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WO2005115612A1 - Catalyseur: production et utilisation - Google Patents

Catalyseur: production et utilisation Download PDF

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Publication number
WO2005115612A1
WO2005115612A1 PCT/ZA2005/000074 ZA2005000074W WO2005115612A1 WO 2005115612 A1 WO2005115612 A1 WO 2005115612A1 ZA 2005000074 W ZA2005000074 W ZA 2005000074W WO 2005115612 A1 WO2005115612 A1 WO 2005115612A1
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WO
WIPO (PCT)
Prior art keywords
gold
catalyst
carrier
zinc
metal
Prior art date
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Ceased
Application number
PCT/ZA2005/000074
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English (en)
Inventor
Stephen John Roberts
Gabriele Hildegard Steinbach
Diandree Padayachee
Jason Scott Mcpherson
Gary Pattrick
Elma Van Der Lingen
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Mintek
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Mintek
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Filing date
Publication date
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Publication of WO2005115612A1 publication Critical patent/WO2005115612A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/16—Reducing
    • B01J37/18—Reducing with gases containing free hydrogen
    • 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
    • B01J21/005—Spinels
    • 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
    • B01J23/005—Spinels
    • 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
    • B01J23/48—Silver or gold
    • B01J23/52—Gold
    • 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
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8953—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/03—Precipitation; Co-precipitation
    • B01J37/031—Precipitation
    • 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
    • B01J37/06—Washing

