WO2009095216A2 - Katalysator für die katalytische gasphasenoxidation von aromatischen kohlenwasserstoffen zu aldehyden, carbonsäuren und/oder carbonsäureanhydriden, insbesondere zu phthalsäureanhydrid - Google Patents
Katalysator für die katalytische gasphasenoxidation von aromatischen kohlenwasserstoffen zu aldehyden, carbonsäuren und/oder carbonsäureanhydriden, insbesondere zu phthalsäureanhydrid Download PDFInfo
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- WO2009095216A2 WO2009095216A2 PCT/EP2009/000534 EP2009000534W WO2009095216A2 WO 2009095216 A2 WO2009095216 A2 WO 2009095216A2 EP 2009000534 W EP2009000534 W EP 2009000534W WO 2009095216 A2 WO2009095216 A2 WO 2009095216A2
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- 239000004323 potassium nitrate Substances 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000011164 primary particle Substances 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000002356 single layer Substances 0.000 description 1
- 235000010288 sodium nitrite Nutrition 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 229910052715 tantalum Inorganic materials 0.000 description 1
- GUVRBAGPIYLISA-UHFFFAOYSA-N tantalum atom Chemical compound [Ta] GUVRBAGPIYLISA-UHFFFAOYSA-N 0.000 description 1
- 229910052716 thallium Inorganic materials 0.000 description 1
- BKVIYDNLLOSFOA-UHFFFAOYSA-N thallium Chemical compound [Tl] BKVIYDNLLOSFOA-UHFFFAOYSA-N 0.000 description 1
- 238000009997 thermal pre-treatment Methods 0.000 description 1
- 229910052718 tin Inorganic materials 0.000 description 1
- 239000011135 tin Substances 0.000 description 1
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 1
- 229910001887 tin oxide Inorganic materials 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 238000012549 training Methods 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 238000010626 work up procedure Methods 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
- GFQYVLUOOAAOGM-UHFFFAOYSA-N zirconium(iv) silicate Chemical compound [Zr+4].[O-][Si]([O-])([O-])[O-] GFQYVLUOOAAOGM-UHFFFAOYSA-N 0.000 description 1
Classifications
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- 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
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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
- 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
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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
- 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
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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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/66—Silver or gold
- B01J23/68—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/682—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with vanadium, niobium, tantalum or polonium
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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
- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
- B01J37/0221—Coating of particles
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- 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
- B01J8/04—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 the fluid passing successively through two or more beds
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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
- 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
- B01J8/067—Heating or cooling the reactor
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- 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
-
- 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
- C07C51/31—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting
- C07C51/313—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation of cyclic compounds with ring-splitting with molecular oxygen
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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
- 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
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/023—Details
- B01J2208/024—Particulate material
- B01J2208/025—Two or more types of catalyst
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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
- B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
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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
- B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
- B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
Definitions
- the invention relates to a catalyst for the catalytic gas-phase oxidation of aromatic hydrocarbons to aldehydes, carboxylic acids and / or carboxylic anhydrides, in particular to phthalic anhydride, according to the preamble of claim 1.
- carboxylic acids and / or carboxylic anhydrides are produced industrially by the catalytic gas-phase oxidation of aromatic hydrocarbons such as benzene, xylene, naphthalene, toluene or durene in fixed bed reactors, preferably tube bundle reactors.
- aromatic hydrocarbons such as benzene, xylene, naphthalene, toluene or durene
- benzoic acid, maleic anhydride, phthalic anhydride, isophthalic acid, terephthalic acid or pyromellitic anhydride are obtained.
- reaction tubes are arranged in parallel and in which there is a bed of a suitable catalyst. Due to the strong formation of heat in such oxidation reactions, it is necessary to surround the reaction tubes with a heat transfer medium, for example a molten salt, in order to produce the reaction mixture
- the heat transfer medium used is generally a salt melt, preferably a mixture of sodium nitrite and potassium nitrate.
- hot spots may come in the catalyst bed to form local temperature maxima, the so-called hot spots ("hot spots").
- Example 2 a reduced selectivity by partial total oxidation of the starting material or an increased formation of undesirable by-products such as Benzoic acid, maleic anhydride and phthalide in the oxidation of o-xylene to phthalic anhydride, which can be separated only partially with increased effort with partial loss of the desired end product.
- Another major disadvantage in the formation of such locally partly greatly increased temperatures ("hot spots") in the catalyst bed is the significant amount of time after initial commissioning, which is needed to achieve the desired maximum throughput of raw material and extreme training of one or several hot spots even the permanent limitation of the load below the desired range, in order to avoid irreversible catalyst damage.
- multi-layer catalysts which are arranged in layers in the catalyst bed, in particular with superimposed catalyst layers, and where the least active catalyst is usually closest to the gas inlet and thus comes first in contact with the starting mixture.
- Too high an activity of this first catalyst layer would lead to an uncontrolled rise in the hot-spot temperature, which can lead to the selectivity losses already mentioned or to irreversible damage to the catalyst.
- the catalyst layer (s) following in the direction of the gas outlet generally has an increased activity in order, on the one hand, to ensure complete conversion of the starting material and, on the other hand, to reduce the content of undesired by-products as far as possible.
- US-A 4,356,112 describes a catalyst with two layers of different activity for the production of phthalic anhydride, wherein the antimony trioxide (Sb 2 O 3) content is 0.5 to 10 wt .-%.
- the best yields are achieved with an antimony oxide content of 2 wt .-% and a vanadium pentoxide content of 3 wt .-% of the active composition. It is disclosed that antimony oxide improves the heat resistance and selectivity of the catalysts.
- EP-A-0 522 871 describes a catalyst for the production of phthalic anhydride with two different catalyst layers by gas-phase oxidation, using a pentavalent antimony compound as antimony source.
- the disclosed catalysts have a Sb 2 O 5 content of 2.5 wt .-% and a Sb 2 O 3 content of 2.0 wt .-% and have a V 2 O 5 : Sb 2 ⁇ 3 ratio of 2: 2.0 or a V 2 0 5 : Sb 2 0 5 - ratio of 2: 2.5.
- DE 103 23 461 A1 describes a process for the preparation of phthalic anhydride, wherein a catalyst with two different layers with increasing activity from the gas inlet to the gas outlet is used and at the same time the ratio of V 2 O 5 to Sb 2 O 3 in the first layer at 3, 5: 1 to 5: 1.
