outre un procédé d'oxydation en phase gazeuse, selon lequel on dirige un courant gazeux qui comprend au moins un hydrocarbure et de l'oxygène moléculaire à travers plusieurs couches de catalyseur, la température en zone de surchauffe maximale étant inférieure à 425°C.
EP10781485A 2009-11-20 2010-11-15 Catalyseur multicouche utilisé pour la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique, à l'antimoniate de vanadium dans au moins une couche de catalyseur, et procédé de production d'anhydride d'acide phtalique à basse température en zone de surchauffe maximale Withdrawn EP2501472A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US26293809P 2009-11-20 2009-11-20
PCT/EP2010/067432 WO2011061132A1 (fr) 2009-11-20 2010-11-15 Catalyseur multicouche utilisé pour la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique, à l'antimoniate de vanadium dans au moins une couche de catalyseur, et procédé de production d'anhydride d'acide phtalique à basse température en zone de surchauffe maximale

Publications (1)

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EP2501472A1 true EP2501472A1 (fr) 2012-09-26

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EP10781485A Withdrawn EP2501472A1 (fr) 2009-11-20 2010-11-15 Catalyseur multicouche utilisé pour la production d'acides carboxyliques et/ou d'anhydrides d'acide carboxylique, à l'antimoniate de vanadium dans au moins une couche de catalyseur, et procédé de production d'anhydride d'acide phtalique à basse température en zone de surchauffe maximale

Country Status (7)

Country Link
US (2) US20110124885A1 (fr)
EP (1) EP2501472A1 (fr)
JP (1) JP2013511377A (fr)
CN (1) CN102612406A (fr)
BR (1) BR112012011701A2 (fr)
TW (1) TW201134547A (fr)
WO (1) WO2011061132A1 (fr)

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US9656983B2 (en) 2013-06-26 2017-05-23 Basf Se Process for starting up a gas phase oxidation reactor
BR112015032335A2 (pt) 2013-06-26 2017-07-25 Basf Se processo para preparar anidrido ftálico
EP3107654A1 (fr) * 2014-02-17 2016-12-28 Basf Se Système catalyseur pour l'oxydation d'o-xylène et/ou de naphtalène en anhydride phtalique
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WO2011061132A1 (fr) 2011-05-26
US20110124885A1 (en) 2011-05-26
CN102612406A (zh) 2012-07-25
BR112012011701A2 (pt) 2016-03-01
US20140213801A1 (en) 2014-07-31
TW201134547A (en) 2011-10-16

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