Definitions

  • This invention relates to a catalyst which is suitable for use in the oxidation of carbon monoxide, and to the production and use thereof.
  • Precious metals are known to act as catalysts for the conversion of carbon monoxide to carbon dioxide.
  • US-4839327 discloses catalysts for oxidising carbon monoxide to carbon dioxide comprising an ultra-fine deposit of gold upon metal oxides including MnO 2 , Fe 2 O 3 , CuO, CuMnO 2 , AI 2 O 3 , SiO 2 , TiO 2 .
  • metal oxides including MnO 2 , Fe 2 O 3 , CuO, CuMnO 2 , AI 2 O 3 , SiO 2 , TiO 2 .
  • Taylor et al disclose the use of a mixed oxide of copper and zinc for this purpose.
  • Chinese patent specification CN-1464058 discloses a complex catalyst system which has three active components (Au, Pt and Pd) and at least 2 promoters (Fe, Cu and, optionally, Zn) on a support made of alumina, silica, bentonite or molecular sieve material.
  • Carbon monoxide is a colourless, odourless and highly toxic compound which is produced in many chemical industrial processes or as a product of incomplete combustion e.g. in furnaces or internal combustion engines, as well as in mines.
  • the invention provides a catalyst formed from gold on a carrier which includes at least zinc oxide
  • the carrier may be formed from a mixed oxide of zinc and at least one metal
  • the gold has a particle size less than 100 nanometres (e g below 70 nm), advantageously less than 50 nanometres (e g below 25nm) and desirably less than 10 nanometres (e g 5 nm or lower)
  • the amount of gold is preferably at least 0 01 wt-% of the catalyst, advantageously at least 0 05 wt %, desirably at least 0 5 wt % and conveniently 1 wt-% or more
  • the catalysts tend to be more effective as the amount of gold on the carrier increases
  • the amount of gold on the carrier should not exceed 5 wt-% and is desirably no more than 4 wt-%
  • Gold is easier to deposit upon substrates that have iso-elect ⁇ c points in the pH range from 6 to 10
  • At least one other metal is therefore preferably selected so that the mixed oxide has an iso-elect ⁇ c point of from 6 to 10
  • Pure zinc oxide has an iso-electnc point of about 9, which will alter when mixed with another oxide with a different iso-electnc point
  • Suitable other metals for incorporation in the carrier therefore include aluminium (which forms the oxide AI 2 O 3 which has an iso-electnc point from 8 to 9), cerium (which forms CeO 2 with an iso-elect ⁇ c point of 7), titanium (which forms T ⁇ O 2 with an iso-electnc point of 6), zirconium (which forms ZrO 2 with an iso-electnc point of 6 7), iron (which forms Fe 2 0 3 with an ⁇ so r elect ⁇ point of 6 5-6 9), and copper (which forms cupnc oxide with an iso- elect ⁇ c point of about 6 5)
  • Effective catalysts are those in which the carrier is a mixed oxide of zinc and aluminium or a mixed oxide of copper and zinc
  • the mixed oxide may be in the form of a mixture of two oxides of metals with individual crystal structures, for example a mixture of zinc oxide and aluminium oxide
  • the relative quantities of zinc and the other metal may vary widely
  • the weight ratio of zinc to the other metal in the mixed metal oxide may vary from 100 1 to 1 100, but preferably the range is from 80 1 to 1 80
  • the weight ratios of zinc to the other metal will be at least 5 and preferably at least 6 5 parts of zinc to 80 parts of the other metal
  • Higher relative amounts of zinc can be used, e g 10, 20, 30, 40, 50, 60, 70, or 80 parts of zinc to 80 of the other metal Zinc may be present in greater weight proportions than the other metal, for example in ratios of 2, 5, 10, 20, 30, 40 50, 60, 70 or 80 parts to 1 of the other metal
  • Zinc to other metal weight ratios in the range of 80-20 1 are typically useful, preferably 25-65 1, desirably 35 45:1, especially weight ratios of about 40 1
  • the other metal is at least one of aluminium, graphite, silicon, titanium, zirconium, copper and iron
  • the aforementioned ranges also apply to possible molar ratios of zinc to the other metal
  • the molar ratio of zinc to the other metal may be in the range of 80-1 to 1 80, and intermediate values, eg 2 1 to 1 2
  • the molar ratio of zinc to the other metal is greater than 1 1
  • zinc is the more important metallic element although it may be present in amounts as low as 2% by weight of the catalyst, it is preferably present in amounts of at least 5% by weight, preferably at least 10%, desirably at least 15% and advantageously at least 20%, 25 wt% or 30 wt-%
  • the carrier may be composed predpminantly of zinc oxide, and may contain up to 80% by weight of zinc, for example 75 wt-% or preferably 70 wt-%, or conveniently 65 wt-%, or less, such as 50 wt-%, 45 wt-% or 40 wt-%.
  • the preferred catalysts may be prepared in any appropriate way e.g. by using co- precipitation, impregnation or inverse deposition-precipitation techniques, as described in the specification of South African patent application No 2003/8981.
  • the invention also extends to a method of producing a catalyst of the aforementioned kind wherein an aqueous solution containing at least one water soluble gold compound (for example tetrachloroauric acid, gold cyanide or sodium tetrachloroaurate and other such complexes or compounds) and water soluble salts (for example the nitrates) of zinc and at least one other metal is prepared, using quantities required to produce a desired ratio of gold, zinc and the other metal in the finished mixed metal oxide.
  • the pH of the solution may be increased by the addition of a base such as ammonium or an alkali metal carbonate or hydroxide (e.g.