- DE 198 39 001 describes a shell catalyst for the gas phase oxidation of hydrocarbons with a total content of up to 10 wt .-% Sb 2 O 3 , in which the catalytically active layers are applied in two or more layers on the inert support and wherein the inner layer or inner layers have a total content of antimony trioxide of up to 15 wt .-% and the outer layer has a reduced by 50 to 100% Sb 2 O 3 content.
- the proportion of active mass of the inner layer or inner layers is 10 to 90% of the total active mass.
- EP 1 084 115 B1 describes a process for the oxidation of o-xylene and / or naphthalene with at least three layers arranged one above the other, in which the catalyst activity increases continuously from the gas inlet side to the gas outlet side.
- the content of active mass increases from the reactor inlet to the reactor outlet and the alkali metal content optionally additionally decreases from the gas inlet to the gas outlet.
- DE 102 378 18 describes a catalyst for the preparation of phthalic anhydride with at least three successive layers, the activity of the layers continuously increasing from the gas inlet to the gas outlet.
- the control of the increase in activity is achieved here by using TiO 2 with different BET surface area.
- the BET surface area of the titanium dioxide used is lowest in the gas inlet layer and highest in the last gas outlet layer.
- EP 1 063 222 describes a process for the preparation of phthalic anhydride, wherein the catalyst consists of three or more different catalyst layers.
- the reaction may be carried out in one or more consecutive fixed bed reactors.
- the conversion of the starting material used is 30 to 70% after the first layer and at least 70% after the second layer.
- Phthalic anhydride in which the catalyst activity increases in the flow direction and at the same time decreases the active mass of the various layers from the gas inlet to the gas outlet.
- DE 103 23 817 A1 describes a catalyst for the preparation of phthalic anhydride with at least three different layers, wherein the activity of the layers increases from the gas inlet to the gas outlet and only the last layer closest to the gas outlet contains phosphorus and more than 10% by weight. % V 2 O 5 .
- WO 2006/092304 describes the use of a multilayer catalyst for producing phthalic anhydride with at least three catalyst layers, wherein the first layer located to the gas inlet side has a higher activity than the subsequent second layer.
- WO 2006/092305 describes a process for the preparation of phthalic anhydride with an initial catalyst consisting of at least two catalyst layers of different activity, wherein a portion of the first gas inlet layer is replaced by a higher activity catalyst.
- the content of at least one of these elements in the catalytically active composition of at least one upstream catalyst layer over the content of the same element in the catalytically active mass of the hot-spot catalyst layer reduced.
- the antimony especially antimony oxide content of the catalytically active material in at least one of the hot-spot catalyst layers upstream catalyst alga against the antimony, especially antimony oxide content of the catalytically active material in the hot-spot catalyst layer by a predetermined Value reduced.
- this antimony content is reduced by 20 to 100 wt .-%, most preferably reduced by 40 to 100 wt .-%.
- the idea of the invention will be described below by way of example in conjunction with a reduced antimony content. Analogously, however, the following also applies to bismuth or niobium, without explicitly mentioning this again. The same applies to the claims.
- the general inventive concept of claim 1 with the term "antimony” or "antimony content” was further developed in the subclaims merely for reasons of clarity and clarity, although antimony is the preferred element of the three mentioned elements antimony, bismuth and niobium.
- antimony or “antimony content” is thus hereby expressly synonymous with “bismuth” or “bismuth content” on the one hand and “niobium” or “niobium content” on the other hand, that is quasi as a generic term for all three elements antimony, bismuth and niobium be valid.
- hotspot refers to the largest locally measured temperature in the entire catalyst bed.
- this largest hot spot which is located in a fresh catalyst usually in a range of 50 to 120 cm deep in the catalyst bed (measured from the gas inlet in the direction of gas outlet), quite a few smaller side hot spots in further catalyst layers occur.
- the location of the largest hotspot at optimum operating temperature is preferably used in the present invention in which the catalyst achieves its highest selectivity and produces a sufficiently good product quality, preferably after the start-up (break-in period) of the catalyst about three months after the first start up of the catalyst.
- a catalyst layer in a broader sense is understood to mean a reaction region which is distinguished by a substantially uniform catalyst composition or, in the case of a mixture of several catalysts, by a uniform mixture composition in this range.
- the transitions between the individual catalyst reaction areas can be flowing.
- the different Catalysts thus formed by catalyst reaction areas, which have a more or less flowing transition to each other.
- the different catalyst layers are formed in the conventional sense by individual so-called catalyst rings, in which the catalytically active composition is applied to an inert, non-porous carrier ring, for example.
- the catalytic mass of one or more catalyst layers can be applied in two or more layers to a support, in particular a ceramic support.
- the antimony content of at least one coating layer of at least one upstream catalyst layer is preferably reduced by a predetermined value, in particular by 20 to 100%, compared to the antimony content of the coating layer with the highest antimony content in the hot-spot catalyst layer.
- the hot-spot catalyst layer on at least two coating layers wherein at least one of the coating layers by a predetermined value, preferably by 20 to 100%, reduced antimony content of the catalytically active material compared to that coating layer having the highest antimony content.
- the or at least one layer (s) applied to the inner layer can have an antimony content of the catalytically active composition which is reduced by a predetermined value, in particular by 20 to 100%, compared with the inner layer.
- a predetermined value in particular by 20 to 100%
- At least one upstream catalyst layer can be applied in several layers to the carrier rings, for example, and any of the layers, in particular the outer layer, have a lower content of antimony than the antimony content of the hot-spot catalyst layer in a single-layer structure the hot-spot catalyst layer; whereas in the case of an inhomogeneous composition in which the hot-spot catalyst layer itself has multiple layers, any layer, most preferably an outer coating layer, of an upstream catalyst layer may have a lower antimony content than the highest antimony content coating layer in the hot spot catalyst layer.
- a mixture of at least two different catalysts in particular with regard to the composition of the catalytically active composition, can also be used in the hot-spot catalyst layer.
- the advantages according to the invention are achieved when the antimony content, in particular the antimony oxide content, of the catalytically active composition of at least one catalyst of the hot-spot catalyst layer is reduced by a predetermined value, preferably by 20 to 100%, compared to the antimony content of the catalytically active material of the catalyst having the highest antimony content in the hot-spot catalyst layer.
- the antimony content, in particular the antimony oxide content, the catalytically active composition of at least one catalyst of this considered, upstream and a catalyst mixture containing catalyst layer is reduced by a predetermined value, preferably by 20 to 100%, compared to the antimony content of the catalytically active material of that catalyst having the highest antimony content in the hot-spot catalyst layer.
