EP1005394A1 - Verfahren zur herstellung von mo, v und cu enthaltenden multimetalloxidmassen - Google Patents

Verfahren zur herstellung von mo, v und cu enthaltenden multimetalloxidmassen

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Publication number
EP1005394A1
EP1005394A1 EP98939640A EP98939640A EP1005394A1 EP 1005394 A1 EP1005394 A1 EP 1005394A1 EP 98939640 A EP98939640 A EP 98939640A EP 98939640 A EP98939640 A EP 98939640A EP 1005394 A1 EP1005394 A1 EP 1005394A1
Authority
EP
European Patent Office
Prior art keywords
starting mass
aqueous solution
mass
aqueous
temperature
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Withdrawn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
EP98939640A
Other languages
German (de)
English (en)
French (fr)
Inventor
Hartmut Hibst
Signe Unverricht
Andreas Tenten
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
Priority claimed from DE19736105A external-priority patent/DE19736105A1/de
Priority claimed from DE19740493A external-priority patent/DE19740493A1/de
Application filed by BASF SE filed Critical BASF SE
Publication of EP1005394A1 publication Critical patent/EP1005394A1/de
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/888—Tungsten
    • B01J23/8885—Tungsten containing also molybdenum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/885—Molybdenum and copper
    • 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
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8877—Vanadium, tantalum, niobium or polonium
    • 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
    • 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
    • B01J37/0081—Preparation by melting
    • 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