  • NH 4 OH, NaOH, KOH, Na 2 CO 3 , K 2 CO 3 or Li 2 CO 3 ) or urea to a point at which gold is precipitated simultaneously with the hydroxides, carbonates, hydroxy- carbonates, oxides (or a combination thereof) of zinc and the at least one other metal.
  • This will normally be in the pH range of 7 to 10, depending on the precursors used for the gold and the other metal of the carrier.
  • the resulting gold-bearing catalyst material is separated from the aqueous liquor, washed and dried. Washing is particularly important where the gold is deposited from chloride-containing solutions.
  • the gold catalyst is produced by depositing gold on a carrier material.
  • the carrier may be prepared in a variety ways including, but not limited to, co- precipitation of metal precursors and physical mixing of metal oxides.
  • any commercially available zinc containing carrier can be used with no particular restriction thereon
  • the carrier material generally has a surface area of from 4 to 180 m 2 /g (as determined by the BET/N 2 method (ASTM D3037)
  • Gold may be deposited upon the carrier by treating the carrier with an aqueous solution of a gold precursor compound The amount of gold deposited may be varied by varying the relative proportions of gold solution and carrier.
  • the gold precursor compound may be selected at least from, gold (I) cyanide [AuCN], sodium tetrachloroaurate (III) [NaAuCI 4 ], potassium dicyanoaurate (I) [KAu(CN) 2 ], gold (III) acethylacetonate [(CH 3 ) 2 Au(CH 3 COCH 2 COCH 3 ) and tetrachloroauric (III) acid
  • the gold precursor may be dissolved to form a treatment solution with a gold content in the range of from 1x10 "1 to 1x10 "4 , preferably in the range 1x10 "2 to 5x10 "3 M.
  • the treatment solution may initially have a pH below 7, preferably in the range of from 1 to 3.
  • the pH of the treatment solution may be adjusted to a desired value, e g. from 2 to 8.5, by adding a suitable alkali such as sodium carbonate solution.
  • the relative proportion of these species is dependent on the degree of hydrolysis that the HAuCI 4 species undergoes. As such, the degree of hydrolysis is in part a function of solution pH, with higher pH's promoting further hydrolysis
  • the treatment solution and the carrier are preferably brought into contact at an elevated temperature, preferably in the range 20-90°C , ideally 40-80°C, conveniently 65- 75°C
  • the solution is contacted with the carrier Gold is then precipitated from the solution, for example by increasing the pH of the solution to a desired value by adding an alkaline solution of, for example sodium, potassium or ammonium hydroxide or carbonate, or urea This will normally be in the pH range of 4 to 11.
  • an alkaline solution of, for example sodium, potassium or ammonium hydroxide or carbonate, or urea
  • the pH at which precipitation will occur similarly depends on the nature of the precipitate. [Au(OH) n CI .
  • Gold hydroxide however precipitates at higher pH values, (typically from 7 to 10, preferably 8 to 9.5, ideally about 8.5). This is advantageous because high pH values lead to well-dispersed gold with a low particle size in the nanometre range.
  • the gold species prevalent at high pH values contain less chloride. The presence of chloride species is believed to increase the formation of larger gold particles, thereby decreasing catalytic activity, due to the sintering of the gold particles as a result of the formation of CI-Au-CI bridges.
  • Residual chloride may also serve to poison the catalytic active site.
  • the contacting time of the gold containing solution and the carrier material is performed for a suitable period, for example 0.5 to 3 hours, preferably about 1 hour.
  • the solid material is then separated and washed.
  • the washing is preferably carried out with a base, such as aqueous ammonia solution, NaOH or urea, which also assists in the removal of chloride ions.
  • the catalyst material is dried, preferably at a temperature of from 20 to 150°C, e.g. at 120°C. Further washing with an alkaline solution can be performed on the dried catalyst material to remove excess chloride and other undesired ions, if required.
  • the activity of the catalyst may be modified by further treatment of the gold-bearing carrier.
  • the catalytic mechanism of gold is not fully understood, but may depend upon the presence of both metallic gold (Au°) species and positively charged gold species (Au ⁇ + ).
  • Au° metallic gold
  • Au ⁇ + positively charged gold species
  • the presence of these gold species can be affected by further treatment of the catalyst material.
  • catalyst material obtained by a co-precipitation, impregnation or inverse deposition-precipitation technique may be calcined before use, typically by heating the catalyst material to a temperature from 50 to 500°C (preferably from 100 to 300°C) for a period of from 1 to 5 hours.
  • the effect of calcining is to reduce Au(OH) 3 species present in the catalyst to metallic gold
  • the catalyst material may be treated in a reducing atmosphere, for example hydrogen or, preferably, carbon monoxide Such treatment also affects the nature of the gold species on the surface of the catalyst
  • a 1 34M aqueous solution of zinc nitrate [Zn(NO 3 ) 2 6H 2 O] and a 0 081 M aqueous solution of aluminium nitrate [AI(NO 3 ) 3 9H 2 O] were mixed together in proportions such that the weight ratio zinc aluminium was 40 1
  • the solution was heated to a temperature of approximately 80°C, and the pH of the solution was adjusted from an initial value of 1 1 to a value of 9 1 by adding an aqueous solution of sodium carbonate while stirring, thereby producing a precipitate of the hydroxides of zinc and aluminium