- this one catalyst layer has an antimony content of the catalytically active composition, which is reduced by a predetermined value compared to the antimony content of the catalytically active material of the hot-spot catalyst layer.
- the antimony content of the catalytically active material of at least one of the upstream catalyst layers is reduced by a predetermined value compared with the antimony content of the catalytically active material of the hot-spot catalyst layer.
- this single catalyst layer has an active material content which is less than or equal to the active material content of the hot-spot catalyst layer.
- at least one of the reduced antimony content having upstream catalyst layers having an active material content which is less than or equal to the active material content of the hot-spot catalyst layer.
- the selectivity can be significantly increased if the catalyst layers having a reduced antimony content have a vanadium oxide content of from 0 to 9% by weight, most preferably from 3 to 6% by weight.
- the selectivity of the catalyst can be further increased by the fact that at least one of the reduced antimony content having upstream catalyst layers has a phosphorus content of 0 to 0.3 wt .-%, most preferably from 0 to 0.15 wt .-%, based on having the catalytically active composition of this catalyst layer.
- first catalyst layer is always the catalyst layer located directly toward the gas inlet.
- the following catalyst layer which adjoins the first catalyst layer in the direction of the gas outlet, is referred to as the second catalyst layer and the subsequent catalyst layer as the third catalyst layer.
- the adjoining catalyst layers are referred to as the fourth, fifth and optionally as the sixth catalyst layer.
- the sixth and last catalyst layer is directly at the gas outlet.
- active composition catalytically active compound
- the second catalyst layer located downstream and closer to the gas outlet is immediately adjacent to the first catalyst layer located at the gas inlet and has a correspondingly higher antimony content in the active composition.
- this second catalyst layer is the catalyst layer with the highest hot spot.
- the subsequent third catalyst layer which is located further downstream and closest to the gas outlet, usually has a higher activity than the second catalyst layer.
- the antimony content of this last catalyst layer may be the same size, smaller or larger than the antimony content of the second layer.
- the possibilities of setting the activity of the individual catalyst layers are familiar to the person skilled in the art, with various measures being available.
- the increase in activity of this last catalyst layer is preferred by a reduced content G achieved at activity-damping promoters and / or a higher BET surface area of the titanium dioxide used and / or by an increased addition of activity-increasing promoters and / or by a higher content of active material.
- a catalyst layer or two catalyst layers with an antimony content reduced by 20 to 100% can preferably be in the direction of the gas inlet before the layer with the highest hot spot. If only one layer with reduced antimony content is present in front of the catalyst layer with the highest hotspot, then this catalyst layer has an equal or, preferably, a smaller active mass, than the catalyst layer with the highest hotspot, regardless of its activity.
- the catalyst layer with the highest hot spot is followed by two further catalyst layers in the direction of the gas outlet, the activity of these catalyst layers preferably increasing in the direction of gas outlet.
- the antimony content may be uneven. It is preferred if one of the catalyst layers has a reduced content compared to the catalyst layer with the highest hot spot and is particularly preferred when both catalyst layers have a reduced Sb content.
- the highest hot spot catalyst layer is the third catalyst layer to which a fourth catalyst layer closest to the gas exit is connected.
- a catalyst with a total of five layers there are several different options in which one, two or three catalyst layers of the catalyst layer with the highest hot spot can be preceded in the direction of gas inlet.
- all three upstream catalyst layers have a reduced Sb content and two of the upstream catalyst layers (with the largest fill levels) have a reduced active mass.
- particular preference is given to catalysts in which all three upstream catalyst layers have a reduced Sb content of active mass and at the same time also a reduced active mass.
- Hot spot in the direction of gas outlet depending on the number of upstream catalyst layers one, two or three catalyst layers downstream towards the gas outlet.
- the downstream Catalysts usually have in the direction of gas leakage an increasing activity, which can be achieved as described by various measures.
- the catalyst layer closest to the gas outlet is referred to herein as the fifth catalyst layer and typically has the highest activity of all layers.
- the activity increases from the second catalyst layer to the fifth catalyst layer in the direction of gas outlet.
- the activity of the upstream first catalyst layer may be greater than or less than or equal to the activity of the second catalyst layer with the highest hot spot.
- two upstream catalyst layers with reduced antimony content and reduced active mass are provided in a catalyst with a total of five catalyst layers.
- the first catalyst layer located at the gas inlet has the lowest activity of all catalyst layers and at the same time has a reduced Sb content of 20 to 100% compared to the catalyst layer with the highest hot spot.
- the second upstream catalyst layer preferably has a higher activity than the first catalyst layer and has over the catalyst layer with the highest hot spot a 20 to 100% reduced Sb content and an equal or more preferably a lower active mass.
- the activity of the two catalyst layers following the catalyst layer with the highest hot spot preferably increases in the direction of gas exit. It is particularly preferred if the last catalyst layer lying in the direction of the gas outlet has a very high activity.
- up to four catalyst layers can be preceded by the catalyst layer with the highest hot spot.
- the composition and activity of the upstream catalyst layers may well be different.
- This layer preferably has the highest filling level of all the layers upstream.
- this upstream catalyst layer has an Sb content reduced by 20 to 100% and an active substance of the same size as the catalyst layer with the highest hotspot.
- the active mass is smaller than the active mass of the catalyst layer with the highest hot spot.
- the highest hotspot layer in this catalyst is the second catalyst layer as defined above.
- the activity of the four subsequent catalyst layers increases gradually towards the gas outlet.
- the downstream catalyst layers differ in their chemical composition and / or their physical properties and / or in the content of active mass.
- two catalyst layers with a reduced antimony content and reduced active mass are preceded by a catalyst with a total of six catalyst layers of the catalyst layer with the highest hot spot.
- the first catalyst layer lying directly on the gas inlet has the lowest activity of all catalyst layers and preferably also has the lowest content of active material.
- the second catalyst layer has a higher activity than the first catalyst layer and preferably has a higher active mass than the first catalyst layer.
- the antimony content in relation to the catalyst layer with the highest hotspot is preferably reduced by 20 to 100% and the active mass is the same size or preferably smaller than the active mass of the catalyst layer with the highest hotspot.
- the activity of this second catalyst layer may be smaller or preferably greater than that of the subsequent catalyst layer with the highest hot spot.