Definitions

  • the present invention relates to a process for the preparation of multimetal oxide compositions of the general formula I
  • X 1 W, Nb, Ta, Cr and / or Ce, preferably W, Nb and / or Cr, X2 : Cu, Ni, Co, Fe, Mn and / or Zn, preferably Cu, Ni, Co and / or Fe ,
  • 25 1 to 8, preferably 2 to 6, 0.2 to 5, preferably 0.5 to 2.5, 0 to 23, preferably 0 to 4, 0 to 50, preferably 0 to 3, 0 to 2, preferably 0 to 0.3,
  • P Numbers other than zero, their ratio p / q 160: 1 to 1: 1, preferably 20: 1 to 1: 1 and particularly preferably
  • starting mass 1 45 separately in finely divided form (starting mass 1) and then the preformed solid starting mass 1 in an aqueous solution of sources of the elements Mo, V, X 1 , X 2 , X 3 , X 4 , ⁇ 5 # X 6 , which the aforementioned elements in stoichiometry A
  • Multimetal oxide compositions of the general formula I are e.g. known from DE-A 19528646 and find e.g. in gas-phase catalytic oxidations of organic compounds such as alkanes, alkanols, alkanals, alkenes and alkenols (preferably propylene, acrolein, methacrolein, tert-butanol, methyl ether of tert-butanol, isobutene, isobutane), preferably having 3 to 6 carbon atoms or isobutyraldehyde) to olefinically unsaturated aldehydes and / or carboxylic acids, and the corresponding nitriles (ammoxidation, especially from propene to acrylonitrile and from isobutene or tert-butanol to methacrylonitrile) are used as catalysts.
  • organic compounds such as alkanes, alkanols, alkanals, alkenes and al
  • DE-A 19528646 recommends the preparation of the multimetal oxide compositions as described at the beginning, the incorporation of the solid starting composition 1 into the aqueous starting composition 2 in all cases at a temperature in the exemplary embodiments . 80 ° C takes place.
  • DE-A 19528646 does not contain any further details on the incorporation temperature.
  • a disadvantage of the aforementioned preparation method of DE-A 19528646 is that when the resulting multimetal oxide compositions I are used as catalysts for the gas-phase catalytic oxidation of acrolein to acrylic acid, the selectivity of the formation of acrylic acid cannot be fully satisfied.
  • EP-A 668 104 takes place as described in DE-A 19528646.
  • EP-A 668104 makes essentially no information about the incorporation temperature of the solid starting mass 1 into the aqueous starting mass 2.
  • the object of the present invention was therefore to provide an improved process for the preparation of multimetal oxide compositions I which no longer has the aforementioned disadvantage.
  • a process for the preparation of multimetal oxide compositions I as described in the introduction is found, which is characterized in that the solid starting composition 1 is incorporated into the aqueous starting composition 2 at a temperature ⁇ 70 ° C.
  • the incorporation temperature is preferably ⁇ 60 ° C, and particularly preferably ⁇ 40 ° C. As a rule, incorporation will take place at room temperature, so that the incorporation temperature is generally> 0 ° C.
  • the finely divided starting mass 1 advantageously consists of particles whose size diameter d ß (longest connecting section through the center of gravity of the particles of two points located on the surface of the particles)> 0 to 300 ⁇ m, preferably 0.1 to 200 ⁇ m, particularly preferably 0 , 5 to 50 ⁇ m and very particularly preferably 1 to 30 ⁇ m.
  • the particle diameter d ß can also be 10 to 80 ⁇ m or 75 to 125 ⁇ .
  • the starting material 1 to be used according to the invention has a specific surface area 0 B (determined according to DIN 66131 by gas adsorption (N 2 ) according to Brunauer-Emmet-Teller (BET)) ⁇ 20 m 2 / g, preferably ⁇ 5 m 2 / g and very particularly preferably ⁇ 1 m 2 / g.
  • 0 B > 0.1 m 2 / g.
  • the starting material 1 can be used according to the invention both amorphously and / or crystalline.
  • the starting mass 1 consists of crystallites of oxometalates or contains those oxometal crystallites which have the X-ray diffraction pattern and thus the crystal structure type of at least one of the subsequent copper molybdates (the expression in brackets represents the source for the associated X-ray diffraction fingerprint) or if that Starting mass 1 consists of crystallites of these copper molybdates or contains such copper molybdate crystallites:
  • Multimetal oxide compositions B which contain or consist of oxometalates, which have the X-ray diffraction pattern and thus the crystal structure type of the subsequent copper molybdate, or which themselves contain or consist of copper molybdate, are advantageous according to the invention:
  • B + C 0 to 1, preferably 0 to 0.7
  • y is a number determined by the valency and frequency of elements other than oxygen
  • y is a number determined by the valency and frequency of elements other than oxygen
  • y a number determined by the valency and frequency of elements other than oxygen.
  • oxometalates or starting materials B are disclosed, for example, in EP-A 668 104.
  • Suitable multimetal oxide compositions B are also those which contain oxometalates of the stochiometry VI below
  • y a number determined by the valency and frequency of the elements other than oxygen
  • HT copper molybdate structure a structure type, which is referred to as HT copper molybdate structure and is subsequently defined by its X-ray diffraction pattern (fingerprint), reproduced by its most characteristic and most intense diffraction lines in the form of network plane spacings d [ ⁇ ] which are independent of the wavelength of the X-radiation used:
  • the multimetal oxide mass B contains or consists of a mixture of different oxometalates
  • a mixture of oxometalates with a tungsten and HT copper molybdate structure is preferred.
  • the weight ratio of crystallites with HT copper molybdate structure to crystallites with tungsten structure can be 0.01 to 100, 0.1 to 10, 0.25 to 4 and 0.5 to 2.
  • multimetal oxide compositions B which are suitable according to the invention can be prepared in a simple manner by producing an intimate, preferably finely divided, dry mixture which is composed in accordance with their stochiometry from suitable sources of their elemental constituents and this at temperatures of 200 to 1000 ° C., preferably 250 to 800 ° C, calcined for several hours under inert gas or preferably in air, the calcination time being from a few minutes to a few hours.