  • the pH and temperature of the solution were maintained to allow the precipitate to age in contact with the solution for about 5 hours
  • the precipitate was filtered from the solution, washed with high-purity water to remove unwanted ions, and dried in air at approximately 120°C for 16 hours
  • the dried precipitate was then calcined by heating in air at 400°C for four hours
  • the resulting earner material (A) was then ground into
  • a volume of deionised water sufficient to support a sample of carrier A in suspension was heated to 70°C.
  • a solution of tetrachloroauric [HAuCU] acid containing sufficient gold was added to the water.
  • the pH of the solution was adjusted from an initial pH of 2 to 5.5 by adding a solution of Na 2 CO 3 . Having stabilised the temperature and pH, the carrier was added, and the suspension agitated for a period of 1 hour. The solid material was separated, washed with a ammonia solution of a desired concentration and dried in air at 120°C.
  • gold, deposited upon alumina alone, does not function as a catalyst for oxidation of CO under the conditions tested.
  • Gold deposited upon zinc oxide shows some catalytic function, but the best catalytic function is exhibited by gold when deposited upon a carrier composed of the mixed oxides of zinc and aluminium, especially when the ratio of zinc to aluminium in the carrier is over 20:1. Also the catalysts with higher gold loading (2% by weight or more) perform more effectively.
  • Examples 9 - 14 Au/CuZnOx catalyst Samples of catalyst material comprising gold on a carrier material consisting of the mixed oxides of copper and zinc were prepared. Carrier Preparation
  • Gold catalysts were produced on the aforementioned carriers by means of inverse deposition precipitation using an aqueous solution of HAuCI 4 of desired concentration. This solution was preheated to 70°C and the pH adjusted to 8.5 by adding Na 2 CO 3 solution. The carrier materials were then added to separate batches of the gold solution and each was aged for 1 hour at 70°C with pH control. Thereafter, the catalyst materials were filtered, washed several times with deionised water, dried in an oven at 120°C for 16 hours and calcined if necessary.
  • a batch of support material was prepared using the method described for Examples 1 to 8, with a Zn:AI ratio of 40:1.
  • the resulting material was treated with gold as described in Examples 9 - 14, with the exception that the solid-liquid contacting (ageing) time and temperatures were varied as shown in Table 4.
  • Supports with zinc to aluminium ratios of 20:1, 40:1 , 80:1 as well as 100% ZnO and 100% AI 2 O 3 were prepared according to the method highlighted in Examples 1 - 8.
  • Gold was deposited onto these carriers as described in Examples 9 - 14. Effect of zinc to aluminium ratio on catalyst activity and gold loading
  • the gold adsorption is also affected by Zn to Al ratios and the highest gold loading was obtained at Zn/AI ratios of 40:1.
  • the alumina catalyst had very low gold loading. This trend is shown in
  • catalysts prepared on G72D are more active than the gold catalysts prepared on the individual metal oxide carriers alone.
  • Gold loading from solution onto the all the carriers is higher at low pH when compared to high pH preparation, the inverse is true for CO oxidation activity.
  • Examples 29 - 37 Au/ZnO impregnated on AbOs
  • gold was deposited or impregnated onto an AI 2 O 3 carrier impregnated with ZnO.
  • a support was prepared comprising a ZnO layer on Al 2 0 3 using one of the following techniques:
  • the mixture was subjected to impregnation described in method (b). Washing, drying and calcining followed as described in method (a).
  • the gold catalyst was prepared by the inverse deposition precipitation method highlighted in Examples 1 - 8.
  • Catalysts were prepared by contacting the necessary amount of carrier material and gold containing solution to obtain a maximum gold loading of 1 wt%.
  • the deposition- precipitation conditions employed are similar to those described in Examples 9 - 14.
  • Catalytic activity was determined using 0.05 - 0.1 g of catalyst in a micro fixed-bed reactor under conditions identical to those described in Examples 9 - 14.
  • Catalysts prepared using the recycled gold solution compare well in terms of gold loading and catalytic activity to their freshly prepared counterpart. Recycling of the gold solution used in catalyst synthesis is possible.
  • a commercially available zinc- aluminium oxide (supplied by S ⁇ d-Chemie under product reference No G72D) was used as the carrier material.
  • Gold catalysts were prepared by depositing gold onto two carriers composed of a commercially available zinc-aluminium oxide (supplied by S ⁇ d-Chemie under product reference No G72D) and a commercially available copper-zinc oxide (supplied by S ⁇ d- Chemie under product reference No G66B). In each case the carrier was crushed and sieved to a particle size in the range 500-1000 ⁇ m. Gold was deposited onto the carrier by an inverse deposition precipitation technique as described in Example 9 - 14.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Catalysts (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un catalyseur utilisé dans l'oxydation de monoxyde de carbone en dioxyde de carbone, qui contient de l'or sur un support d'oxyde de zinc mélangé à au moins un autre métal.
PCT/ZA2005/000074 2004-05-28 2005-05-24 Catalyseur: production et utilisation Ceased WO2005115612A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ZA200404125 2004-05-28
ZA2004/4125 2004-05-28