- the activity of the three catalyst outlet situated in the direction of the gas outlet and after the location with the highest hot spot increases gradually in the direction of gas outlet.
- the last catalyst layer has a particularly high activity and a lower content of active material optionally as the catalyst layer with the highest hot spot and / or the immediately upstream upstream catalyst layer.
- the filling level of the first catalyst inlet located upstream of the catalyst inlet and the highest hot spot upstream of the catalyst layer is 10 to 90 cm and preferably 20 to 70 cm. If only one catalyst layer in the direction of gas inlet in front of the catalyst layer with the highest local temperature maximum, the filling height of this catalyst layer is particularly advantageous 30 to 60 cm.
- this upstream catalyst layer is required in order to achieve optimum selectivity and stability of the catalyst.
- Fill level of this upstream catalyst layer can be selected. Here it is priority
- two catalyst beds are used in front of the catalyst layer having the highest local temperature maximum, wherein the total fill level of the two upstream catalyst layers is preferably between 15 and 90 cm and more preferably between 30 to 70 cm.
- the filling level of the first closest to the gas inlet catalyst layer is 5 to 25 cm and the lowest
- Catalyst layer selected a filling height of 5 to 15 cm.
- this first inactive serves
- the filling level of the second upstream catalyst layer is 20 to 60 cm and in a particularly preferred embodiment 30 to 50 cm.
- the filling level of the individual catalyst layers depends decisively on the total filling level of the reaction tubes, which in turn is determined by the tube length. According to the state of the art, today generally total filling heights of 2.80 to 3.40 m are selected.
- the catalysts with a total of four catalyst layers have a filling height of 30 to 60 cm for the first catalyst layer, 80 to 150 cm for the second catalyst layer (catalyst layer with highest hot spot), 40 to 100 cm for third catalyst layer and 40 bis 100 cm for the fourth catalyst layer.
- a filling height of 30 to 50 cm for the first catalyst layer, 90 to 130 cm for the second catalyst layer, 50 to 80 cm for the third catalyst layer and 50 to 80 cm for the fourth catalyst layer.
- the catalysts preferably have a filling level of 5 to 15 for the first catalyst layer, 20 to 50 cm for the second catalyst layer, 80 to 130 cm for the third catalyst layer (hot spot), 50 to 100 cm for the fourth catalyst layer and 50 to 100 cm for the fifth catalyst layer, depending on the available Automatchelliere.
- the first catalyst layer has a filling height of 5 to 15 cm
- the second catalyst layer a filling height of 30 to 50 cm
- the third catalyst layer (catalyst bed with the highest hot spot) a filling height of 80 to 130 cm
- the fourth catalyst layer has a filling height of 40 to 60 cm
- the fifth catalyst layer has a filling height of 60 to 80 cm
- the sixth catalyst layer has a filling height of 50 to 70 cm.
- the activity of the catalyst layers in the direction of gas entry may be smaller and / or greater than the activity of the catalyst layer having the largest local temperature maximum.
- the activity of the catalyst layer or the catalyst layers which lies or lie after the bed with the highest temperature maximum, or usually has a greater activity than the catalyst layer having the highest temperature maximum, the activity usually from catalyst layer to catalyst layer in the direction of gas outlet increases.
- the first, closest to the gas inlet catalyst layer has a particularly low activity in order to increase the reliability of the process for the production of phthalic anhydride. It is well known to those skilled in the art that in phthalic anhydride technical installations explosions often occur at the reactor inlet, in particular when the reactors are operated at high loadings. One reason for this is often the impact of incompletely evaporated raw material drops on the Beginning of the catalyst bed.
- the activity of the catalyst layers is set as follows:
- I AK (LI) «AK (L2) ⁇ / /> AK (L3) ⁇ AK (L4) ⁇ AK (L5) ⁇ AK (L6)
- the activity of a catalyst layer can be reduced by various measures known to the person skilled in the art by:
- counteracting measures are used for activity adjustment and selectivity adjustment, depending on the position of the respective catalyst layer in the catalyst bed and the task of the respective catalyst layer in the overall play of the various catalyst layers.
- the active masses of the individual catalyst layers preferably have a different chemical composition and / or different physical properties. In this case, individual catalyst layers can differ in particular only by a different Gehait of active mass.
- the content of active composition is distributed over the individual layers as follows:
- AM (LI) «AM (L2) ⁇ AM (L3) ⁇ AM (L4) ⁇ / AM (L5)> AM (L6)
- the grading of the active composition in a catalyst with a total of six catalyst layers is disclosed here:
- the first catalyst layer has a very low active composition content in order to avoid ignition of the mixture by locally very high raw material concentrations in the event of incomplete evaporation.
- the second catalyst layer has a significantly higher active mass content in comparison to the first catalyst layer and at the same time particularly preferably a lower active material content than the catalyst layer with the highest hot spot.
- the catalyst layer with the highest hotspot preferably has an average active material content, on the one hand to ensure a moderate hot-spot guidance even at high loadings and on the other hand to convert most of the raw material to not in the subsequent downstream active catalyst layers not one totally oxidize considerable part of the raw material.
- the catalyst layers immediately following the catalyst layer with the largest hot spot have a higher active material content and a higher activity than the catalyst layer with the highest hot spot in order to complete the conversion of the starting material to the largest part.
- the active material content of these two catalyst layers is preferably approximately the same, while the activity of the catalyst layer located closer to the hot-spot catalyst layer is smaller than that of the subsequent catalyst layer.
- This increase in activity can be achieved, for example, by other measures known to the person skilled in the art, preferably by a reduction of the cesium content.
- the last, located to the gas outlet sixth catalyst layer has a very high activity in order to keep the by-product level as low as possible.
- this last layer has a lower active material content than the catalyst layer with the highest hot spot and / or the immediately preceding catalyst layer. It has been found that with high activity and at the same time high active mass of the catalyst layer located at the gas outlet, a drop in selectivity of the overall catalyst is caused.
- the first catalyst layer has an active material content of 3 to 10 wt .-% and particularly preferably from 3 to 6 wt .-%
- the second catalyst layer preferably has an active composition content of 4 to 11 wt .-%, and particularly preferably from 5 to 9 wt .-%.
- the catalyst layer with the highest hotspot it is preferred for the catalyst layer with the highest hotspot to have an active material content of from 5 to 12% by weight and more preferably from 6 to 11% by weight and in particular from 7 to 9% by weight .
- the fourth and fifth catalyst layers have an active composition content of from 5 to 15% by weight and in particular from 6 to 12% by weight and more preferably from 7 to 11% by weight.