  • the calcination atmosphere can additionally contain water vapor.
  • Suitable sources for the elemental constituents of the multimetal oxide mass B are those compounds which are already oxides and / or those compounds which can be converted into oxides by heating, at least in the presence of oxygen.
  • such starting compounds are, above all, halides, nitrates, formates, oxalates, citrates, acetates, carbonates,
  • Ammine complex, ammonium salts and / or hydroxides compounds such as NH 4 OH, (NH 4) 2 C0 3, NH 4 N0 3, NH 4 CH0 2, CH 3 COOH, NH 4 CH 3 C0 2 or ammonium oxalate, the can be broken down and / or decomposed at the latest when calcining later to form completely gaseous compounds, can also be incorporated).
  • the intimate mixing of the starting compounds for the production of multimetal oxide compositions B can take place in dry or in wet form. If it is carried out in dry form, the starting compounds are expediently used as finely divided powders and, after mixing and optionally compacting, are subjected to the calcination.
  • the intimate mixing is preferably carried out in wet form.
  • the starting compounds are mixed together in the form of an aqueous solution and / or suspension.
  • Particularly intimate dry mixtures are obtained in the dry process described if only sources of the elementary constituents present in dissolved form are used.
  • a solution medium is preferably water.
  • the aqueous mass obtained is then dried, the drying process preferably by spray drying the aqueous mixture with
  • the mixture of the starting compounds used is thermally treated in an overpressure vessel (autoclave) in counter
  • the pressure range typically extends up to 500 atm, preferably up to 250 atm. This hydrothermal treatment is particularly advantageously carried out in the temperature range from> 100 to
  • the multimetallic oxide masses B, 20 obtainable as described above can contain the oxometalates of a single structural type or a mixture of oxometalates of different structural types or consist exclusively of oxometalates of a single structural type or a mixture of oxometalates of different structural types can now, optionally after grinding 25 and / or Classification to desired sizes, e.g. can be used as a solid starting mass 1.
  • the starting compounds in particular are halides, nitrates, formates, oxalates,
  • citrates, acetates, carbonates and / or hydroxides into consideration compounds such as NH 4 0H, (NH 4 ) 2 C0 3 , NH 4 HC0 3 , NH 4 N0 3 , NH 4 CHO 2 , CH 3 COOH or NHCH 3 C0 2 which can disintegrate and / or decompose at the latest during the later calcination to give completely gaseous compounds, can also be incorporated).
  • Particularly suitable starting compounds of Mo, V, W and Nb are also their oxo compounds (molybdates, vanadates, tungstates and niobates) or the acids derived therefrom.
  • the Mo content of such aqueous solutions which are cooled to temperatures of up to 20 ° C. or below (usually not below 0 ° C.) and are suitable as starting material 2, based on the solution, is not more than 35% by weight.
  • multimetal oxide materials I prepared according to the invention using aqueous solutions prepared as starting material 2 for the preparation of which the fine-particle starting material 1 is incorporated at low temperature
  • aqueous solutions prepared as starting material 2 for the preparation of which the fine-particle starting material 1 is incorporated at low temperature
  • partial gas phase Oxidation of acrolein to acrylic acid lead to higher acrylic acid selectivities.
  • T L 60 60 ° C (for example at up to 65 ° C, or at up to 75 ° C, or at up to 85 ° C, or at up to 95 ° C or at ⁇ 100 ° C) an aqueous solution suitable as starting mass 2 is produced.
  • T E ⁇ T L After cooling to a temperature T E ⁇ T L, the finely divided solid starting material 1 is then incorporated into this aqueous solution.
  • T L will be > 70 ° C and T E ⁇ 70 ° C.
  • T L > 60 ° C is also possible.
  • the preparation of the prepared solid starting mass 1 into the aqueous starting mass 2 is usually carried out by adding the starting mass 1 into the, as already stated, cooled aqueous starting mass 2 and subsequent mechanical mixing, e.g. using stirring or dispersing agents over a period of a few hours to several days, preferably in a period of several hours.
  • the solid starting mass 1 is incorporated into the aqueous starting mass 2 at temperatures ⁇ 70 ° C., preferably at temperatures ⁇ 60 ° C. and particularly preferably at temperatures ⁇ 40 ° C.
  • the incorporation temperature will be> 0 ° C.
  • the solid starting mass 1 is incorporated into an aqueous starting mass 2, the pH of which is 4 to 7, preferably 5 to 6.5, at 25 ° C.
  • the latter can e.g. can be achieved by adding one or more pH buffer systems to the aqueous starting mass 2.
  • An addition of ammonia and acetic acid and / or formic acid or an addition of ammonium acetate and / or ammonium formate is suitable as such.
  • ammonium carbonate can also be used with regard to the aforementioned purpose.
  • the drying of the aqueous mixture obtained when the starting material 1 is incorporated into the aqueous starting material 2 is usually carried out by spray drying. Outlet temperatures of 100 to 150 ° C. are expediently set. It can be spray dried both in cocurrent and in countercurrent.
  • the shaping to the desired catalyst geometry is preferably carried out by application to preformed inert catalyst carriers, it being possible for the application to take place before or after the final calcination.
  • the relevant 5 precursor mass is calcined before the carrier coating.
  • Coating of the support bodies for the production of the coated catalysts is generally carried out in a suitable rotatable container, such as that e.g. is known from DE-A 2909671 or from EP-A 293859.
  • a suitable rotatable container such as that e.g. is known from DE-A 2909671 or from EP-A 293859.
  • the carrier bodies moisten the powder mass to be applied and after application, e.g. by means of hot air.
  • the layer thickness of the powder composition applied to the carrier body is expediently selected in the range from 50 to 500 ⁇ m, preferably in the range from 150 to 250 ⁇ m.