Publications (1)

Publication Number Publication Date
WO2005115612A1 true WO2005115612A1 (fr) 2005-12-08

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Country Status (6)

Country Link
AR (1) AR051171A1 (fr)
MY (1) MY149330A (fr)
PE (1) PE20060386A1 (fr)
UY (1) UY28921A1 (fr)
WO (1) WO2005115612A1 (fr)
ZA (1) ZA200610870B (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2008169054A (ja) * 2007-01-09 2008-07-24 National Institute Of Advanced Industrial & Technology Ａｌ含有アモルファスマトリックス中に固定化したＺｎＯナノ粒子及びその作製方法
WO2008107445A1 (fr) * 2007-03-05 2008-09-12 Institut Català D'investigació Química (Iciq) Catalyseurs à base d'or pour l'hydrogénation sélective de composés insaturés
WO2009091389A1 (fr) * 2008-01-14 2009-07-23 3M Innovative Properties Company Catalyseurs d'oxydation multifonctionnels et procédés de fabrication
US8058202B2 (en) 2005-01-04 2011-11-15 3M Innovative Properties Company Heterogeneous, composite, carbonaceous catalyst system and methods that use catalytically active gold
US8137750B2 (en) 2006-02-15 2012-03-20 3M Innovative Properties Company Catalytically active gold supported on thermally treated nanoporous supports
WO2009087040A3 (fr) * 2008-01-11 2012-03-29 H.C. Starck Gmbh Poudre de catalyseur
CN103084185A (zh) * 2013-01-25 2013-05-08 天津大学 多元金属氧化物负载金催化剂及其制备方法
WO2015027031A1 (fr) * 2013-08-23 2015-02-26 Basf Corporation Catalyseurs pour l'oxydation de monoxyde de carbone et/ou de composés organiques volatils

Citations (4)

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EP0454022A1 (fr) * 1990-04-23 1991-10-30 Phillips Petroleum Company Catalyseur et procédé pour la déshydrogénation et la déshydrocyclisation
DE4238640A1 (en) * 1991-12-06 1993-06-09 Agency Of Industrial Science & Technology, Ministry Of International Trade & Industry, Tokio/Tokyo, Jp Highly reactive metal oxide and gold catalyst for low temps. - useful for hydrogenation of carbon mono or di:oxide in synthesis of methanol
EP0794006A1 (fr) * 1996-03-08 1997-09-10 Ykk Corporation Catalyseur métal-oxyde métallique et son procédé de fabrication par un traitement d'alliation mécanique
FR2841438A1 (fr) * 2002-06-26 2004-01-02 Rhodia Elect & Catalysis Cigarette comprenant un catalyseur pour le traitement des fumees