- the last and closest to the gas outlet catalyst layer has in a preferred embodiment, an active material content of 4 to 11 wt .-% and particularly preferably from 5 to 10 wt .-%.
- the active material content of the catalyst layer of the highest hot spot to catalyst layer at the gas outlet is consistent and / or decreasing and / or increasing, since the activity design in particular the catalyst layers according to Catalyst situation with the largest hot spot can be achieved in many ways, without having to accept significant loss of selectivity.
- the active masses of the individual catalyst layers may, for example, have a different chemical composition.
- the individual catalyst layers, in particular the first and second upstream Katalysatoriage differ only by a different content of active mass.
- the individual catalyst layers contain as main constituents in each case at least titanium dioxide in the anatase modification and a vanadium compound in the active composition.
- an antimony compound is preferably used, preferably antimony trioxide for improving the thermal stability and service life of the catalysts.
- a cesium compound is used in the catalysts according to the invention as a selectivity-increasing and activity-damping component.
- the antimony content of the first two catalyst layers is in a range from 0 to 2.5% by weight, in particular 0 to 1.5% by weight and more preferably 0 to 1% by weight. Calculated as Sb 2 O 3 , this content is preferably reduced by 20 to 100% compared to the antimony content of the active material of the catalyst layer with the highest hot spot.
- the antimony content of the catalyst layer with the highest hot spot is in a preferred embodiment of the invention in a range of 0 to 5 wt .-%, in particular 1 to 4 wt .-% and particularly preferably from 1, 5 to 3.5 wt .-% (calculated as Sb 2 O 3 ).
- the antimony content in the catalyst layers which lie after the catalyst layer with the highest hotspot in the direction of gas exit, initially increases further and is preferably in a range from 0 to 5% by weight and particularly preferably between 1 , 5 to 4 wt .-% (calculated as Sb 2 O 3 ).
- the last catalyst layer closest to the gas outlet has a reduced antimony content compared with the previous catalyst layers, which is preferably 0 to 4% by weight and more preferably 0 to 3.0% by weight.
- the catalyst according to the invention preferably has a structured grading with regard to the antimony content of the catalytically active composition in order to adequately fulfill the different tasks of the individual catalyst layers.
- the catalyst layers following the hot-spot catalyst layer also contain antimony oxide. If only one catalyst layer in the direction of the gas outlet after the layer with the highest hot spot, then preferably the antimony content is equal to or more preferably smaller than the antimony content of the catalyst layer with the highest hot spot.
- the antimony content advantageously increases continuously from the first catalyst layer to the fourth catalyst layer and is then reduced again in the last catalyst layer lying to the gas outlet ,
- the antimony content in the first two catalyst layers is identical and increases in stages from the second to the fifth catalyst layer and then decreases again in the last catalyst layer.
- the different antimony content is used essentially for the selectivity control of the various catalyst layers and not for controlling activity, since antimony oxide has only a small influence on the activity of the catalyst.
- all catalyst layers contain 0 to 5 wt .-%, particularly preferably 0 to 3.5 wt .-% antimony oxide.
- those catalysts are also covered by the invention in which the antimony content in the hot-spot catalyst layer is greatest and the downstream catalyst layers partly have a smaller and in some cases a higher antimony content in the active composition than the hot-spot catalyst layer.
- antimony sources are advantageously antimony pentoxide and especially antimony trioxide.
- the vanadium content in the first two upstream catalyst layers in a range of 2.5 to 9 wt .-% and more preferably in a range of 3 to 6 wt .-%. It has also been found that according to a preferred embodiment of the invention, the vanadium content advantageously increases from catalyst layer to catalyst layer from the gas inlet in the direction of the gas outlet.
- the content of vanadium pentoxide is advantageously in the catalyst layer with the highest hot spot and the two downstream catalyst layers in a range of 3.5 to 12 wt .-% and particularly advantageously at 4 to 9 wt .-%.
- the vanadium content is advantageously in a range of 7 to 25 wt .-% and particularly advantageously in a range of 7 to 22 wt .-%, in particular 8 to 17 wt .-%.
- the vanadium source is a series of further compounds, such as vanadium oxalate, vanadium halides, metavanadic acid, pyrovanadic acid and vanadium carboxylates, such as vanadium formate, vanadium salicylate or vanadium tartrate.
- vanadium oxalate is preferably used to prepare the catalysts.
- all catalyst layers of the catalyst according to the invention also contain cesium and / or another element of the first main group in the active composition.
- the cesium content of the upstream or downstream catalyst layers increases to the catalyst layer with the highest hot spot and reaches its maximum in this catalyst layer, and then gradually decrease again in the downstream catalyst layers.
- the cesium content in the present invention is preferably in a range of 0 to 0.7% by weight, and more preferably 0 to 0.5% by weight.
- the cesium content in the upstream catalyst layers is in a range of 0.1 to 0.3 wt .-%.
- no phosphorus compound is used in the preparation of the active material, especially in the upstream layers.
- the phosphorus content gradually increases from the catalyst layer with the highest hot spot downstream to the last catalyst layer, wherein it is particularly preferred that the phosphorus content in the last layer is significantly increased compared to the previous upstream catalyst layer.
- the catalyst layer with the highest hot spot contains bismuth vanadate (BiVO 4 ) in the active composition.
- the preferred content of bismuth vanadate in the active composition in an embodiment according to the invention is in a range from 0 to 4% by weight and in particular in the range from 0 to 2% by weight and particularly preferably from 0 to 1% by weight.
- the use of a bismuth compound in the active composition of catalysts for phthalic anhydride preparation has long been known (EP 0 180 335 A1). In this case, however, preferably bismuth compounds are used, which can be converted during calcination in the corresponding oxides such as Bi 2 O 3 .
- At least one of the catalyst layers in particular in the catalyst layers up to and including the hot-spot catalyst layer, comprises silver or a silver component, preferably in the form of mixed oxides of silver, most preferably in the form of silver vanadate and / or silver molybdate and / or silver tungstate.
- silver vanadate AgVO 3
- one or more or all of the catalyst layers mentioned have a silver vandate content of from 0.01 to 4% by weight, in particular from 0.03 to 2.0% by weight and particularly preferably from 0.05 to 1, 0 wt .-% on.
- the catalyst layers preferably contain at least titanium dioxide and a vanadium compound in the active composition.