  • carrier materials Conventional porous or non-porous aluminum oxides, silicon dioxide, thorium dioxide, zirconium dioxide, silicon carbide or silicates such as magnesium or aluminum silicate can be used as carrier materials.
  • the carrier bodies can be used regularly or incorrectly.
  • 25 supports made of steatite, the diameter of which is 1 to 8 mm, preferably 4 to 5 mm.
  • precursor mass obtained in the course of the process according to the invention during spray drying can also be used for the precursor mass obtained in the course of the process according to the invention during spray drying.
  • the precursor mass is compressed before or after the calcination to the desired catalyst geometry (e.g. by tableting, extrusion or extrusion), where appropriate the auxiliaries which are customary per se, such as e.g. Graphite or stearic acid as
  • 35 lubricants and / or molding aids and reinforcing agents such as microfibers made of glass, asbestos, silicon carbide or potassium titanate can be added.
  • Preferred all-catalyst geometries are hollow cylinders with an outer diameter and a length of 2 to 10 mm and a wall thickness of 1 to 3 mm.
  • the calcination can be carried out under inert gas (eg N 2 ), a mixture of inert gas and oxygen (eg air), with reducing gases such as coal Hydrogen (for example methane), aldehydes (for example acrolein) or ammonia, but also under a mixture of O 2 and reducing gases (for example all of the above) are carried out, as described for example in DE-A 4335973.
  • inert gas eg N 2
  • reducing gases such as coal Hydrogen (for example methane), aldehydes (for example acrolein) or ammonia
  • reducing gases for example methane
  • the multimetal oxide compositions I obtainable according to the invention are particularly suitable as catalysts with increased selectivity (for a given conversion) for the gas-phase catalytic oxidation of acrolein to acrylic acid.
  • Acrolein which was generated by the catalytic gas phase oxidation of propene, is normally used in the process.
  • the reaction gases of this propene oxidation containing acrolein are used without intermediate purification.
  • Gas-phase catalytic oxidation of acrolein in tube-bundle reactors is usually carried out as a heterogeneous fixed bed oxidation. Oxygen, expediently diluted with inert gases (for example in the form of air), is used as the oxidizing agent in a manner known per se.
  • Suitable dilution gases are, for example, N 2 , CO 2 , hydrocarbon, recycled reaction gases and / or water vapor.
  • the reaction pressure is generally 1 to 3 bar and the total space load is preferably 1000 to 3500 Nl / (lh).
  • Typical multi-tube fixed bed reactors are described, for example, in the documents DE-A 28 30 765, DE-A 22 01 528 or US-A 3 147 084.
  • the reaction temperature is usually chosen so that the acrolein conversion in a single pass is above 90%, preferably above 98%. Normally, reaction temperatures of 230 to 330 ° C are required.
  • the process products according to the invention are also capable of gas-phase catalytic oxidation of other organic compounds such as, in particular, other alkanes, alkanols, alkanals, alkenes and alkenols (for example propylene, methacrolein, tert.) which preferably have 3 to 6 carbon atoms -Butanol, methyl ether of tert-butanol, isobutene, isobutane or isobutyraldehyde) to give olefinically unsaturated aldehydes and / or carboxylic acids, and the corresponding nitriles (ammoxidation, especially of propene to acrylonitrile and from isobutene or tert.
  • other alkanes alkanols, alkanals, alkenes and alkenols (for example propylene, methacrolein, tert.)
  • alkenes and alkenols for example propy
  • acrolein, methacrolein and methacrylic acid may be mentioned by way of example. However, they are also suitable for the oxidative dehydrogenation of olefinic compounds.
  • turnover, selectivity and residence time are defined as follows:
  • the temperature of the solution was then reduced to 40 ° C. 10
  • the solution remained clear and precipitation-free.
  • starting mass 2 The clear, orange-colored solution obtained (starting mass 2) was then cooled to 25 ° C. 172.7 g of the starting mass 1 were stirred into the starting mass 2 cooled to 25 ° C., so that the molar ratio of the aforementioned stoichiometric
  • starting mass 1 20 units 1 (starting mass 1) was 6.5 (starting mass 2). Subsequently, 150.0 g of ammonium acetate were stirred into the aqueous suspension, the resulting suspension was stirred at 25 ° C. for 1 h and then the aqueous mixture was spray-dried. After that, the spray powder was mixed with
  • the modeling clay was first heated to 210 ° C. in 20 minutes, then heated to 400 ° C. in the course of 5 hours and then held at this temperature for 3 hours.
  • the resulting catalytically active material had the following gross stoichiometry:
  • the X-ray diffractogram of the active composition obtained still contained the superposition of the tungsten structure type and HT-copper 45 molybdate structure type. After the calcined active material had been ground, it was used to turn non-porous and surface-rough steatite balls with a diameter of 4 to 5 mm in a rotary drum an amount of 50 g of active powder per 200 g of steatite balls with the simultaneous addition of 18 g of water. The shell catalyst obtained was then dried with hot air at 110 ° C.
  • the clear, orange-colored solution obtained (starting mass 2) was then cooled to 25 ° C. and 116.9 g of acetic acid and 132.3 g of ammonia solution (25% by weight of ammonia in water) were added to this in succession. 172.7 g of the starting mass 1 were stirred into the starting mass 2, which had been cooled and buffered to 25 ° C., so that the molar ratio of the aforementioned stoichiometric units 1 (starting mass 1) to 6.5 (starting mass 2). The suspension obtained was stirred at 25 ° C. for 1 h. The aqueous mixture obtained was then spray dried and processed as in Example 3.
  • Example 3 The procedure was as in Example 3. Deviating from this, however, the starting mass 1 was stirred into the aqueous starting mass 2 at 95 ° C. and the resulting suspension was stirred at 95 ° C. for 1 h after the addition of ammonium acetate.
  • the multimetal oxide catalysts produced in Examples 3, 4 and in Comparative Example 2 were placed in a tubular reactor (V2A steel, 25 mm inner diameter, 2000 g of catalyst bed, salt bath temperature control) and at reaction temperatures in the