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0454022A1 (fr) * 1990-04-23 1991-10-30 Phillips Petroleum Company Catalyseur et procédé pour la déshydrogénation et la déshydrocyclisation
DE4238640A1 (en) * 1991-12-06 1993-06-09 Agency Of Industrial Science & Technology, Ministry Of International Trade & Industry, Tokio/Tokyo, Jp Highly reactive metal oxide and gold catalyst for low temps. - useful for hydrogenation of carbon mono or di:oxide in synthesis of methanol
EP0794006A1 (fr) * 1996-03-08 1997-09-10 Ykk Corporation Catalyseur métal-oxyde métallique et son procédé de fabrication par un traitement d'alliation mécanique
FR2841438A1 (fr) * 2002-06-26 2004-01-02 Rhodia Elect & Catalysis Cigarette comprenant un catalyseur pour le traitement des fumees

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8664149B2 (en) 2005-01-04 2014-03-04 3M Innovative Properties Company Heterogeneous, composite, carbonaceous catalyst system and methods that use catalytically active gold
US8518854B2 (en) 2005-01-04 2013-08-27 3M Innovative Properties Company Heterogeneous, composite, carbonaceous catalyst system and methods that use catalytically active gold
US8314046B2 (en) 2005-01-04 2012-11-20 3M Innovative Properties Company Heterogeneous, composite, carbonaceous catalyst system and methods that use catalytically active gold
US8058202B2 (en) 2005-01-04 2011-11-15 3M Innovative Properties Company Heterogeneous, composite, carbonaceous catalyst system and methods that use catalytically active gold
US8137750B2 (en) 2006-02-15 2012-03-20 3M Innovative Properties Company Catalytically active gold supported on thermally treated nanoporous supports
JP2008169054A (ja) * 2007-01-09 2008-07-24 National Institute Of Advanced Industrial & Technology Ａｌ含有アモルファスマトリックス中に固定化したＺｎＯナノ粒子及びその作製方法
WO2008107445A1 (fr) * 2007-03-05 2008-09-12 Institut Català D'investigació Química (Iciq) Catalyseurs à base d'or pour l'hydrogénation sélective de composés insaturés
EP1970117A1 (fr) * 2007-03-05 2008-09-17 Institut Catala D'Investigacio Quimica Catalyseur à base d'or pour l'hydrogénation sélective de composés insaturés
WO2009087040A3 (fr) * 2008-01-11 2012-03-29 H.C. Starck Gmbh Poudre de catalyseur
EP2253377A3 (fr) * 2008-01-14 2010-12-29 3M Innovative Properties Co. Catalyseurs d'oxydation multifonction
US8236725B2 (en) 2008-01-14 2012-08-07 3M Innovative Properties Company Gold carbon monoxide oxidation catalysts with etched substrate
AU2008348197B2 (en) * 2008-01-14 2011-09-01 3M Innovative Properties Company Multifunctional oxidation catalysts and methods of making
JP2011509824A (ja) * 2008-01-14 2011-03-31 スリーエム イノベイティブ プロパティズ カンパニー 多機能性酸化触媒及び製造方法
CN101952035B (zh) * 2008-01-14 2013-11-06 3M创新有限公司 多功能氧化催化剂及制备方法
WO2009091389A1 (fr) * 2008-01-14 2009-07-23 3M Innovative Properties Company Catalyseurs d'oxydation multifonctionnels et procédés de fabrication
KR101414428B1 (ko) 2008-01-14 2014-07-01 쓰리엠 이노베이티브 프로퍼티즈 컴파니 다기능 산화 촉매 및 제조 방법
CN103084185A (zh) * 2013-01-25 2013-05-08 天津大学 多元金属氧化物负载金催化剂及其制备方法
WO2015027031A1 (fr) * 2013-08-23 2015-02-26 Basf Corporation Catalyseurs pour l'oxydation de monoxyde de carbone et/ou de composés organiques volatils
US9399208B2 (en) 2013-08-23 2016-07-26 Basf Corporation Catalysts for oxidation of carbon monoxide and/or volatile organic compounds

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ZA200610870B (en) 2007-11-28
AR051171A1 (es) 2006-12-27
UY28921A1 (es) 2005-06-30

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