- the active composition contains at least one more alkali metal, particularly preferably cesium as a selectivity-enhancing and activity-damping additive.
- the silver is attributed a selectivity-enhancing role, namely by the suppression of the total oxidation of o-xylene and / or naphthalene to CO and CO 2 .
- Catalysts can be achieved in terms of selectivity, if the invention
- Mixed oxide silver metavanadate AgVO 3 which is not a so-called silver bronze, is used as an additive in catalyst preparation.
- the active composition preferably at least still contain titanium dioxide and a vanadium compound and preferably also cesium and / or another element of the first main group and in the case of the catalyst layer with the highest hot spot additionally an antimony and / or bismuth and / or Phosphorveruindung.
- composition ranges of the active masses in the individual catalyst layers are preferably in the following ranges.
- a particularly preferred catalyst according to the invention with a total of six catalyst layers is listed, in which the third catalyst layer is the catalyst layer with the highest hot spot:
- the remainder of the active composition consists predominantly of titanium dioxide in the anatase modification.
- the remainder of the active composition consists of at least 90% by weight of titanium dioxide and in particular of 95% by weight, particularly preferably 100% by weight, of titanium dioxide.
- alkali and alkaline earth metals include compounds of alkali and alkaline earth metals, thallium, antimony, bismuth, aluminum, zirconium iron, nickel, cobalt, copper, manganese, tin, silver, chromium, molybdenum, tungsten, iridium, tantalum, niobium, arsenic, cerium and phosphorus ,
- the alkali metal compounds act as the activity-reducing and selectivity-increasing promoters, while phosphorus compounds increase the activity but have a negative influence on the selectivity.
- compounds such as silicon carbide and other carbides and nitrides are suitable as additives for the active mass in the hot-spot region of the catalysts in order to achieve a better control of the reaction, especially at high loadings.
- a structuring of the average surface of the titanium dioxide used in the various catalyst layers is also used in order to adjust the activity of the respective catalyst layers advantageous.
- an equal or larger mean BET surface area of the titanium dioxide of the at least one upstream catalyst layer is preferred in comparison to the catalyst layer with the largest hot spot.
- the mean surface in the downstream catalyst layers initially decreases again, and then increases again in the last catalyst layer. Accordingly, according to this aspect of the invention, the activity structuring of the catalyst is not achieved exclusively by using titanium dioxides having defined properties, but rather by a combination of partly countercurrent measures known to the person skilled in the art.
- different grades of titanium dioxide having different BET surface areas are used to set the desired BET mean surface area for the respective catalyst layers.
- An essential component of the catalyst according to the invention is titanium dioxide in the
- titanium dioxides with a different specification with regard to surface area, particle size and particle structure than described here can also be used in the catalyst according to the invention.
- one or more types of titanium dioxide with different surface areas and particle sizes and porosities can be used in certain or all catalyst layers.
- the mean BET surface area of the titanium dioxide of the third catalyst layer in which the highest hot spot is located is preferably the same size and particularly preferably less than the mean surface area of the second catalyst layer.
- the mean BET surface area of the titanium dioxide of the central catalyst layers downstream of the catalyst layer with the highest hot spot is preferably the same or more preferably smaller than the mean BET surface area of the titanium dioxide of the catalyst layer having the highest hot-spot. spot.
- the mean BET surface area of the titanium dioxide of the last catalyst layer closest to the gas outlet is higher than the mean BET surface area of the titanium dioxide of the fourth and fifth catalyst layers, and preferably equal to or more preferably greater than the mean BET surface area of the titanium dioxide all other catalyst layers.
- the following distribution of the BET surface area is selected for a catalyst having a total of five catalyst layers and two upstream catalyst layers:
- Multilayer catalysts can more than two catalyst layers with different
- composition of the catalyst layer with the highest hot spot Preceding the composition of the catalyst layer with the highest hot spot and / or be downstream of more than three catalyst layers of the catalyst layer with the highest hot spot.
- the catalysts used in the invention are generally shell catalysts in which the catalytically active material in one or more Layers are cupped on an inert carrier.
- the layer thickness of the catalytically active composition is generally 0.02 to 0.4 mm, more preferably 0.05 to 0.15 mm. In general, however, at least most of the catalyst layers, and preferably the catalyst layers following downstream of the highest Hot Sport catalyst layer, have a homogeneous chemical composition of the active material.
- the catalytically active material is usually on a generally inert under reaction conditions, non-porous support material such as quartz, porcelain, magnesium oxide, tin oxide, silicon carbide, rutile, alumina (Al2O3), aluminum silicate, magnesium silicate (steatite), zirconium silicate or mixtures thereof Carrier materials applied.
- non-porous support material such as quartz, porcelain, magnesium oxide, tin oxide, silicon carbide, rutile, alumina (Al2O3), aluminum silicate, magnesium silicate (steatite), zirconium silicate or mixtures thereof Carrier materials applied.
- non-porous carrier of the active mass balls or in particular rings of steatite have proven particularly useful.
- steatite rings are used with an outer diameter of 5 to 9 mm, a length of 4 to 8 mm and an inner diameter of 3 to 7 mm.
- aqueous or organic solvent-containing solution or suspension of the active composition components and / or their precursor compounds is preferably sprayed onto the support material in a heated drum at elevated temperature until the desired active mass fraction of the total catalyst weight is reached.
- the coating of the inert support can also be carried out in the fluidized bed process (DE 2106796), since the inside of hollow cylinders is also uniformly coated here.
- the art has been used to advantageously add so-called organic binders, preferably copolymers, to the solution or suspension with the catalytically active constituents in the form of an aqueous dispersion.
- the binder is added in amounts of about 5 to 20 wt .-% based on the solids content of the catalytically active composition.
- the coating temperatures are advantageously in a range from 50 to 450 ° C. and particularly advantageously in a range from 50 to 200 ° C.
- the binder applied to the support material together with the active ingredients is decomposed after the catalyst has been charged during the heating of the reactor and completely removed from the active mass.
- the binder addition has the additional advantage that the active material firmly adheres to the carrier and there is no loss of active material by abrasion during transport of the catalyst and when the reactor is charged.
- the catalysts thus prepared are preferably used for the gas phase oxidation of o-xylene or naphthalene or o-xylene / naphthalene mixtures to phthalic anhydride.
- the catalysts to be used according to the invention are filled into the reaction tubes, which are advantageously thermostated from the outside, for example by means of a salt bath, to the reaction temperature.