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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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Catalysts (AREA)
EP98939640A 1997-08-20 1998-07-25 Verfahren zur herstellung von mo, v und cu enthaltenden multimetalloxidmassen Withdrawn EP1005394A1 (de)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
DE19736105 1997-08-20
DE19736105A DE19736105A1 (de) 1997-08-20 1997-08-20 Verfahren zur Herstellung von Multimetalloxidmassen
DE19740493 1997-09-15
DE19740493A DE19740493A1 (de) 1997-09-15 1997-09-15 Verfahren zur Herstellung von Multimetalloxidmassen
PCT/EP1998/004665 WO1999008788A1 (de) 1997-08-20 1998-07-25 Verfahren zur herstellung von mo, v und cu enthaltenden multimetalloxidmassen

Publications (1)

Publication Number Publication Date
EP1005394A1 true EP1005394A1 (de) 2000-06-07

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EP98939640A Withdrawn EP1005394A1 (de) 1997-08-20 1998-07-25 Verfahren zur herstellung von mo, v und cu enthaltenden multimetalloxidmassen

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EP (1) EP1005394A1 (pt)
JP (1) JP2001515004A (pt)
KR (1) KR20010023081A (pt)
CN (1) CN1267236A (pt)
AU (1) AU8807798A (pt)
BR (1) BR9811310A (pt)
CA (1) CA2301704A1 (pt)
WO (1) WO1999008788A1 (pt)

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Publication number Priority date Publication date Assignee Title
JP4182237B2 (ja) * 1997-09-30 2008-11-19 住友化学株式会社 イソブタンの気相接触酸化反応用触媒およびこれを用いてなるアルケンおよび／または含酸素化合物の製造方法
MY121878A (en) * 1999-03-10 2006-02-28 Basf Ag Method for the catalytic gas-phase oxidation of propene into acrylic acid
JP4793962B2 (ja) * 1999-10-12 2011-10-12 日立マクセルエナジー株式会社 リチウム電池用正極活物質およびそれを用いたリチウム電池
JP2004532725A (ja) * 2001-05-31 2004-10-28 オーストラリアン ニュークリア サイエンス アンド テクノロジー オーガニゼーション 汚染金属イオンを液体の流れから除去する無機イオン交換体
JP2005205263A (ja) * 2004-01-20 2005-08-04 Mitsubishi Chemicals Corp 複合酸化物触媒の製造方法。
CN101618327B (zh) * 2007-12-21 2011-06-08 中国科学院山西煤炭化学研究所 一种甲烷氧化合成甲醇和甲醛的催化剂及制法和应用
CN105597773B (zh) * 2014-11-20 2018-05-11 中国石油化工股份有限公司 烯烃氧化制不饱和醛及不饱和酸的催化剂

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Publication number Priority date Publication date Assignee Title
EP0668104B1 (de) * 1994-02-22 1999-05-19 BASF Aktiengesellschaft Multimetalloxidmassen.
DE19528646A1 (de) * 1995-08-04 1997-02-06 Basf Ag Multimetalloxidmassen
DE19542755A1 (de) * 1995-11-16 1997-05-22 Basf Ag Multimetalloxide

Non-Patent Citations (1)

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Title
See references of WO9908788A1 *

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CN1267236A (zh) 2000-09-20
CA2301704A1 (en) 1999-02-25
JP2001515004A (ja) 2001-09-18
KR20010023081A (ko) 2001-03-26
AU8807798A (en) 1999-03-08
WO1999008788A1 (de) 1999-02-25
BR9811310A (pt) 2000-08-29

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