- the reaction gas at temperatures of generally from 300 0 C to 45O 0 C, preferably at 320 ° C to 400 0 C and more preferably at 330 ° C to 390 0 C, at an overpressure of 0.1 to 2.5 bar, preferably from 0.3 to 1, 5 bar at a space velocity of generally 750 to 5000 1 / h passed.
- the reaction gas supplied to the catalyst is generally mixed by mixing a molecular oxygen-containing gas, preferably air, which may contain, besides oxygen, still suitable reaction moderators and / or diluents such as steam, carbon dioxide, sulfur dioxide and / or nitrogen with the aromatic to be oxidized Hydrocarbon generated, wherein the molecular oxygen-containing gas is generally 1 to 100 vol .-%, preferably 2 to 50 vol .-% and particularly preferably 10 to 30 vol .-% oxygen, 0 to 30 vol .-% and preferably 0 to 10% by volume of water vapor, and 0 to 50% by volume, preferably 0 to 1% by volume of carbon dioxide, may contain nitrogen.
- the gas containing the molecular oxygen is generally charged with 25 to 140 grams per Nm 3 of the hydrocarbon to be oxidized.
- the catalysts according to the invention are temperature-treated or calcined in the customary manner before use. It has proved to be advantageous if the catalyst for at least 6 h at least 390 0 C, especially between 12 and 24 h at 400 0 C to 430 0 C in a molecular oxygen-containing gas, in particular air is conditioned. It is advantageous if the amount of air used in a range of 0.05 to 1 Nm 3 per tube and hour.
- Catalyst activity of the catalyst according to the invention are familiar to the person skilled in the art.
- the measurement of the activity of a catalyst must be carried out under reasonable operating conditions (Salt bath temperature) and can be used for comparison purposes only after the catalyst to be considered has reached its final maximum activity.
- phthalic anhydride of o-xylene and / or naphthalene can be prepared with high selectivities and good qualities at the same time high loading.
- the catalysts of the invention are stable and allow for an economical, industrial production of phthalic anhydride over a long time.
- the various components of the active composition and / or their course compounds are added successively as solutions and / or as a powder in deionized water and the resulting suspension is stirred advantageously for at least 12 h.
- Titanium dioxide, vanadium oxalate, cesium sulfate, ammonium dihydrogen phosphate, antimony trioxide, bismuth vanadate and silver vanadate are advantageously used as sources for the components containing the catalyst according to the invention.
- an organic binder in the form of an aqueous dispersion of a vinyl acetate copolymer is added to the aqueous suspension and the total of about 20 to 25% suspension is stirred for a further 30 minutes.
- aqueous suspension which contains the active substances and / or their precursor compounds and the organic binder is applied by spraying to the inert support (steatite rings with 7x7x4 mm or 8x6x5 mm dimension) to a certain amount of the adhesive-containing suspension is applied to the rings, so that after the calcination, the stated in the examples active mass content.
- the active material content or content in each case refers to the proportion of the catalytically active composition in the total weight of the catalyst, including the support in the respective catalyst layer, measured after four hours of calcination at 400 ° C.
- the details of the BET surface areas of the catalysts or catalyst layers relate to the average BET surface area of the titanium dioxide materials used (dried in vacuo at 150 ° C.). It is known to the person skilled in the art that the BET surface area of a catalyst is essentially determined by the BET surface area of the TiO.sub.2 used and this is modified to some extent by the addition of further catalytically active components, depending on the amount and surface area of the additional components.
- the stated content of phosphorus in the examples refers to the amount of a phosphorus component added in the production of the suspension. It is known to those skilled in the art that the actual content of phosphorus in the active composition may vary depending on how much the TiO 2 used is contaminated with phosphorus.
- reaction gas leaving the reaction tube is passed through an oil-cooled condenser in which, in particular, the phthalic anhydride formed is largely completely separated and by-products such as benzoic acid, maleic anhydride and phthalide only partially precipitate.
- the raw PSA deposited in the condensates is melted by means of hot oil, collected, weighed and then the content of phthalic anhydride is determined by GC analysis.
- an average raw PSA yield (based on 100% o-xylene purity) was achieved after the run-in phase of 115.0% by weight, and the phthalide content in the crude PSA was 0.03% by weight.
- this catalyst system is a multi-layer system with four different layers.
- the catalyst system can also be considered as a fictitious five-layer system, wherein the first lying at the gas inlet layer is divided into two layers of identical composition
- an average raw PSA yield (based on 100% o-xylene purity) was achieved after the run-in phase of 114.0% by weight, and the phthalide content in the crude PSA was 0.06% by weight.
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Abstract
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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EP09707013A EP2247384A2 (de) | 2008-02-01 | 2009-01-28 | Katalysator für die katalytische gasphasenoxidation von aromatischen kohlenwasserstoffen zu aldehyden, carbonsäuren und/oder carbonsäureanhydriden, insbesondere zu phthalsäureanhydrid |
CN200980103798.XA CN101939104B (zh) | 2008-02-01 | 2009-01-28 | 将芳族烃催化气相氧化成醛、羧酸和/或羧酸酐,特别是邻苯二甲酸酐用的催化剂 |
BRPI0905796A BRPI0905796A2 (pt) | 2008-02-01 | 2009-01-28 | catalisador para oxidação catalítica de fase gasosa de hidrocarbonetos aromáticos para formar aldeídos, ácidos carboxílicos e/ou anidridos de ácido carboxílico, especialmente para formar anidrido de ácido ftálico |
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DE102008007450.0 | 2008-02-01 | ||
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DE102008011011.6 | 2008-02-25 | ||
DE102008011011A DE102008011011A1 (de) | 2008-02-01 | 2008-02-25 | Katalysator für die katalytische Gasphasenoxidation von aromatischen Kohlenwasserstoffen zu Aldehyden, Carbonsäuren und/oder Carbonsäureanhydriden, insbesondere zu Phthalsäureanhydrid |
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KR (1) | KR101620949B1 (de) |
CN (1) | CN101939104B (de) |
BR (1) | BRPI0905796A2 (de) |
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Cited By (2)
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WO2010022830A2 (de) * | 2008-08-29 | 2010-03-04 | Josef Breimair | Katalysator für die katalytische gasphasenoxidation von aromatischen kohlenwasserstoffen zu aldehyden, carbonsäuren und/oder carbonsäureanhydriden, insbesondere zu phthalsäurenanhydrid, sowie verfahren zur herstellung eines solchen katalysators |
WO2011032658A1 (de) * | 2009-09-17 | 2011-03-24 | Süd-Chemie AG | Verfahren zur herstellung einer katalysatoranordnung für die herstellung von phthalsäureanhydrid |
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DE102010012090A1 (de) * | 2010-03-19 | 2011-11-17 | Süd-Chemie AG | Verfahren zur katalytischen Gasphasenoxidation von Kohlenwasserstoffen und Katalysereaktionsvorrichtung |
BR112015031535B1 (pt) | 2014-04-24 | 2021-09-21 | Clariant International Ltd. | Arranjo de catalisadores com fração de vazios otimizada, seu uso e processo de preparação de anidrido de ácido ftálico |
DE102014005939A1 (de) * | 2014-04-24 | 2015-10-29 | Clariant International Ltd. | Katalysatoranordnung mit optimierter Oberfläche zur Herstellung von Phthalsäureanhydrid |
EP3047904A1 (de) | 2015-01-22 | 2016-07-27 | Basf Se | Katalysatorsystem zur Oxidierung von O-Xylen und/oder Naphthalen zu Phthalsäureanhydrid |
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DE19839001A1 (de) | 1998-08-27 | 2000-03-02 | Basf Ag | Schalenkatalysatoren für die katalytische Gasphasenoxidation von aromatischen Kohlenwasserstoffen |
EP1063222A1 (de) | 1999-06-24 | 2000-12-27 | Nippon Shokubai Co., Ltd. | Verfahren zur Herstellung von Phthalsäureanhydrid |
DE10237818A1 (de) | 2002-07-29 | 2004-02-19 | Huhtamaki Ronsberg, Zweigniederlassung Der Huhtamaki Deutschland Gmbh & Co. Kg | Isolierung für Flaschen o. dgl. |
DE10323461A1 (de) | 2003-05-23 | 2004-12-09 | Basf Ag | Herstellung von Aldehyden, Carbonsäuren und/oder Carbonsäureanhydriden mittels Vanadiumoxid, Titandioxid und Antimonoxid enthaltender Katalysatoren |
DE10323817A1 (de) | 2003-05-23 | 2004-12-09 | Basf Ag | Verfahren zur Herstellung von Phthalsäureanhydrid |
DE102004026472A1 (de) | 2004-05-29 | 2005-12-22 | Süd-Chemie AG | Mehrlagen-Katalysator zur Herstellung von Phthalsäureanhydrid |
WO2006092304A1 (de) | 2005-03-02 | 2006-09-08 | Süd-Chemie AG | Verwendung eines mehrlagen -katalysators zur herstellung von phthalsäureanhydrid |
WO2006092305A1 (de) | 2005-03-02 | 2006-09-08 | Süd-Chemie AG | Verfahren zur herstellung eines mehrlagen-katalysators zur erzeugung von phthalsäureanhydrid |
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TW415939B (en) * | 1996-10-23 | 2000-12-21 | Nippon Steel Chemical Co | Gas-phase oxidization process and process for the preparation of phthalic anhydride |
DE19707943C2 (de) * | 1997-02-27 | 1999-07-08 | Basf Ag | Verfahren zur Herstellung von Phthalsäureanhydrid und Katalysator hierfür |
DE10334132A1 (de) * | 2003-07-25 | 2005-04-07 | Basf Ag | Silber, Vanadium und ein Promotormetall enthaltendes Multimetalloxid und dessen Verwendung |
DE102004014918A1 (de) * | 2004-03-26 | 2005-10-13 | Basf Ag | Katalysator mit einer Silber-Vanadiumoxidphase und einer Promotorphase |
JP5174462B2 (ja) * | 2004-11-18 | 2013-04-03 | ビーエーエスエフ ソシエタス・ヨーロピア | 触媒を製造するための二酸化チタン混合物の使用 |
CN101472680A (zh) * | 2006-06-20 | 2009-07-01 | 巴斯夫欧洲公司 | 制备羧酸和/或羧酸酐的催化剂体系和方法 |
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2008
- 2008-02-25 DE DE102008011011A patent/DE102008011011A1/de not_active Withdrawn
-
2009
- 2009-01-17 TW TW98101757A patent/TWI466719B/zh active
- 2009-01-28 KR KR1020107018613A patent/KR101620949B1/ko active IP Right Grant
- 2009-01-28 EP EP09707013A patent/EP2247384A2/de not_active Withdrawn
- 2009-01-28 CN CN200980103798.XA patent/CN101939104B/zh active Active
- 2009-01-28 BR BRPI0905796A patent/BRPI0905796A2/pt not_active Application Discontinuation
- 2009-01-28 WO PCT/EP2009/000534 patent/WO2009095216A2/de active Application Filing
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010022830A2 (de) * | 2008-08-29 | 2010-03-04 | Josef Breimair | Katalysator für die katalytische gasphasenoxidation von aromatischen kohlenwasserstoffen zu aldehyden, carbonsäuren und/oder carbonsäureanhydriden, insbesondere zu phthalsäurenanhydrid, sowie verfahren zur herstellung eines solchen katalysators |
WO2010022830A3 (de) * | 2008-08-29 | 2010-05-20 | Josef Breimair | Katalysator für die katalytische gasphasenoxidation von aromatischen kohlenwasserstoffen zu aldehyden, carbonsäuren und/oder carbonsäureanhydriden, insbesondere zu phthalsäurenanhydrid, sowie verfahren zur herstellung eines solchen katalysators |
WO2011032658A1 (de) * | 2009-09-17 | 2011-03-24 | Süd-Chemie AG | Verfahren zur herstellung einer katalysatoranordnung für die herstellung von phthalsäureanhydrid |
US8796173B2 (en) | 2009-09-17 | 2014-08-05 | Süd-Chemie Ip Gmbh & Co. Kg | Method for producing a catalyst arrangement for the production of phthalic anhydride |
Also Published As
Publication number | Publication date |
---|---|
CN101939104B (zh) | 2016-06-01 |
TWI466719B (zh) | 2015-01-01 |
KR101620949B1 (ko) | 2016-05-13 |
TW200946225A (en) | 2009-11-16 |
EP2247384A2 (de) | 2010-11-10 |
DE102008011011A1 (de) | 2009-08-06 |
KR20100111299A (ko) | 2010-10-14 |
BRPI0905796A2 (pt) | 2016-06-21 |
CN101939104A (zh) | 2011-01-05 |
WO2009095216A3 (de) | 2010-04-29 |
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